CN109423558A - A kind of technique of municipal administration and metallurgical difficult solid waste collaboration resource utilization - Google Patents

A kind of technique of municipal administration and metallurgical difficult solid waste collaboration resource utilization Download PDF

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Publication number
CN109423558A
CN109423558A CN201710743661.7A CN201710743661A CN109423558A CN 109423558 A CN109423558 A CN 109423558A CN 201710743661 A CN201710743661 A CN 201710743661A CN 109423558 A CN109423558 A CN 109423558A
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China
Prior art keywords
gas
delivered
calciner
powder
section
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CN201710743661.7A
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Chinese (zh)
Inventor
叶恒棣
周志安
范晓慧
刘水石
甘敏
李康
刘海玉
代友训
夏春才
景涛
苏道
李文林
李继淦
杨正伟
邬斌
陈宇
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Central South University
Zhongye Changtian International Engineering Co Ltd
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Central South University
Zhongye Changtian International Engineering Co Ltd
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Priority to CN201710743661.7A priority Critical patent/CN109423558A/en
Publication of CN109423558A publication Critical patent/CN109423558A/en
Pending legal-status Critical Current

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    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00Working 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
    • C22B7/02Working-up flue dust
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00Preliminary treatment of ores or scrap
    • C22B1/02Roasting processes
    • C22B1/08Chloridising roasting
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00Preliminary treatment of ores or scrap
    • C22B1/14Agglomerating; Briquetting; Binding; Granulating
    • C22B1/24Binding; Briquetting ; Granulating
    • C22B1/2406Binding; Briquetting ; Granulating pelletizing
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B13/00Obtaining lead
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B15/00Obtaining copper
    • C22B15/0002Preliminary treatment
    • C22B15/001Preliminary treatment with modification of the copper constituent
    • C22B15/0013Preliminary treatment with modification of the copper constituent by roasting
    • C22B15/0019Chloridizing roasting
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B19/00Obtaining zinc or zinc oxide
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00Technologies related to metal processing
    • Y02P10/20Recycling

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • Manufacturing & Machinery (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

A kind of technique of municipal administration and metallurgical difficult solid waste collaboration resource utilization, the technique is the following steps are included: 1) ingredient: by the metallurgical dust in the incineration of refuse flyash and metallurgical dust storehouse in incineration of refuse flyash storehouse after vibration bucket, batcher, being delivered to mixing arrangement;2) mix: mixing arrangement is mixed, and obtains mixed powder;3) profit mill: carrying out profit mill for mixed powder, the mixed powder after obtaining profit mill;4) pelletizing: the mixed powder after profit mill is granulated, and powder pelletizing is obtained;5) dry: powder pelletizing is dried, the powder pelletizing after being dried;6) preheat: the powder pelletizing after dry is preheated, the powder pelletizing after being preheated;7) roast: the powder pelletizing after preheating carries out high temperature chlorination roasting.The present invention using incineration of refuse flyash as chlorinating agent, using the heavy metal metallurgies dust such as the leaded, zinc of high temperature chlorination roasting process, fume treatment and the recycling of valuable metal etc..

Description

A kind of technique of municipal administration and metallurgical difficult solid waste collaboration resource utilization
Technical field
The present invention relates to solid waste resource recoveries to utilize field, more particularly to is a kind of municipal administration and the difficult solid waste of metallurgy The technique for cooperateing with resource utilization, or make a kind of technique that incineration of refuse flyash is utilized with ferrous metallurgy powder dust resources.It is main It solves incineration of refuse flyash and metallurgical solid waste and does not dispose bring environment and social concern properly.
Background technique
With the accelerated development of China's urbanization, the yield of China's municipal refuse is continuously increased.Current garbage disposal is main It is landfill, burning and compost, wherein burning disposal has the advantages that volume reduction, decrement, while can also generate electricity, and obtains in recent years It is widely applied.But the by-product flying dust that waste incineration generates, it is a kind of dangerous gurry, because flying dust is enriched with dioxin, a huge sum of money The pollutants such as category and chlorine, harm is big, handles hardly possible, easy secondary pollution.Domestic and international flying dust method of disposal mainly has cement solidification, medicament Stabilization, hot setting etc., cement solidification or chemical stabilization processing land occupation is big, heavy metal long-time stability are poor, and hot setting Investment is big, output is low.
Ferrous metallurgical industry be to resource and can source height recycle renewable resources industry, it is fast with China's steel industry Speed development, steel production capacity sharply increase, and iron and steel enterprise generates a large amount of metallurgical slag and metallurgical dust in process of production, causes The increasingly increase of environmental pollution pressure.As country continues to increase the pollution degree of control, metallurgical slag and metallurgical dust Administer the great attention for being subjected to the whole industry.
Ferrous Metallurgy dust is the higher solid waste of iron content mostly, according to its source, can be divided into sintering dust, Blast furnace dust, electric furnace/converter dust, nonferrous metallurgy ion dust mud contaning etc., currently, the main method of steel plant's disposition metallurgical dust is Sintering will be returned after dust collection, because the fluctuation of its chemical constituent is larger, when supplying is sintered, Yi Yinqi sinter quality is unstable, Further, since mostly element containing effumability, such as lead, zinc, alkali metal etc., meeting constantly recycle rich in blast furnace in metallurgical dust Collection, causes furnace nodulation, to constrain the scale processing of metallurgical dust, causes a large amount of dust that can only fill or stack, The waste of land resource is not only caused, pollution is brought to environment, also causes the waste of the valuable element in metallurgical dust.
Metal and its oxide and other complex compounds, under certain condition, the overwhelming majority can be with chemical activity very High chlorine forms metal chloride.Various metal chlorides compared with other compounds of respective metal, mostly have low melting point, High volatile, the easily properties such as being reduced property, the subsequent nature difference according to chloride, can effectively realize respectively metal separation, Enrichment, the purpose extracted and refined, but chloridising roasting process needs to consume expensive chlorinating agent, to limit its big rule Application and the development of mould.
Summary of the invention
Incineration of refuse flyash is the thin particulate matter trapped in garbage burning factory flue gas purification system and heat recovery system, about The 3~5% of the amount of burning away the refuse are accounted for, are a kind of solid waste in typical city, but wherein contain about 15% chlorine element, needle The characteristics of to the difficulty in treatment and incineration of refuse flyash of the heavy metal metallurgies dust containing zinc etc. at present, the purpose of the present invention is by flying dust Cooperative disposal is carried out with metallurgical dust, waves weight (alkali) metal such as the lead in metallurgical dust, zinc, potassium, sodium using the chlorine in flying dust Hair enrichment, while making dioxin high temperature degradation, not only dispose flying dust properly, also the low iron-bearing material of acquisition impurity content With the flue dust for being rich in valuable metal, the comprehensive utilization in city and metallurgical solid waste is realized.The present invention is using incineration of refuse flyash as chlorine Agent, using heavy metal metallurgies dust such as the leaded, zinc of high temperature chlorination roasting process, main processes include following work Sequence: ingredient, mixing, profit mill, pelletizing is dry, preheats, and roasts, cooling, fume treatment and the recycling of valuable metal etc..
The first embodiment provided according to the present invention provides a kind of municipal administration and metallurgical difficult solid waste collaboration recycling The system utilized, or make a kind of incineration of refuse flyash and high temperature chlorination roasting is cooperateed with to realize resource utilization with Ferrous Metallurgy dust System.
The system of a kind of municipal administration and metallurgical difficult solid waste collaboration resource utilization, the system include:
1) proportioner: proportioner includes feed bin;
2) mixing arrangement: the discharge port of feed bin is connected by the feed inlet of the first mineral aggregate conveying device and mixing arrangement;
3) damp mill: the discharge port of mixing arrangement is connected by the feed inlet of third mineral aggregate conveying device and damp mill;
4) pelletizer: the discharge port of damp mill is connected by the feed inlet of the 4th mineral aggregate conveying device and pelletizer;
5) drying device: the discharge port of pelletizer is connected by the feed inlet of the 5th mineral aggregate conveying device and drying device;
6) preheating device: the discharge port of drying device is connected by the feed inlet of the 6th mineral aggregate conveying device and preheating device It connects;
7) calciner: the discharge port of preheating device is connected by the feed inlet of the 7th mineral aggregate conveying device and calciner It connects.
Preferably, the system further include:
8) cooling device.The discharge port of calciner is connected by the feed inlet of the 8th mineral aggregate conveying device and cooling device It connects.
Preferably, the discharge port of cooling device is connected to blast furnace ironmaking workshop by the 9th mineral aggregate conveying device.
Preferably, the system further include: 9) flue gas processing device.The exhanst gas outlet of calciner is defeated by the 9th gas The smoke inlet of pipeline and flue gas processing device is sent to connect.
Preferably, proportioner includes feed bin, vibration bucket, batcher, feed bin includes incineration of refuse flyash storehouse and metallurgy Dust cabin, two vibration buckets are separately positioned on the lower section of the respective discharge port in incineration of refuse flyash storehouse and metallurgical dust storehouse, feed The lower section of vibration bucket discharge port is arranged in machine;The discharge port of batcher passes through the charging of the first mineral aggregate conveying device and mixing arrangement Mouth connection.
Preferably, the mixing arrangement includes digester and intensive mixer.The discharge port of batcher passes through the first mine The discharge port of the connection of the feed inlet of material conveying device and digester, digester passes through the second mineral aggregate conveying device and intensive mixer Feed inlet connection, the discharge port of intensive mixer connected by the feed inlet of third mineral aggregate conveying device and damp mill.
Preferably, the drying device includes blasting drying period and down-draft drying zone.It is run along flying dust and dust The upstream of down-draft drying zone is arranged in direction, blasting drying period.
Preferably, cooling device includes High-temperature cooling section, medium temperature cooling section, sub-cooled section.Along flying dust and dust The direction of operation, High-temperature cooling section, medium temperature cooling section, sub-cooled section are set gradually.
Preferably, the flue gas processing device includes first segment spray and second segment spray.It is discharged along calciner The direction of flue gas, first segment spray and second segment spray are set gradually.Or, it is preferred that the flue gas processing device includes Porous film dust-remover;It is further preferred that porous film dust-remover is flexible film dust-remover or ceramic film dust-remover.Preferably, soft Property film is intermetallic compound flexible membrane.Porous film dust-remover is a kind of corrosion-resistant, anti-oxidant, thermal shock resistance, wear-resistant, anti-clogging Film dust-remover.
Preferably, the flue gas processing device be dry method flue gas processing unit, the device include high temperature section reclaimer, Middle-temperature section reclaimer, low-temperature zone reclaimer;It (is arranged in other words along calciner along the direction of calciner discharge flue gas The direction that flue gas is run in flue gas processing device out), high temperature section reclaimer, middle-temperature section reclaimer, low-temperature zone recycling are set It is standby to set gradually.
In the present invention, the exhanst gas outlet of second segment spray is connected to chimney by the tenth gas transmission pipeline.
Optionally, demister and/or corrosive resistant fan and/or purification device are successively arranged on the tenth gas transmission pipeline.
In the present invention, the exhanst gas outlet of low-temperature zone recycling is connected to chimney by the tenth gas transmission pipeline.Optionally, Deduster and/or corrosive resistant fan and/or purification device are successively arranged on tenth gas transmission pipeline.Preferably, deduster is Porous film dust-remover.
Preferably, the system further include: the liquid outlet of first segment spray passes through the first liquid transporting apparatus and filtering Device connection.Filter device includes liquid outlet and solid outlet, and the liquid outlet of filter device passes through the 4th liquid conveying dress It sets and is connect with filter-pressing device.
Preferably, the liquid outlet of second segment spray is connected to acid-base neutralization device by second liquid conveying device.
Preferably, the solid outlet of the solid outlet of filter device and filter-pressing device is defeated by the tenth mineral aggregate conveying device It send to valuable metal recovery device.
Preferably, the recycling outlet connection copper recyclable device of high temperature section reclaimer, the recycling of middle-temperature section reclaimer Outlet connection lead recyclable device, the recycling outlet connection zinc recovering device of low-temperature zone reclaimer.Preferably, the powder of deduster Dirt exports the feed inlet that intensive mixer is connected to by dust conveyer.
In the present invention, the digester is equipped with chloride entrance.The damp mill is equipped with additive entrance.It is described First segment spray is equipped with hydrochloric acid entrance.The second segment spray is equipped with water inlet.The acid-base neutralization device is equipped with alkali Entrance.
In the present invention, the calciner is equipped with coal powder entrance and/or fuel gas inlet.
In the present invention, system further include: air is delivered to the air of cooling device by first gas conveyance conduit Entrance.Preferably, air by first gas conveyance conduit independently be delivered to High-temperature cooling section, medium temperature cooling section, The air intake of sub-cooled section.The gas vent of High-temperature cooling section is connected to preheating device by second gas conveyance conduit Gas access.The gas vent of medium temperature cooling section is connected to the gas access of down-draft drying zone by third gas conveyance conduit. The gas vent of sub-cooled section is connected to the gas access of blasting drying period by the 4th gas transmission pipeline.Preheating device Gas vent connects the 5th gas transmission pipeline.The gas vent of down-draft drying zone connects the 6th gas transmission pipeline.Air blast is dry Dry section of the 7th gas transmission pipeline of body outlet connection.5th gas transmission pipeline, the 6th gas transmission pipeline and the 7th gas Conveyance conduit is connected to the gas access of calciner by the 8th gas transmission pipeline after merging.The exhanst gas outlet of calciner The smoke inlet of the smoke inlet or high temperature section reclaimer that are sprayed by the 9th gas transmission pipeline and first segment is connect;
Preferably, the same side of calciner is arranged in the exhanst gas outlet of calciner and the feed inlet of calciner, The same side of calciner is arranged in the gas access of calciner and the discharge port of calciner.It is further preferred that roasting dress The exhanst gas outlet set is Chong Die with the gating location of calciner, the gas access of calciner and the discharge port position of calciner Set overlapping.
Preferably, the discharge port of acid-base neutralization device is connected to chloride entrance by third liquid transporting apparatus.The The hydrochloric acid entrance of one section of spray is connect with hydrochloric acid conveying device.The water inlet of the second segment spray is connect with water conveying device. The liquid outlet of filter-pressing device is entered by the hydrochloric acid that the 5th liquid transporting apparatus is connected to hydrochloric acid conveying device or first segment spray Mouthful.
In the present invention, first gas conveyance conduit is equipped with the first air blower.4th gas transmission pipeline is equipped with the Two air blowers.6th gas transmission pipeline is equipped with exhaust fan.
Preferably, the system further includes airflow pipe.Air is delivered to the 8th gas by airflow pipe The gas access of conveyance conduit or calciner.
Preferably, the vibration bucket is vibration funnel.The batcher is constant feeder.The digester position is multistage Digester, preferably two-stage digester or three-level digester.Pelletizer position disc balling machine.The drying device be with The trolley of grid section.Preheating device position drying grate.The calciner be shaft furnace, rotary hearth furnace, circular grate pelletizing machine, rotary kiln or One of belt type roasting machine.The flue gas processing device is anti-corrosion flue gas processing device.
The another embodiment provided according to the present invention provides a kind of incineration of refuse flyash and cooperates with Ferrous Metallurgy dust The technique of high temperature chlorination roasting realization resource utilization.
A kind of technique of municipal administration and metallurgy difficult solid waste collaboration resource utilization, the technique the following steps are included:
1) metallurgical dust in the incineration of refuse flyash and metallurgical dust storehouse in incineration of refuse flyash storehouse ingredient: is passed through the One mineral aggregate conveying device is delivered to mixing arrangement;
2) mix: incineration of refuse flyash and metallurgical dust are mixed in mixing arrangement, are uniformly mixed, and mixed powder is obtained Material;
3) profit mill: being delivered to damp mill by third mineral aggregate conveying device for mixed powder and carry out profit mill, after obtaining profit mill Mixed powder;
4) pelletizing: the mixed powder after profit mill is delivered to pelletizer by the 4th mineral aggregate conveying device and is granulated, is obtained Obtain powder pelletizing;
5) dry: powder pelletizing being delivered to drying device by the 5th mineral aggregate conveying device and is dried, drying is obtained Powder pelletizing afterwards;
6) it preheats: the powder pelletizing after drying being delivered to preheating device by the 6th mineral aggregate conveying device and is preheated, Improve the temperature and intensity of powder pelletizing, the powder pelletizing after being preheated;
7) it roasts: the powder pelletizing after preheating being delivered to calciner by the 7th mineral aggregate conveying device and carries out high-temperature chlorine Change roasting.
Preferably, the technique further include:
8) cooling: the powder pelletizing after high temperature chlorination roasting is delivered to cooling device by the 8th mineral aggregate conveying device It is cooled down.Preferably, powder pelletizing after cooling is delivered to blast furnace ironmaking workshop by the 9th mineral aggregate conveying device and carries out Ironmaking.
Preferably, the mixing arrangement includes digester and intensive mixer.Powder is passed through by the discharge port of batcher It crosses the first mineral aggregate conveying device and is delivered to digester and carry out digestion mixing, later, digest mixed powder and pass through the second mineral aggregate Conveying device is delivered to intensive mixer and carries out strength mixing, obtains mixed powder.
In step 1), by the metallurgical dust in the incineration of refuse flyash and metallurgical dust storehouse in incineration of refuse flyash storehouse point It is not transferred on batcher via (two) vibration buckets, mixing arrangement is then delivered to by the first mineral aggregate conveying device.
Preferably, the drying device includes blasting drying period and down-draft drying zone.Powder pelletizing is passed through into the 5th mine Material conveying device is delivered to blasting drying period and is dried, and later, is dried by down-draft drying zone, the powder after being dried Pellet group.
Preferably, cooling device includes High-temperature cooling section, medium temperature cooling section, sub-cooled section.It is roasted by high-temp chlorination Powder pelletizing after burning is delivered to cooling device by the 8th mineral aggregate conveying device, successively cooling by High-temperature cooling section, medium temperature Section, sub-cooled section are cooled down.
In the present invention, air is delivered to the air intake of cooling device by first gas conveyance conduit.Preferably, Air passes through the sky for being delivered to High-temperature cooling section, medium temperature cooling section, sub-cooled section of first gas conveyance conduit independently Gas entrance.
In the present invention, air is in cooling device and after the powder pelletizing heat exchange after high temperature chlorination roasting, High-temperature cooling The gas of section is delivered to preheating device for heated material by second gas conveyance conduit, and the gas of the High-temperature cooling section is pre- It exchanges heat in thermal with the powder pelletizing in preheating device, the gas after heat exchange is connected to the 5th gas transmission pipeline.In The gas of warm cooling section is dried material by the gas access that the conveying of third gas conveyance conduit is connected to down-draft drying zone, The gas of the medium temperature cooling section exchanges heat in down-draft drying zone with the powder pelletizing in down-draft drying zone, the gas after heat exchange It is connected to the 6th gas transmission pipeline.The gas of sub-cooled section is connected to blasting drying period by the conveying of the 4th gas transmission pipeline Gas access to material carry out preliminarily dried, the gas of the sub-cooled section is in blasting drying period and in blasting drying period Powder pelletizing exchanges heat, and the gas after heat exchange is connected to the 7th gas transmission pipeline.5th gas transmission pipeline, the 6th gas Calciner is delivered to by the 8th gas transmission pipeline after gas merging in conveyance conduit and the 7th gas transmission pipeline Gas access, the gas are roasted in calciner.
Preferably, the technique further include:
9) fume treatment: calciner discharge gas by the 9th gas transmission pipeline be delivered to flue gas processing device into Row fume treatment is delivered to chimney by the tenth gas transmission pipeline by flue gas processing device treated flue gas and is arranged It puts.
Preferably, the flue gas processing device includes first segment spray and second segment spray.The gas of calciner discharge Body is delivered to flue gas processing device by the 9th gas transmission pipeline, passes sequentially through first segment spray and second segment spray carries out cigarette Gas disposal.
Preferably, the flue gas processing device includes porous film dust-remover;It is further preferred that porous film dust-remover is soft Property film dust-remover or ceramic film dust-remover.
Preferably, the flue gas processing device includes high temperature section reclaimer, middle-temperature section reclaimer, low-temperature zone recycling Equipment;The gas of calciner (9) discharge is delivered to flue gas processing device by the 9th gas transmission pipeline, passes sequentially through high temperature Section reclaimer, middle-temperature section reclaimer, low-temperature zone reclaimer carry out fume treatment.
Preferably, successively pass through demisting on the tenth gas transmission pipeline by flue gas processing device treated flue gas Chimney is delivered to after device progress demisting and/or corrosive resistant fan and/or purification device progress gas cleaning to be discharged.
Preferably, successively pass through dedusting on the tenth gas transmission pipeline by flue gas processing device treated flue gas Chimney is delivered to after device (22) and/or the progress gas cleaning of corrosive resistant fan and/or purification device to be discharged.
In the present invention, in first segment spray, the flue gas for entering first segment spray is sprayed using hydrochloric acid, is passed through Cleaning solution is obtained after spray.Cleaning solution is delivered to filter device by the first liquid transporting apparatus and is filtered, and is filtered Filtrate and excessively filter solid.Filter liquor is delivered to filter-pressing device by the 4th liquid transporting apparatus and carries out filters pressing, obtains filters pressing filter Liquid and filter cake.
Preferably, filters pressing filtrate is delivered to the hydrochloric acid entrance of first segment spray by the 5th liquid transporting apparatus.
In the present invention, in second segment spray, the flue gas for entering second segment spray is sprayed using water.In flue gas Hydrogen chloride gas be all only absorbed by the water, acquired solution by second liquid conveying device be delivered to acid-base neutralization device carry out in With.
Preferably, the chloride obtained after neutralization is entered by the chloride that third liquid transporting apparatus is delivered to digester Mouthful.
In the present invention, the technique further include:
10) valuable metal recovery: filter solid and filter cake will be crossed by the tenth mineral aggregate conveying device and be delivered to valuable metal time Receiving apparatus carries out valuable metal recovery.
Preferably, the copper chloride that the recycling of high temperature section reclaimer obtains is delivered to from high temperature section reclaimer recycling outlet Copper recyclable device, the lead chloride that the recycling of middle-temperature section reclaimer obtains are delivered to lead recycling from middle-temperature section reclaimer recycling outlet Device, the zinc chloride that the recycling of low-temperature zone reclaimer obtains are delivered to zinc recovering device from low-temperature zone reclaimer recycling outlet. Preferably, the dust outlet of deduster is connected to the feed inlet of intensive mixer by dust conveyer.
In the present invention, the digester is equipped with chloride entrance.Powder passes through first by the discharge port of batcher Mineral aggregate conveying device be delivered to digester carry out digestion mixing when, from chloride entrance be added or spray chloride.Preferably, The chloride is calcium chloride solution.
In the present invention, the damp mill is equipped with additive entrance.Mixed powder is passed through into third mineral aggregate conveying device Be delivered to damp mill carry out profit mill when, from additive entrance be added additive.Preferably, the additive is bentonite.
In the present invention, the acid-base neutralization device is equipped with alkali entrance.Acquired solution passes through second liquid conveying device When being delivered to acid-base neutralization device and being neutralized, alkali is added from alkali entrance.Preferably, the alkali is calcium hydroxide solution.
Preferably, first gas conveyance conduit is equipped with the first air blower, the cooling device is cooling using air blast.The Four gas transmission pipelines are equipped with the second air blower, and the blasting drying period uses forced air drying.On 6th gas transmission pipeline Equipped with exhaust fan, the down-draft drying zone is dry using exhausting.
Preferably, the calciner is equipped with coal powder entrance and/or fuel gas inlet, the powder pelletizing after preheating is being roasted When burning device progress high temperature chlorination roasting, coal dust and/or combustion gas are sprayed into calciner.
Preferably, the same side of calciner is arranged in the exhanst gas outlet of calciner and the feed inlet of calciner, The same side of calciner, flue gas and stream contrary is arranged in the gas access of calciner and the discharge port of calciner.More Preferably, the exhanst gas outlet of calciner and the gating location of calciner are Chong Die, the gas access of calciner and roasting Burn the discharge port position overlapping of device.Preferably, control is weakly reducing atmosphere in calciner.Control is weak in calciner Reducing atmosphere is realized in the following way: coal dust is sprayed into calciner.Coal dust acts not only as fuel combustion, and And its carbon monoxide generated has reproducibility, which is weakly reducing atmosphere.It is different that coal dust is just added with beginning ingredient, The reason of coal dust is just added at this time is that preferably control reducing atmosphere, avoids the excess or deficiency of coal dust.
Preferably, the system further includes airflow pipe, air is delivered to the 8th gas by airflow pipe The gas access of conveyance conduit or calciner.
In the present invention, when mixed powder being carried out profit mill in step 3), additive is added, the weight of additive is mixing The 0.1-8% of powder weight, preferably 0.3-6%, more preferably 0.5-4%, further preferably 0.8-2%.
In the present invention, granulation obtains the diameter of powder pelletizing for 3-30mm, preferably 5-25mm, more preferably in step 4) For 6-20mm, further preferably 8-12mm.
In the present invention, in step 7), the temperature that powder pelletizing enters calciner is 300-1000 DEG C, preferably 400- 900 DEG C, more preferably 500-800 DEG C, further preferably 550-700 DEG C.Temperature in calciner is 1000-1600 DEG C, Preferably 1100-1500 DEG C, more preferably 1150-1400 DEG C, further preferably 1200-1300 DEG C.Calciner is to powder The time that pelletizing carries out high temperature chlorination roasting is 0.2-5h, preferably 0.5-4h, more preferably 0.8-3h, further preferably 1- 2h。
In the present invention, following system and technique are mainly used:
Feed proportioning system, feed proportioning system include garbage flying ash storehouse, Ferrous Metallurgy dust storehouse, and vibration leakage is equipped under each storehouse It struggles against (preventing orlop putty and feed), constant feeder is provided with below Vibrating funnel, for measuring the proportion of each material;
Hybrid system, including two sections of mixing, first segment are that preliminary profit is mixed, and proportioned material is transported to second level or three-level Digester (digester in the patent ZL 201620521055 and ZL201620518434 of present inventor), in digester, Spray chloride containing calcium solution (calcium chloride content increases with the proportion of flying dust and reduced);Second segment is that strength mixes, and profit has been mixed Material send into intensive mixer carry out strength mixing so that material is sufficiently mixed uniformly.
Damp mill will be sufficiently mixed uniform material and send into damp mill, carries out profit mill, it is (preferably swollen to add additive Profit soil, additional amount are 1%~2%), the balling-up and green-ball characteristic of mixture is transformed.
Mixture after profit mill is prepared into the bead (ball of diameter 8-12mm by disc balling machine in disc balling machine Group).
Drying system, including Two stage dryer, first segment are forced air drying, are arranged in bead material is smooth with grid section On trolley, carry out forced air drying to trolley bead material (air blast herein can be natural wind or hot wind);Second segment is dry for exhausting It is dry, it is passed through hot gas to trolley top, and carry out exhausting from pallet bottom, hot gas is further dried bead material by the bed of material.
The complete bead of Two stage dryer is sent into preheating device and carries out spray combustion gas progress in advance by preheating device (preferably drying grate) Heat improves the temperature and intensity of bead.
Calciner (preferably shaft furnace, also optional rotary kiln, rotary hearth furnace, circular grate pelletizing machine, belt type roasting machine etc.), will preheat Complete bead is sent to calciner, and sprays into coal dust, and the roasting carried out to bead is lighted in spray combustion gas, and the flue gas of generation is filled from roasting The arrival end of glove material is discharged, and flue gas and stream contrary, the bead material roasted are discharged from the outlet end of calciner material. Control is weakly reducing atmosphere in calciner, and feed end temperature is about 600 DEG C, and high temperature section temperature is 1200~1300 DEG C, pelletizing The residence time is about 1~2 hour in calciner, which is chloridising roasting, makes original by chlorinity higher in bead Zinc in material, lead, potassium, sodium etc. are with chlorine reaction bonded volatilizing and enriching into flue gas.
Cooling system carries out on cooling device cold after the outlet end discharge of the pellet roasting device material after chloridising roasting But, it is cooling to carry out air blast, with the direction of motion of the pelletizing on cooling device, is divided into high temperature section, middle-temperature section, low-temperature zone.By The cooling air of high temperature section, temperature highest, is passed through in preheating device, is used for combustion-supporting and heated material;By the cooling air of middle-temperature section, Temperature is higher, and material is dried in the second segment dry section being passed through in drying system;By the cooling air of low-temperature zone, temperature First segment dry section that is lower, being passed through in drying system carries out preliminarily dried to material.Obtain after cooling weight (alkali) metal and The very low ferrous material of chlorinity, the material can be sent directly into blast furnace for smelting iron.
Baking flue gas processing system, the flue gas that chloridising roasting generates contain a large amount of chlorination metal objects, have certain corrosion Property, flue gas is passed through in anti-corrosive apparatus, it is carried out first segment spray (spray liquid is dilute hydrochloric acid), gained cleaning solution filters to obtain cigarette Dirt and partially recycled valuable metal;Flue gas after first segment sprays carries out second segment spray (spray liquid is water), cigarette again Hydrogen chloride gas in gas is all only absorbed by the water, and acquired solution obtains chloride containing calcium solution after calcium hydroxide neutralisation treatment, It can be used in hybrid system;Flue gas after second segment sprays is after demister, after corrosive resistant fan is discharged into purifying column, then Through chimney outlet, flue gas emission is up to standard at this.Filters pressing is carried out again after first segment spray gained cleaning solution filtering, obtains filter cake and filter Liquid, filtrate can be used as the supplement of first segment spray, filter cake and cleaning solution filter flue dust together as valuable metal (lead zinc etc.) The recycling of high-content raw material progress valuable metal.
In the present invention, smoke processing system (or flue gas processing device) can use wet flue gas processing unit, Dry method flue gas processing unit can be used.Dry method flue gas processing unit, flue gas gradually cool down in the apparatus, due to containing in flue gas There are many chlorides of non-ferrous metal, and the set point of the chloride of various non-ferrous metals is not identical, as flue gas is in the device The chloride of middle cooling, the non-ferrous metal of set point high (temperature is high) can become at the high temperature section reclaimer of flue gas processing device For liquid, exports and be discharged from the recycling of high temperature section reclaimer;Set point take second place (temperature is taken second place) non-ferrous metal chloride It can become liquid at the middle-temperature section reclaimer of flue gas processing device, export and be discharged from the recycling of middle-temperature section reclaimer;It is solidifying The chloride of the non-ferrous metal of node low (temperature is low) can become liquid at the low-temperature zone reclaimer of flue gas processing device, from The recycling of low-temperature zone reclaimer exports discharge.In general, the chloride of main non-ferrous metal is copper chloride, chlorine in the flue gas Change lead, zinc chloride, according to the set point of these three chlorides, copper chloride can become liquid at high temperature section reclaimer, from height The recycling of temperature section reclaimer exports discharge, is then sent to copper recyclable device;Lead chloride can become at middle-temperature section reclaimer For liquid, exports and be discharged from the recycling of middle-temperature section reclaimer, be then sent to lead recyclable device;Zinc chloride can be returned in low-temperature zone Become liquid at receiving unit, exports and be discharged from the recycling of low-temperature zone reclaimer, be then sent to zinc recovering device.
In the present invention, " connection " of the feed inlet of the discharge port and another equipment of an equipment refers to is set by conveying The material branch mode that the both ends of standby (such as conveyer or pipeline) are realized.For example, unloaded from the discharge port of an equipment Material is transported to the feed inlet of (entrance) another equipment by conveying equipment.Conveying equipment described here includes but unlimited In: conveyer or pipeline.
It in the present invention, include spray equipment, filter device and filter-pressing device in flue gas processing device, spray equipment wraps again Include first segment spray and second segment spray.Filter liquor is obtained by filter device by the filtrate of first segment spray and filtering is solid Body, filter liquor obtain filters pressing filtrate and filter cake by filters pressing, and filters pressing filtrate can be delivered in first segment spray as spray Liquid is recycled.Valuable metal recovery device can be delivered to and further recycle valuable metal by crossing filter solid and filter cake, to flying dust It is more thorough simultaneously with dust processing, recycle the metal (such as lead, zinc, alkali metal) of organic matter, furthermore, it is possible to reduce solid Pollution of the metal to environment in the discharge and reduction solid waste of waste.The cleaning solution main component sprayed by second segment It is hydrochloric acid, which generates calcium chloride after acid-base neutralization device, and the calcium chloride of generation is delivered to digester as digestion Liquid is recycled.
In the present invention, if using dry method flue gas processing unit, the non-ferrous metals such as copper, lead, zinc can directly be recycled.Together When, the flue gas handled is discharged into deduster dedusting, dust is crossed from the dust outlet of deduster, and is delivered to intensive mixer work For feedstock circulation use;On the one hand the non-ferrous metal that can be enriched in dust increases the rate of recovery;On the other hand, discharge cigarette is reduced The content of non-ferrous metal in gas protects environment.
In the present invention, if using dry method flue gas processing unit, there is no particular/special requirement to device, as long as can be by flue gas Gradually cool down.For example, shell side can be walked using pipe shell type heat exchange equipment processing flue gas, flue gas, cooling medium (such as water, Air, nitrogen etc.) tube side is walked, entire pipe shell type heat exchange equipment is divided into three sections, respectively high temperature section reclaimer (namely high temperature Exhausting section), middle-temperature section reclaimer (namely medium temperature exhausting section), low-temperature zone reclaimer (namely low temperature exhausting section), Recycling outlet is respectively equipped on this three sections shell side, for recycling the chloride of each section of condensation;Such as high temperature exhausting section recycles chlorine Change copper, medium temperature exhausting section recycles lead chloride, and low temperature exhausting section recycles zinc chloride.According to concrete technology, entire pipe shell type heat exchange is set It is standby to be divided into one or more snippets, it is distinguished according to the ingredient of non-ferrous metal chloride in flue gas or type.
In the present invention, mixing arrangement can sufficiently be burnt rubbish using the combination of both digester and intensive mixer Flying dust is burnt to be uniformly mixed with Ferrous Metallurgy dust, meanwhile, it is handled using digester, enables to incineration of refuse flyash and steel smelting The digestion of bronze dirt thoroughly, accelerates incineration of refuse flyash and the subsequent reaction speed of Ferrous Metallurgy dust, but also waste incineration flies Ash reacts more thorough with Ferrous Metallurgy dust.
In the present invention, drying device includes blasting drying period and down-draft drying zone, using Two stage dryer, blasting drying period Preliminarily dried is carried out using forced air drying, down-draft drying zone is dry using the dry further progress of exhausting, and abundant garbage drying is burnt Burn the mixture of flying dust and Ferrous Metallurgy dust.
In the present invention, cooling device includes High-temperature cooling section, medium temperature cooling section, sub-cooled section.Cooling device plays While cooling powder pelletizing, the gas of High-temperature cooling section is delivered to preheating device for heating by second gas conveyance conduit Material, the gas of the medium temperature cooling section exchange heat in down-draft drying zone with the powder pelletizing in down-draft drying zone;The low temperature The gas of cooling section exchanges heat in blasting drying period with the powder pelletizing in blasting drying period;This design can make full use of Thermal energy, the gas after heat exchange are delivered to calciner, the temperature of combustion-supporting gas in calciner are improved, to improve calciner Working efficiency.
In the present invention, after the cooling temperature for reaching needs of the powder pelletizing after apparatus for supercooling, the part powder ball Group is delivered to blast furnace ironmaking workshop by the 9th mineral aggregate conveying device and is smelted iron.Raw material (incineration of refuse flyash and the metallurgical powder Dirt) in the impurity such as chlorine, valuable metal after calciner, the impurity such as most of chlorine, valuable metal are all come by flue gas band Enter smoke processing system or flue gas processing device, the main component in powder pelletizing after apparatus for supercooling is iron, impurity pole Few, practical is low impurity iron-bearing material, and being delivered to blast furnace ironmaking workshop can directly be smelted iron.
In the present invention, the direction run along flying dust and dust, refers to powder pelletizing chlorination high temperature in calciner After roasting, conveying device is delivered to the direction of cooling device.Along the direction that flying dust and dust are run, High-temperature cooling section, medium temperature Cooling section, sub-cooled section are set gradually;That is, entrance of the High-temperature cooling section close to entire cooling device powder pelletizing Place, sub-cooled section are located at High-temperature cooling section and low temperature close to the exit of entire cooling device powder pelletizing, medium temperature cooling section The centre of cooling section.
In the present invention, refer to flowing side of the flue gas in flue gas processing device along the direction of calciner discharge flue gas To.Along the direction of calciner discharge flue gas, first segment spray and second segment spray are set gradually, that is to say, that first segment Spray is positioned close to the position of entire flue gas processing device smoke inlet, and second segment spray is positioned close to entire fume treatment The position of device exhanst gas outlet;Calciner discharge flue gas first passes through first segment spray, sprays using second segment.
In the present invention, the same of calciner is arranged in the exhanst gas outlet of calciner and the feed inlet of calciner Side, the feed inlet of the exhanst gas outlet and calciner that refer to calciner are arranged on the same face of calciner;Roasting dress The same side of calciner is arranged in the discharge port of the gas access and calciner set, refer to the gas access of calciner with The discharge port of calciner is arranged on the same face of calciner;The convection current of flue gas and material may be implemented in this way, promote roasting Burn the roasting effect and working efficiency of device.In general, the feed inlet setting of the exhanst gas outlet and calciner of calciner exists The face that calciner is arranged in the discharge port of the face of calciner and the gas access of calciner and calciner is in opposite Position, for example, the exhanst gas outlet of calciner and the feed inlet of calciner be arranged in calciner left end (or most before End), the right end (or rearmost end) of calciner is arranged in the gas access of calciner and the discharge port of calciner.
In the present invention, the dosage of incineration of refuse flyash and Ferrous Metallurgy dust is determined according to actual process, according to rubbish The content of each component determines in flying ash and Ferrous Metallurgy dust, including dioxin, heavy metal, chlorine equal size determine.
In the present invention, the dosage and concentration of chloride (such as calcium chloride) are unrestricted, as long as digestive juice can be played Effect, can according to actual process determine.In general, the dosage and levels of chloride (such as calcium chloride) are with winged The proportion of ash increases and reduces.
In the present invention, the dosage and concentration of hydrogen chloride are unrestricted in first segment spray, as long as cigarette can be washed sufficiently Heavy metal (or valuable metal, such as lead, zinc, alkali metal) in gas can be determined according to actual process.In second segment spray The dosage of water is unrestricted, can basis as long as the hydrogen chloride after first segment sprays in flue gas can be washed sufficiently Actual process determines.
In the present invention, the dosage and concentration for the alkali (calcium hydroxide solution) being added in acid-base neutralization device are unrestricted, As long as the hydrogen chloride in second segment spray washing liquid can be neutralized, can be determined according to actual process.
In the present invention, purification device plays the role of handling flue gas, removes the pollutant component in flue gas, reaches discharge mark It is quasi-.In general, purification device includes desulfuring and denitrifying apparatus;Preferably, wherein desulfurizer is active carbon desulfurization device (example Such as, the applicant's unit granted patent -- activated carbon method flue gas purification device ZL201520901540.7).
It in the present invention, optionally, is to indicate to carry out perhaps to be provided with or without without selecting or not selecting.
In the present invention, the component and device not being described are component and device well known to those skilled in the art.
Compared with prior art, the present invention has following advantageous effects:
1, it solves the heavy metal metallurgies dust difficulty such as steel plant's zincy lead and sets bring environment and social concern;
2, make full use of the effective chlorine element of flying dust for chloridising roasting, realize flying dust resource utilization and innoxious place It sets;
3, this method eliminates the harmful elements such as zinc, lead, potassium, sodium in zinc-containing metallurgy dust, and products obtained therefrom can be used as refining Iron raw materials for production;
4, the non-ferrous metals such as zinc, lead can also be recycled, resource recovery is increased;
5, flue gas realization recycles, energy-saving and emission-reduction.
Detailed description of the invention
Fig. 1 is the structural schematic diagram that a kind of municipal administration of the present invention and the difficult solid waste of metallurgy cooperate with resource utilization system;
Fig. 2 is the pipeline connection signal that a kind of municipal administration of the present invention and the difficult solid waste of metallurgy cooperate with resource utilization system Figure;
Fig. 3 is another fume treatment that a kind of municipal administration of the present invention and the difficult solid waste of metallurgy cooperate with resource utilization system Apparatus structure schematic diagram;
Fig. 4 is the artwork using present system;
Fig. 5 is the process flow chart of present system;
Fig. 6 is the flow diagram of flue gas processing device in present system;
Fig. 7 is the flow diagram of another flue gas processing device in present system.
Appended drawing reference:
1: feed bin;101: incineration of refuse flyash storehouse;102: metallurgical dust storehouse;2: vibration bucket;3: batcher;4: mixing dress It sets;401: digester;40101: chloride entrance;402: intensive mixer;5: damp mill;501: additive entrance;6: pelletizing Machine;7: drying device;701: blasting drying period;702: down-draft drying zone;8: preheating device;9: calciner;901: coal dust enters Mouthful;902: fuel gas inlet;10: cooling device;1001: High-temperature cooling section;1002: medium temperature cooling section;1003: sub-cooled section; 11: flue gas processing device;1101: first segment spray;1102: second segment spray;1103: high temperature section reclaimer;1104: medium temperature Section reclaimer;1105: low-temperature zone reclaimer;12: the first air blowers;13: the second air blowers;14: demister;15: anti- Rotten blower;16: purification device;17: chimney;18: exhaust fan;19: filter device;20: acid-base neutralization device;2001: alkali entrance; 21: filter-pressing device;22: deduster;L1: first gas conveyance conduit;L2: second gas conveyance conduit;L3: third gas conveying Pipeline;L4: the four gas transmission pipeline;L5: the five gas transmission pipeline;L6: the six gas transmission pipeline;L7: the seven gas Conveyance conduit;L8: the eight gas transmission pipeline;L9: the nine gas transmission pipeline;L10: the ten gas transmission pipeline;L11: empty Letter shoot road;G1: the first mineral aggregate conveying device;G2: the second mineral aggregate conveying device;G3: third mineral aggregate conveying device;G4: the Four mineral aggregate conveying devices;G5: the five mineral aggregate conveying device;G6: the six mineral aggregate conveying device;G7: the seven mineral aggregate conveying device; G8: the eight mineral aggregate conveying device;G9: the nine glass of mineral aggregate conveying device;G10: the ten glass of mineral aggregate conveying device;G11: dust conveying Device;Y1: the first liquid transporting apparatus;Y2: second liquid conveying device;Y3: third liquid transporting apparatus;Y4: the four liquid Conveying device;Y5: the five liquid transporting apparatus;Y6: hydrochloric acid conveying device;Y7: water conveying device.
Specific embodiment
The first embodiment provided according to the present invention provides a kind of municipal administration and metallurgical difficult solid waste collaboration recycling The system utilized.
The system of a kind of municipal administration and metallurgical difficult solid waste collaboration resource utilization, the system include:
1) proportioner: proportioner includes feed bin 1;
2) mixing arrangement 4: the discharge port of feed bin 1 is connected by the feed inlet of the first mineral aggregate conveying device G1 and mixing arrangement 4 It connects;
3) damp mill 5: the discharge port of mixing arrangement 4 is connected by the feed inlet of third mineral aggregate conveying device G3 and damp mill 5 It connects;
4) pelletizer 6: the discharge port of damp mill 5 is connect by the 4th mineral aggregate conveying device G4 with the feed inlet of pelletizer 6;
5) drying device 7: the discharge port of pelletizer 6 passes through the feed inlet of the 5th mineral aggregate conveying device G5 and drying device 7 Connection;
6) preheating device 8: the discharge port of drying device 7 passes through the charging of the 6th mineral aggregate conveying device G6 and preheating device 8 Mouth connection;
7) calciner 9: the discharge port of preheating device 8 passes through the charging of the 7th mineral aggregate conveying device G7 and calciner 9 Mouth connection.
Preferably, the system further include:
8) cooling device 10.The discharge port of calciner 9 by the 8th mineral aggregate conveying device G8 and cooling device 10 into Material mouth connection.
Preferably, the discharge port of cooling device 10 is connected to blast furnace ironmaking workshop by the 9th mineral aggregate conveying device G9.
Preferably, the system further include: 9) flue gas processing device 11.The exhanst gas outlet of calciner 9 passes through the 9th gas Body conveyance conduit L9 is connect with the smoke inlet of flue gas processing device 11.
Preferably, proportioner includes feed bin 1, vibration bucket 2, batcher 3, feed bin 1 includes incineration of refuse flyash storehouse 101 With metallurgical dust storehouse 102, it is respective out that two vibration buckets 2 are separately positioned on incineration of refuse flyash storehouse 101 and metallurgical dust storehouse 102 The lower section of vibration 2 discharge ports of bucket is arranged in the lower section of material mouth, batcher 3;The discharge port of batcher 3 passes through the first mineral aggregate conveying dress G1 is set to connect with the feed inlet of mixing arrangement 4.
Preferably, the mixing arrangement 4 includes digester 401 and intensive mixer 402.The discharge port of batcher 3 is logical It crosses the first mineral aggregate conveying device G1 to connect with the feed inlet of digester 401, the discharge port of digester 401 is conveyed by the second mineral aggregate Device G2 is connect with the feed inlet of intensive mixer 402, and the discharge port of intensive mixer 402 passes through third mineral aggregate conveying device G3 It is connect with the feed inlet of damp mill 5.
Preferably, the drying device 7 includes blasting drying period 701 and down-draft drying zone 702.Along flying dust and dust The upstream of down-draft drying zone 702 is arranged in the direction of operation, blasting drying period 701.
Preferably, cooling device 10 includes High-temperature cooling section 1001, medium temperature cooling section 1002, sub-cooled section 1003. Along the direction that flying dust and dust are run, High-temperature cooling section 1001, medium temperature cooling section 1002, sub-cooled section 1003 are successively set It sets.
Preferably, the flue gas processing device 11 includes first segment spray 1101 and second segment spray 1102.Along roasting The direction that flue gas is discharged in device 9 is burnt, first segment spray 1101 and second segment spray 1102 are set gradually.Or, it is preferred that institute Stating flue gas processing device 11 includes porous film dust-remover;It is further preferred that porous film dust-remover is flexible film dust-remover or ceramics Film dust-remover.Such as flexible film dust-remover.Preferably, flexible membrane is intermetallic compound flexible membrane.Porous film dust-remover is A kind of corrosion-resistant, anti-oxidant, thermal shock resistance, wear-resistant, anticlogging film dust-remover.
Preferably, the flue gas processing device 11 include high temperature section reclaimer 1103, middle-temperature section reclaimer 1104, Low-temperature zone reclaimer 1105;The direction of flue gas, high temperature section reclaimer 1103, middle-temperature section recycling are discharged along calciner 9 Equipment 1104, low-temperature zone reclaimer 1105 are set gradually.
In the present invention, the exhanst gas outlet of second segment spray 1102 is connected to chimney by the tenth gas transmission pipeline L10 17。
Optionally, demister 14 and/or corrosive resistant fan 15 and/or net are successively arranged on the tenth gas transmission pipeline L10 Makeup sets 16.
In the present invention, the exhanst gas outlet of low-temperature zone reclaimer 1105 is connected to by the tenth gas transmission pipeline L10 Chimney 17;Optionally, deduster 22 and/or corrosive resistant fan 15 and/or purification dress are successively arranged on the tenth gas transmission pipeline L10 Set 16;Preferably, deduster 22 is porous film dust-remover.
Preferably, the system further include: the liquid outlet of first segment spray 1101 passes through the first liquid transporting apparatus Y1 It is connect with filter device 19.Filter device 19 includes liquid outlet and solid outlet, and the liquid outlet of filter device 19 passes through the Four liquid transporting apparatus Y4 are connect with filter-pressing device 21.
Preferably, the liquid outlet of second segment spray 1102 is connected to acid-base neutralization by second liquid conveying device Y2 Device 20.
Preferably, the solid outlet of the solid outlet of filter device 19 and filter-pressing device 21 is filled by the conveying of the tenth mineral aggregate It sets G10 and is delivered to valuable metal recovery device.
Preferably, the recycling outlet connection copper recyclable device of high temperature section reclaimer 1103, middle-temperature section reclaimer 1104 recycling outlet connection lead recyclable device, the recycling outlet connection zinc recovering device of low-temperature zone reclaimer 1105.It is preferred that , the dust outlet of deduster 22 is connected to the feed inlet of intensive mixer 402 by dust conveyer G11.
In the present invention, the digester 401 is equipped with chloride entrance 40101.The damp mill 5 is equipped with additive Entrance 501.The first segment spray 1101 is equipped with hydrochloric acid entrance.The second segment spray 1102 is equipped with water inlet.It is described Acid-base neutralization device 20 is equipped with alkali entrance 2001.
In the present invention, the calciner 9 is equipped with coal powder entrance 901 and/or fuel gas inlet 902.
In the present invention, system further include: air is delivered to cooling device 10 by first gas conveyance conduit L1 Air intake.Preferably, air by first gas conveyance conduit L1 independently be delivered to High-temperature cooling section 1001, in The air intake of warm cooling section 1002, sub-cooled section 1003.The gas vent of High-temperature cooling section 1001 is defeated by second gas The gas access for sending pipeline L2 to be connected to preheating device 8.The gas vent of medium temperature cooling section 1002 passes through third gas delivery pipe Road L3 is connected to the gas access of down-draft drying zone 702.The gas vent of sub-cooled section 1003 passes through the 4th air shooter Road L4 is connected to the gas access of blasting drying period 701.The gas vent of preheating device 8 connects the 5th gas transmission pipeline L5. The gas vent of down-draft drying zone 702 connects the 6th gas transmission pipeline L6.The 7th gas of body outlet connection of blasting drying period 701 Body conveyance conduit L7.After 5th gas transmission pipeline L5, the 6th gas transmission pipeline L6 and the 7th gas transmission pipeline L7 merge The gas access of calciner 9 is connected to by the 8th gas transmission pipeline L8.The exhanst gas outlet of calciner 9 passes through the 9th gas Body conveyance conduit L9 is connect with the smoke inlet of the smoke inlet of first segment spray 1101 or high temperature section reclaimer 1103;
Preferably, the same of calciner 9 is arranged in the feed inlet of the exhanst gas outlet of calciner 9 and calciner 9 The same side of calciner 9 is arranged in side, the gas access of calciner 9 and the discharge port of calciner 9.It is further preferred that The exhanst gas outlet of calciner 9 is Chong Die with the gating location of calciner 9, the gas access of calciner 9 and calciner 9 Discharge port position overlapping.
Preferably, the discharge port of acid-base neutralization device 20 is connected to chloride entrance by third liquid transporting apparatus Y3 40101.The hydrochloric acid entrance of first segment spray 1101 is connect with hydrochloric acid conveying device Y6.The water inlet of the second segment spray 1102 It is connect with water conveying device Y7.The liquid outlet of filter-pressing device 21 is connected to hydrochloric acid conveying dress by the 5th liquid transporting apparatus Y5 Set the hydrochloric acid entrance of Y6 or first segment spray 1101.
In the present invention, first gas conveyance conduit L1 is equipped with the first air blower 13.On 4th gas transmission pipeline L4 Equipped with the second air blower 12.6th gas transmission pipeline L6 is equipped with exhaust fan 18.
Preferably, the system further includes airflow pipe L11.Air is delivered to by airflow pipe L11 The gas access of eight gas transmission pipeline L8 or calciner 9.
Preferably, the vibration bucket 2 is vibration funnel.The batcher 3 is constant feeder.The digester 401 For multistage digester, preferably two-stage digester or three-level digester.The pelletizer 6 is disc balling machine.The dry dress 7 are set as the trolley with grid section.The preheating device 8 is drying grate.The calciner 9 is shaft furnace, rotary hearth furnace, ring type roasting One of machine, rotary kiln or belt type roasting machine.The flue gas processing device 11 is anti-corrosion flue gas processing device.
The another embodiment provided according to the present invention provides a kind of municipal administration and metallurgical difficult solid waste collaboration recycling The technique utilized.
A kind of technique of municipal administration and metallurgy difficult solid waste collaboration resource utilization, the technique the following steps are included:
1) ingredient: by the metallurgical dust in the incineration of refuse flyash and metallurgical dust storehouse 102 in incineration of refuse flyash storehouse 101 Mixing arrangement 4 is delivered to by the first mineral aggregate conveying device G1;
2) mix: incineration of refuse flyash and metallurgical dust are mixed in mixing arrangement 4, are uniformly mixed, and mixed powder is obtained Material;
3) profit mill: being delivered to damp mill 5 by third mineral aggregate conveying device G3 for mixed powder and carry out profit mill, obtains profit mill Mixed powder afterwards;
4) pelletizing: being delivered to pelletizer 6 by the 4th mineral aggregate conveying device G4 for the mixed powder after profit mill and be granulated, Obtain powder pelletizing;
5) dry: powder pelletizing being delivered to drying device 7 by the 5th mineral aggregate conveying device G5 and is dried, is done Powder pelletizing after dry;
6) preheat: by the powder pelletizing after drying by the 6th mineral aggregate conveying device G6 be delivered to preheating device 8 carry out it is pre- Heat improves the temperature and intensity of powder pelletizing, the powder pelletizing after being preheated;
7) it roasts: the powder pelletizing after preheating being delivered to calciner 9 by the 7th mineral aggregate conveying device G7 and carries out height Warm chloridising roasting.
Preferably, the technique further include:
8) cooling: the powder pelletizing after high temperature chlorination roasting is delivered to cooling dress by the 8th mineral aggregate conveying device G8 10 are set to be cooled down.Preferably, powder pelletizing after cooling is delivered to blast furnace ironmaking vehicle by the 9th mineral aggregate conveying device G9 Between smelted iron.
In step 1), by the metallurgy in the incineration of refuse flyash and metallurgical dust storehouse 102 in incineration of refuse flyash storehouse 101 Dust is transferred on batcher 3 via vibration bucket 2 respectively, is then delivered to mixing arrangement 4 by the first mineral aggregate conveying device G1.
Preferably, the mixing arrangement 4 includes digester 401 and intensive mixer 402.Powder passes through batcher 3 Discharge port is delivered to digester 401 by the first mineral aggregate conveying device G1 and carries out digestion mixing, later, digests mixed powder Intensive mixer 402 is delivered to by the second mineral aggregate conveying device G2 and carries out strength mixing, obtains mixed powder.
Preferably, the drying device 7 includes blasting drying period 701 and down-draft drying zone 702.Powder pelletizing is passed through 5th mineral aggregate conveying device G5 is delivered to blasting drying period 701 and is dried, and later, is dried by down-draft drying zone 702, Powder pelletizing after being dried.
Preferably, cooling device 10 includes High-temperature cooling section 1001, medium temperature cooling section 1002, sub-cooled section 1003. Powder pelletizing after high temperature chlorination roasting is delivered to cooling device 10 by the 8th mineral aggregate conveying device G8, successively through excessively high Warm cooling section 1001, medium temperature cooling section 1002, sub-cooled section 1003 are cooled down.
In the present invention, air is delivered to the air intake of cooling device 10 by first gas conveyance conduit L1.It is preferred that , air by first gas conveyance conduit L1 independently be delivered to High-temperature cooling section 1001, medium temperature cooling section 1002, The air intake of sub-cooled section 1003.
In the present invention, for air in cooling device 10 and after the powder pelletizing heat exchange after high temperature chlorination roasting, high temperature is cold But the gas of section 1001 is delivered to preheating device 8 for heated material, the High-temperature cooling section by second gas conveyance conduit L2 1001 gas exchanges heat in preheating device 8 with the powder pelletizing in preheating device 8, and the gas after heat exchange is connected to the 5th Gas transmission pipeline L5.The gas of medium temperature cooling section 1002 is connected to down-draft drying zone by third gas conveyance conduit L3 conveying Material is dried in 702 gas access, and the gas of the medium temperature cooling section 1002 is dry with exhausting in down-draft drying zone 702 Powder pelletizing in section 702 exchanges heat, and the gas after heat exchange is connected to the 6th gas transmission pipeline L6.Sub-cooled section 1003 Gas by the 4th gas transmission pipeline L4 conveying be connected to the gas access of blasting drying period 701 material is carried out it is tentatively dry Dry, the gas of the sub-cooled section 1003 is changed in blasting drying period 701 with the powder pelletizing in blasting drying period 701 Heat, the gas after heat exchange are connected to the 7th gas transmission pipeline L7.5th gas transmission pipeline L5, the 6th gas transmission pipeline Calciner 9 is delivered to by the 8th gas transmission pipeline L8 after gas merging in L6 and the 7th gas transmission pipeline L7 Gas access, the gas are roasted in calciner 9.
Preferably, the technique further include:
9) fume treatment: the gas that calciner 9 is discharged is delivered to fume treatment dress by the 9th gas transmission pipeline L9 11 carry out fume treatments are set, are delivered to by treated the flue gas of flue gas processing device 11 by the tenth gas transmission pipeline L10 Chimney 17 is discharged.
Preferably, the flue gas processing device 11 includes first segment spray 1101 and second segment spray 1102.Roasting dress The gas for setting 9 discharges is delivered to flue gas processing device 11 by the 9th gas transmission pipeline L9, passes sequentially through first segment spray 1101 and second segment spray 1102 carry out fume treatments.
Preferably, the flue gas processing device 11 includes porous film dust-remover;It is further preferred that porous film dust-remover is Flexible film dust-remover or ceramic film dust-remover.
Preferably, the flue gas processing device 11 include high temperature section reclaimer 1103, middle-temperature section reclaimer 1104, Low-temperature zone reclaimer 1105;The gas that calciner 9 is discharged is delivered to fume treatment dress by the 9th gas transmission pipeline L9 11 are set, high temperature section reclaimer 1103, middle-temperature section reclaimer 1104, low-temperature zone reclaimer 1105 is passed sequentially through and carries out flue gas Processing.
Preferably, by flue gas processing device 11, treated that flue gas successively passes through on the tenth gas transmission pipeline L10 It crosses after demister 14 carries out demisting and/or corrosive resistant fan 15 and/or the progress gas cleaning of purification device 16 and is delivered to chimney 17 It is discharged.
Preferably, by flue gas processing device 11, treated that flue gas successively passes through on the tenth gas transmission pipeline L10 It crosses deduster 22 and/or corrosive resistant fan 15 and/or purification device 16 and carries out being delivered to chimney 17 after gas cleaning and discharged.
In the present invention, in first segment spray 1101, the flue gas for entering first segment spray 1101 is carried out using hydrochloric acid Spray obtains cleaning solution after spray.Cleaning solution is delivered to filter device 19 by the first liquid transporting apparatus Y1 and carries out Filtering obtains filter liquor and crosses filter solid.Filter liquor by the 4th liquid transporting apparatus Y4 be delivered to filter-pressing device 21 into Row filters pressing obtains filters pressing filtrate and filter cake.
Preferably, filters pressing filtrate is entered by the hydrochloric acid that the 5th liquid transporting apparatus Y5 is delivered to first segment spray 1101 Mouthful.
In the present invention, in second segment spray 1102, the flue gas for entering second segment spray 1102 is sprayed using water Leaching.Hydrogen chloride gas in flue gas is all only absorbed by the water, and acquired solution is delivered in soda acid by second liquid conveying device Y2 It is neutralized with device 20.
Preferably, the chloride obtained after neutralization is delivered to the chlorine of digester 401 by third liquid transporting apparatus Y3 Compound entrance 40101.
In the present invention, the technique further include:
10) valuable metal recovery: filter solid and filter cake will be crossed by the tenth mineral aggregate conveying device G10 and be delivered to valuable metal Recyclable device carries out valuable metal recovery.
Alternatively,
The copper chloride that the recycling of high temperature section reclaimer 1103 obtains is delivered to from the recycling of high temperature section reclaimer 1103 outlet Copper recyclable device, the lead chloride that the recycling of middle-temperature section reclaimer 1104 obtains recycle outlet conveying from middle-temperature section reclaimer 1104 To lead recyclable device, the zinc chloride that the recycling of low-temperature zone reclaimer 1105 obtains is defeated from the recycling of low-temperature zone reclaimer 1105 outlet It send to zinc recovering device;Preferably, the dust outlet of deduster 22 is connected to intensive mixer by dust conveyer G11 402 feed inlet.
In the present invention, the digester 401 is equipped with chloride entrance 40101.Powder passes through the discharge port of batcher 3 By the first mineral aggregate conveying device G1 be delivered to digester 401 carry out digestion mixing when, from chloride entrance 40101 be added or spray Spill chloride.Preferably, the chloride is calcium chloride solution.
In the present invention, the damp mill 5 is equipped with additive entrance 501.Mixed powder is conveyed by third mineral aggregate Device G3 be delivered to damp mill 5 carry out profit mill when, from additive entrance 501 be added additive.Preferably, the additive is Bentonite.
In the present invention, the acid-base neutralization device 20 is equipped with alkali entrance 2001.Acquired solution is defeated by second liquid When sending device Y2 to be delivered to acid-base neutralization device 20 to be neutralized, alkali is added from alkali entrance 2001.Preferably, the alkali is hydrogen Calcium oxide solution.
Preferably, first gas conveyance conduit L1 is equipped with the first air blower 13, the cooling device 10 uses air blast It is cooling.4th gas transmission pipeline L4 is equipped with the second air blower 12, and the blasting drying period 701 uses forced air drying.6th Gas transmission pipeline L6 is equipped with exhaust fan 18, and the down-draft drying zone 702 is dry using exhausting.
Preferably, the calciner 9 is equipped with coal powder entrance 901 and/or fuel gas inlet 902, the powder after preheating Pelletizing sprays into coal dust and/or combustion gas into calciner 9 when calciner 9 carries out high temperature chlorination roasting.
Preferably, the same of calciner 9 is arranged in the feed inlet of the exhanst gas outlet of calciner 9 and calciner 9 The same side of calciner 9, flue gas and stream phase is arranged in side, the gas access of calciner 9 and the discharge port of calciner 9 It is inverse.It is further preferred that the exhanst gas outlet of calciner 9 is Chong Die with the gating location of calciner 9, the gas of calciner 9 Entrance is Chong Die with the discharge port position of calciner 9.Preferably, control is weakly reducing atmosphere in calciner 9.It is described it is weak also Primordial Qi atmosphere is realized in the following way: coal dust is sprayed into calciner.Coal dust acts not only as fuel combustion, and Its carbon monoxide generated has reproducibility, which is weakly reducing atmosphere.It is different from beginning ingredient and coal dust is just added, this When just be added coal dust the reason of be that preferably control reducing atmosphere, avoid the excess or deficiency of coal dust.
Preferably, the system further includes airflow pipe L11, air is delivered to by airflow pipe L11 The gas access of eight gas transmission pipeline L8 or calciner 9.
In the present invention, when mixed powder being carried out profit mill in step 3), additive is added, the weight of additive is mixing The 0.1-8% of powder weight, preferably 0.3-6%, more preferably 0.5-4%, further preferably 0.8-2%.
In the present invention, granulation obtains the diameter of powder pelletizing for 3-30mm, preferably 5-25mm, more preferably in step 4) For 6-20mm, further preferably 8-12mm.
In the present invention, in step 7), the temperature that powder pelletizing enters calciner 9 is 300-1000 DEG C, preferably 400-900 DEG C, more preferably 500-800 DEG C, further preferably 550-700 DEG C.Temperature in calciner 9 is 1000- 1600 DEG C, preferably 1100-1500 DEG C, more preferably 1150-1400 DEG C, further preferably 1200-1300 DEG C.Calciner 9 pairs of powder pelletizings carry out the time of high temperature chlorination roasting for 0.2-5h, preferably 0.5-4h, more preferably 0.8-3h, further Preferably 1-2h.
Embodiment 1
As depicted in figs. 1 and 2, the system of a kind of municipal administration and the difficult solid waste collaboration resource utilization of metallurgy, the system packet It includes:
1) proportioner: proportioner includes feed bin 1, vibration bucket 2, batcher 3, and feed bin 1 includes incineration of refuse flyash storehouse 101 and metallurgical dust storehouse 102, vibration bucket 2 is arranged under the discharge port in incineration of refuse flyash storehouse 101 and metallurgical dust storehouse 102 The lower section of vibration 2 discharge ports of bucket is arranged in side, batcher 3;
2) mixing arrangement 4: the discharge port of batcher 3 passes through the feed inlet of the first mineral aggregate conveying device G1 and mixing arrangement 4 Connection;
3) damp mill 5: the discharge port of mixing arrangement 4 is connected by the feed inlet of third mineral aggregate conveying device G3 and damp mill 5 It connects;
4) pelletizer 6: the discharge port of damp mill 5 is connect by the 4th mineral aggregate conveying device G4 with the feed inlet of pelletizer 6;
5) drying device 7: the discharge port of pelletizer 6 passes through the feed inlet of the 5th mineral aggregate conveying device G5 and drying device 7 Connection;
6) preheating device 8: the discharge port of drying device 7 passes through the charging of the 6th mineral aggregate conveying device G6 and preheating device 8 Mouth connection;
7) calciner 9: the discharge port of preheating device 8 passes through the charging of the 7th mineral aggregate conveying device G7 and calciner 9 Mouth connection.
The vibration bucket 2 is vibration funnel.The batcher 3 is constant feeder.The digester 401 multistage digestion Device, preferably two-stage digester.6 disc balling machines of the pelletizer.The drying device 7 is the trolley with grid section.Institute State 8 drying grates of preheating device.9 shaft furnaces of the calciner.
Embodiment 2
Embodiment 1 is repeated, only the system further include: 8) cooling device 10.The discharge port of calciner 9 passes through the 8th mine Material conveying device G8 is connect with the feed inlet of cooling device 10.The discharge port of cooling device 10 passes through the 9th mineral aggregate conveying device G9 It is connected to blast furnace ironmaking workshop.
Embodiment 3
Embodiment 2 is repeated, only the system further include: 9) flue gas processing device 11.The exhanst gas outlet of calciner 9 passes through 9th gas transmission pipeline L9 is connect with the smoke inlet of flue gas processing device 11.The flue gas processing device 11 is anti-corrosion flue gas Processing unit.
Embodiment 4
Embodiment 3 is repeated, only the mixing arrangement 4 includes digester 401 and intensive mixer 402.Batcher 3 goes out Material mouth is connect by the first mineral aggregate conveying device G1 with the feed inlet of digester 401, and the discharge port of digester 401 passes through the second mine Material conveying device G2 is connect with the feed inlet of intensive mixer 402, and the discharge port of intensive mixer 402 is conveyed by third mineral aggregate Device G3 is connect with the feed inlet of damp mill 5.The drying device 7 includes blasting drying period 701 and down-draft drying zone 702.Edge The direction of flying dust and dust operation, the upstream of down-draft drying zone 702 is arranged in blasting drying period 701.Cooling device 10 includes High-temperature cooling section 1001, medium temperature cooling section 1002, sub-cooled section 1003.Along the direction that flying dust and dust are run, high temperature is cold But section 1001, medium temperature cooling section 1002, sub-cooled section 1003 are set gradually.The flue gas processing device 11 is sprayed including first segment Leaching 1101 and second segment spray 1102.The direction of flue gas, first segment spray 1101 and second segment spray are discharged along calciner 9 1102 set gradually.The exhanst gas outlet of second segment spray 1102 is connected to chimney 17 by the tenth gas transmission pipeline L10.Tenth Demister 14 and corrosive resistant fan 15 and purification device 16 are successively arranged on gas transmission pipeline L10.It is set on the digester 401 There is chloride entrance 40101.The damp mill 5 is equipped with additive entrance 501.The first segment spray 1101 is equipped with hydrochloric acid Entrance.The second segment spray 1102 is equipped with water inlet.The acid-base neutralization device 20 is equipped with alkali entrance 2001.The roasting It burns device 9 and is equipped with coal powder entrance 901 and fuel gas inlet 902.
Embodiment 5
Embodiment 4 is repeated, only the flue gas processing device 11 is set including high temperature section reclaimer 1103, middle-temperature section recycling Standby 1104, low-temperature zone reclaimer 1105;The direction of flue gas, high temperature section reclaimer 1103, medium temperature are discharged along calciner 9 Section reclaimer 1104, low-temperature zone reclaimer 1105 are set gradually.The exhanst gas outlet of low-temperature zone reclaimer 1105 passes through the Ten gas transmission pipeline L10 are connected to chimney 17;Deduster 22, corrosive resistant fan are successively arranged on tenth gas transmission pipeline L10 15, purification device 16;Deduster 22 is porous film dust-remover;The recycling outlet connection copper recycling dress of high temperature section reclaimer 1103 It sets, the recycling outlet connection lead recyclable device of middle-temperature section reclaimer 1104, the recycling of low-temperature zone reclaimer 1105, which exports, to be connected Connect zinc recovering device;The dust outlet of deduster 22 is connected to the charging of intensive mixer 402 by dust conveyer G11 Mouthful.
Embodiment 6
Embodiment 4 is repeated, only the liquid outlet of first segment spray 1101 passes through the first liquid transporting apparatus Y1 and filtering Device 19 connects.Filter device 19 includes liquid outlet and solid outlet, and the liquid outlet of filter device 19 passes through the 4th liquid Conveying device Y4 is connect with filter-pressing device 21.The liquid outlet of second segment spray 1102 passes through second liquid conveying device Y2 connection To acid-base neutralization device 20.The solid outlet of filter device 19 and the solid outlet of filter-pressing device 21 are filled by the conveying of the tenth mineral aggregate It sets G10 and is delivered to valuable metal recovery device.Air is delivered to the air of cooling device 10 by first gas conveyance conduit L1 Entrance.Preferably, air by first gas conveyance conduit L1 independently to be delivered to High-temperature cooling section 1001, medium temperature cold But the air intake of section 1002, sub-cooled section 1003.The gas vent of High-temperature cooling section 1001 passes through second gas delivery pipe Road L2 is connected to the gas access of preheating device 8.The gas vent of medium temperature cooling section 1002 passes through third gas conveyance conduit L3 It is connected to the gas access of down-draft drying zone 702.The gas vent of sub-cooled section 1003 passes through the 4th gas transmission pipeline L4 It is connected to the gas access of blasting drying period 701.The gas vent of preheating device 8 connects the 5th gas transmission pipeline L5.Exhausting The gas vent of dryer section 702 connects the 6th gas transmission pipeline L6.The 7th gas of body outlet connection of blasting drying period 701 is defeated Send pipeline L7.5th gas transmission pipeline L5, the 6th gas transmission pipeline L6 and the 7th gas transmission pipeline L7 pass through after merging 8th gas transmission pipeline L8 is connected to the gas access of calciner 9.The exhanst gas outlet of calciner 9 is defeated by the 9th gas The smoke inlet for sending pipeline L9 to spray 1101 with first segment is connect;The exhanst gas outlet of calciner 9 and the feed inlet of calciner 9 Position overlapping, the gas access of calciner 9 are Chong Die with the discharge port position of calciner 9.The discharging of acid-base neutralization device 20 Mouth is connected to chloride entrance 40101 by third liquid transporting apparatus Y3.The hydrochloric acid entrance and hydrochloric acid of first segment spray 1101 Conveying device Y6 connection.The water inlet of the second segment spray 1102 is connect with water conveying device Y7.The liquid of filter-pressing device 21 Outlet is connected to hydrochloric acid conveying device Y6 by the 5th liquid transporting apparatus Y5.First gas conveyance conduit L1 is equipped with the first drum Blower 13.4th gas transmission pipeline L4 is equipped with the second air blower 12.6th gas transmission pipeline L6 is equipped with exhaust fan 18.
Embodiment 7
Embodiment 6 is repeated, only the system further includes airflow pipe L11.Air is defeated by airflow pipe L11 It send to the 8th gas transmission pipeline L8.
Use embodiment 1
As shown in Figure 3 and Figure 4, the technique of a kind of municipal administration and the difficult solid waste collaboration resource utilization of metallurgy, the technique packet Include following steps:
1) ingredient: by the metallurgical dust in the incineration of refuse flyash and metallurgical dust storehouse 102 in incineration of refuse flyash storehouse 101 After vibration bucket 2, batcher 3, mixing arrangement 4 is delivered to by the first mineral aggregate conveying device G1;
2) mix: incineration of refuse flyash and metallurgical dust are mixed in mixing arrangement 4, are uniformly mixed, and mixed powder is obtained Material;
3) profit mill: being delivered to damp mill 5 by third mineral aggregate conveying device G3 for mixed powder and carry out profit mill, obtains profit mill Mixed powder afterwards;
4) pelletizing: being delivered to pelletizer 6 by the 4th mineral aggregate conveying device G4 for the mixed powder after profit mill and be granulated, Obtain powder pelletizing;
5) dry: powder pelletizing being delivered to drying device 7 by the 5th mineral aggregate conveying device G5 and is dried, is done Powder pelletizing after dry;
6) preheat: by the powder pelletizing after drying by the 6th mineral aggregate conveying device G6 be delivered to preheating device 8 carry out it is pre- Heat improves the temperature and intensity of powder pelletizing, the powder pelletizing after being preheated;
7) it roasts: the powder pelletizing after preheating being delivered to calciner 9 by the 7th mineral aggregate conveying device G7 and carries out height Warm chloridising roasting.
Use embodiment 2
Embodiment 1 is reused, only the technique further include: 8) cooling: the powder pelletizing after high temperature chlorination roasting Cooling device 10 is delivered to by the 8th mineral aggregate conveying device G8 to be cooled down.Preferably, powder pelletizing after cooling passes through 9th mineral aggregate conveying device G9 is delivered to blast furnace ironmaking workshop and is smelted iron.
Use embodiment 3
Embodiment 2 is reused, only the mixing arrangement 4 includes digester 401 and intensive mixer 402.Powder is logical The discharge port for crossing batcher 3 is delivered to digester 401 by the first mineral aggregate conveying device G1 and carries out digestion mixing, later, digestion Mixed powder is delivered to intensive mixer 402 by the second mineral aggregate conveying device G2 and carries out strength mixing, obtains mixed powder Material.The drying device 7 includes blasting drying period 701 and down-draft drying zone 702.Powder pelletizing is passed through into the 5th mineral aggregate conveying dress It sets G5 and is delivered to blasting drying period 701 and be dried, later, be dried by down-draft drying zone 702, the powder after being dried Pellet group.Cooling device 10 includes High-temperature cooling section 1001, medium temperature cooling section 1002, sub-cooled section 1003.By high-temperature chlorine Powder pelletizing after changing roasting is delivered to cooling device 10 by the 8th mineral aggregate conveying device G8, successively passes through High-temperature cooling section 1001, medium temperature cooling section 1002, sub-cooled section 1003 are cooled down.Air is delivered to cold by first gas conveyance conduit L1 But the air intake of device 10.Preferably, air by first gas conveyance conduit L1 independently to be delivered to high temperature cold But the air intake of section 1001, medium temperature cooling section 1002, sub-cooled section 1003.Air in cooling device 10 with high-temp chlorination After powder pelletizing heat exchange after roasting, the gas of High-temperature cooling section 1001 is delivered to pre- hot charging by second gas conveyance conduit L2 8 are set for heated material, the gas of the High-temperature cooling section 1001 in preheating device 8 with the powder pelletizing in preheating device 8 into Row heat exchange, the gas after heat exchange are connected to the 5th gas transmission pipeline L5.The gas of medium temperature cooling section 1002 passes through third gas Material is dried in the gas access that conveyance conduit L3 conveying is connected to down-draft drying zone 702, the gas of the medium temperature cooling section 1002 Body exchanges heat in down-draft drying zone 702 with the powder pelletizing in down-draft drying zone 702, and the gas after heat exchange is connected to the 6th Gas transmission pipeline L6.The gas of sub-cooled section 1003 is connected to blasting drying period by the 4th gas transmission pipeline L4 conveying 701 gas access to material carry out preliminarily dried, the gas of the sub-cooled section 1003 in blasting drying period 701 with air blast Powder pelletizing in dryer section 701 exchanges heat, and the gas after heat exchange is connected to the 7th gas transmission pipeline L7.5th gas is defeated It is defeated by the 8th gas after sending the gas in pipeline L5, the 6th gas transmission pipeline L6 and the 7th gas transmission pipeline L7 to merge The gas access for sending pipeline L8 to be delivered to calciner 9, the gas are roasted in calciner 9.First gas delivery pipe Road L1 is equipped with the first air blower 13, and the cooling device 10 is cooling using air blast.4th gas transmission pipeline L4 is equipped with the Two air blowers 12, the blasting drying period 701 use forced air drying.6th gas transmission pipeline L6 is equipped with exhaust fan 18, institute It is dry using exhausting to state down-draft drying zone 702.The system further includes airflow pipe L11, and air passes through airflow pipe L11 is delivered to the 8th gas transmission pipeline L8.
Use embodiment 4
As shown in Figure 4 and Figure 5, embodiment 3 is reused, only the technique further include: 9) fume treatment: calciner 9 The gas of discharge is delivered to flue gas processing device 11 by the 9th gas transmission pipeline L9 and carries out fume treatment, by fume treatment Treated the flue gas of device 11 is delivered to chimney 17 by the tenth gas transmission pipeline L10 and is discharged.The fume treatment dress Setting 11 includes first segment spray 1101 and second segment spray 1102.The gas that calciner 9 is discharged passes through the 9th air shooter Road L9 is delivered to flue gas processing device 11, passes sequentially through first segment spray 1101 and second segment spray 1102 carries out fume treatment. It is successively removed by demister 14 on the tenth gas transmission pipeline L10 by treated the flue gas of flue gas processing device 11 Chimney 17 is delivered to after mist and the progress gas cleaning of corrosive resistant fan 15 and purification device 16 to be discharged.1101 are sprayed in first segment In, the flue gas for entering first segment spray 1101 is sprayed using hydrochloric acid, obtains cleaning solution after spray.Cleaning solution is logical It crosses the first liquid transporting apparatus Y1 and is delivered to filter device 19 and be filtered, obtain filter liquor and cross filter solid.Filter liquor Filter-pressing device 21 is delivered to by the 4th liquid transporting apparatus Y4 and carries out filters pressing, obtains filters pressing filtrate and filter cake.Filters pressing filtrate is logical Cross the hydrochloric acid entrance that the 5th liquid transporting apparatus Y5 is delivered to first segment spray 1101.In second segment spray 1102, using water The flue gas for entering second segment spray 1102 is sprayed.Hydrogen chloride gas in flue gas is all only absorbed by the water, and acquired solution is logical It crosses second liquid conveying device Y2 and is delivered to acid-base neutralization device 20 and neutralized.The chloride obtained after neutralization passes through third liquid Body conveying device Y3 is delivered to the chloride entrance 40101 of digester 401.
The digester 401 is equipped with chloride entrance 40101.Powder passes through the first mine by the discharge port of batcher 3 Material conveying device G1 be delivered to digester 401 carry out digestion mixing when, from chloride entrance 40101 be added or spray chloride, The chloride is calcium chloride solution.The damp mill 5 is equipped with additive entrance 501.Mixed powder is passed through into third mineral aggregate Conveying device G3 be delivered to damp mill 5 carry out profit mill when, from additive entrance 501 be added additive, the additive be swelling Soil, the weight of additive are the 1.5% of mixed powder weight,.The acid-base neutralization device 20 is equipped with alkali entrance 2001.Gained When solution is delivered to acid-base neutralization device 20 by second liquid conveying device Y2 and is neutralized, alkali is added from alkali entrance 2001, The alkali is calcium hydroxide solution.The calciner 9 is equipped with coal powder entrance 901 and fuel gas inlet 902, the powder after preheating Pelletizing sprays into coal dust and combustion gas into calciner 9 when calciner 9 carries out high temperature chlorination roasting.The flue gas of calciner 9 Export, the gas access of calciner 9 and the discharge port position weight of calciner 9 Chong Die with the gating location of calciner 9 It is folded.
Being granulated in step 4) and obtaining the diameter of powder pelletizing is 10mm.
In step 7), the temperature that powder pelletizing enters calciner 9 is 600 DEG C.Temperature in calciner 9 is 1200 ℃.The time that calciner 9 carries out high temperature chlorination roasting to powder pelletizing is 1.5h.
Use embodiment 5
Embodiment 4 is reused, only the technique further include: 10) valuable metal recovery: filter solid and filter cake are passed through Tenth mineral aggregate conveying device G10 is delivered to valuable metal recovery device and carries out valuable metal recovery.
Use embodiment 6
Embodiment 3 is reused, only the flue gas processing device 11 includes high temperature section reclaimer 1103, middle-temperature section time Receiving unit 1104, low-temperature zone reclaimer 1105;The gas that calciner 9 is discharged is delivered to by the 9th gas transmission pipeline L9 Flue gas processing device 11 passes sequentially through high temperature section reclaimer 1103, middle-temperature section reclaimer 1104, low-temperature zone reclaimer 1105 carry out fume treatment;By flue gas processing device 11, treated that flue gas successively passes through on the tenth gas transmission pipeline L10 Deduster 22, corrosive resistant fan 15, purification device 16 is crossed to be delivered to chimney 17 after carrying out gas cleaning and discharged.
The copper chloride that the recycling of high temperature section reclaimer 1103 obtains is delivered to from the recycling of high temperature section reclaimer 1103 outlet Copper recyclable device, the lead chloride that the recycling of middle-temperature section reclaimer 1104 obtains recycle outlet conveying from middle-temperature section reclaimer 1103 To lead recyclable device, the zinc chloride that the recycling of low-temperature zone reclaimer 1105 obtains is defeated from the recycling of low-temperature zone reclaimer 1103 outlet It send to zinc recovering device;The dust outlet of deduster 22 is connected to the charging of intensive mixer 402 by dust conveyer G11 Mouthful.
Use embodiment 7
Embodiment 4 is reused, only the additive is bentonite, and the weight of additive is mixed powder weight 5%.
Being granulated in step 4) and obtaining the diameter of powder pelletizing is 15mm.
In step 7), the temperature that powder pelletizing enters calciner 9 is 400 DEG C.Temperature in calciner 9 is 1500 ℃.The time that calciner 9 carries out high temperature chlorination roasting to powder pelletizing is 3h.
The method processing incineration of refuse flyash and metallurgical dust of embodiment 4-6 are used using the present invention:
Table 1:

Claims (12)

1. the technique of a kind of municipal administration and metallurgy difficult solid waste collaboration resource utilization, the technique the following steps are included:
1) ingredient: by the metallurgical dust in the incineration of refuse flyash and metallurgical dust storehouse (102) in incineration of refuse flyash storehouse (101) Mixing arrangement (4) are delivered to by the first mineral aggregate conveying device (G1);
2) mix: incineration of refuse flyash and metallurgical dust are mixed in mixing arrangement (4), are uniformly mixed, and mixed powder is obtained;
3) profit mill: being delivered to damp mill (5) by third mineral aggregate conveying device (G3) for mixed powder and carry out profit mill, obtains profit mill Mixed powder afterwards;
4) pelletizing: being delivered to pelletizer (6) by the 4th mineral aggregate conveying device (G4) for the mixed powder after profit mill and be granulated, Obtain powder pelletizing;
5) dry: powder pelletizing being delivered to drying device (7) by the 5th mineral aggregate conveying device (G5) and is dried, is done Powder pelletizing after dry;
6) it preheats: the powder pelletizing after drying being delivered to preheating device (8) by the 6th mineral aggregate conveying device (G6) and is carried out in advance Heat improves the temperature and intensity of powder pelletizing, the powder pelletizing after being preheated;
7) it roasts: the powder pelletizing after preheating being delivered to calciner (9) by the 7th mineral aggregate conveying device (G7) and carries out height Warm chloridising roasting.
2. technique according to claim 1, it is characterised in that: the technique further include:
8) cooling: the powder pelletizing after high temperature chlorination roasting is delivered to cooling device by the 8th mineral aggregate conveying device (G8) (10) it is cooled down;Preferably, powder pelletizing after cooling is delivered to blast furnace ironmaking by the 9th mineral aggregate conveying device (G9) Workshop is smelted iron;And/or
In step 1), by the metallurgy in the incineration of refuse flyash and metallurgical dust storehouse (102) in incineration of refuse flyash storehouse (101) Dust is transferred on batcher (3) via vibration bucket (2) respectively, is then delivered to mixing by the first mineral aggregate conveying device (G1) Device (4).
3. technique according to claim 2, it is characterised in that: the mixing arrangement (4) includes digester (401) and strength Mixing machine (402);Powder is delivered to digester by the first mineral aggregate conveying device (G1) by the discharge port of batcher (3) (401) digestion mixing is carried out, later, mixed powder is digested by the second mineral aggregate conveying device (G2) and is delivered to strength mixing Machine (402) carries out strength mixing, obtains mixed powder;
And/or
The drying device (7) includes blasting drying period (701) and down-draft drying zone (702);Powder pelletizing is passed through into the 5th mine Material conveying device (G5) is delivered to blasting drying period (701) and is dried, and later, is dried by down-draft drying zone (702), Powder pelletizing after being dried;
And/or
Cooling device (10) includes High-temperature cooling section (1001), medium temperature cooling section (1002), sub-cooled section (1003), through excessively high Powder pelletizing after warm chloridising roasting is delivered to cooling device (10) by the 8th mineral aggregate conveying device (G8), successively passes through high temperature Cooling section (1001), medium temperature cooling section (1002), sub-cooled section (1003) are cooled down.
4. technique according to claim 3, it is characterised in that: air is delivered to cold by first gas conveyance conduit (L1) But the air intake of device (10);Preferably, air is supreme by the conveying of first gas conveyance conduit (L1) independently Warm cooling section (1001), medium temperature cooling section (1002), sub-cooled section (1003) air intake;Air is in cooling device (10) In with after the powder pelletizing heat exchange after high temperature chlorination roasting, the gas of High-temperature cooling section (1001) passes through second gas conveyance conduit (L2) preheating device (8) are delivered to for heated material, the gas of the High-temperature cooling section (1001) is in preheating device (8) and in advance Powder pelletizing in thermal (8) exchanges heat, and the gas after heat exchange is connected to the 5th gas transmission pipeline (L5);Medium temperature is cooling The gas of section (1002) is connected to the gas access of down-draft drying zone (702) to material by third gas conveyance conduit (L3) conveying Be dried, the gas of the medium temperature cooling section (1002) in down-draft drying zone (702) with the powder in down-draft drying zone (702) Pelletizing exchanges heat, and the gas after heat exchange is connected to the 6th gas transmission pipeline (L6);The gas of sub-cooled section (1003) is logical It crosses the 4th gas transmission pipeline (L4) and conveys the gas access for being connected to blasting drying period (701) to material progress preliminarily dried, be somebody's turn to do The gas of sub-cooled section (1003) is changed in blasting drying period (701) with the powder pelletizing in blasting drying period (701) Heat, the gas after heat exchange are connected to the 7th gas transmission pipeline (L7);5th gas transmission pipeline (L5), the 6th air shooter Gas in road (L6) and the 7th gas transmission pipeline (L7) passes through the 8th gas transmission pipeline (L8) after merging and is delivered to roasting The gas access of device (9), the gas are roasted in calciner (9).
5. technique described in any one of -4 according to claim 1, it is characterised in that: the technique further include:
9) fume treatment: the gas of calciner (9) discharge is delivered to fume treatment dress by the 9th gas transmission pipeline (L9) It sets (11) and carries out fume treatment, pass through the tenth gas transmission pipeline (L10) by flue gas processing device (11) treated flue gas Chimney (17) is delivered to be discharged;
Preferably, the flue gas processing device (11) includes first segment spray (1101) and second segment spray (1102);Roasting The gas of device (9) discharge is delivered to flue gas processing device (11) by the 9th gas transmission pipeline (L9), passes sequentially through first Section spray (1101) and second segment spray (1102) carry out fume treatment;Or the flue gas processing device (11) includes that perforated membrane removes Dirt device;It is further preferred that porous film dust-remover is flexible film dust-remover or ceramic film dust-remover;Alternatively, the fume treatment dress Setting (11) includes high temperature section reclaimer (1103), middle-temperature section reclaimer (1104), low-temperature zone reclaimer (1105);Roasting The gas of device (9) discharge is delivered to flue gas processing device (11) by the 9th gas transmission pipeline (L9), passes sequentially through high temperature Section reclaimer (1103), middle-temperature section reclaimer (1104), low-temperature zone reclaimer (1105) carry out fume treatment;
Preferably, by flue gas processing device (11), treated that flue gas successively passes through on the tenth gas transmission pipeline (L10) It crosses after demister (14) carry out demisting and/or corrosive resistant fan (15) and/or purification device (16) progress gas cleaning and is delivered to Chimney (17) is discharged;Alternatively, by flue gas processing device (11) treated flue gas in the tenth gas transmission pipeline (L10) On be successively delivered to cigarette after deduster (22) and/or corrosive resistant fan (15) and/or purification device (16) carry out gas cleaning Chimney (17) is discharged.
6. technique according to claim 5, it is characterised in that: in first segment spray (1101), using hydrochloric acid to entrance The flue gas of first segment spray (1101) is sprayed, and obtains cleaning solution after spray;Cleaning solution is conveyed by the first liquid Device (Y1) is delivered to filter device (19) and is filtered, and obtains filter liquor and crosses filter solid, filter liquor passes through the 4th liquid Body conveying device (Y4) is delivered to filter-pressing device (21) and carries out filters pressing, obtains filters pressing filtrate and filter cake;Preferably, filters pressing filtrate The hydrochloric acid entrance of first segment spray (1101) is delivered to by the 5th liquid transporting apparatus (Y5);And/or
In second segment spray (1102), the flue gas for entering second segment spray (1102) is sprayed using water, in flue gas Hydrogen chloride gas is all only absorbed by the water, and acquired solution is delivered to acid-base neutralization device (20) by second liquid conveying device (Y2) It is neutralized;Preferably, the chloride obtained after neutralization is delivered to digester (401) by third liquid transporting apparatus (Y3) Chloride entrance (40101).
7. technique according to claim 6, it is characterised in that: the technique further include:
10) valuable metal recovery: filter solid and filter cake are delivered to valuable metal by the tenth mineral aggregate conveying device (G10) and returned Receiving apparatus carries out valuable metal recovery;
Alternatively,
The copper chloride that high temperature section reclaimer (1103) recycling obtains is delivered to from high temperature section reclaimer (1103) recycling outlet Copper recyclable device, the lead chloride that middle-temperature section reclaimer (1104) recycling obtains is recycled from middle-temperature section reclaimer (1104) to be exported It is delivered to lead recyclable device, the zinc chloride that low-temperature zone reclaimer (1105) recycling obtains is returned from low-temperature zone reclaimer (1105) It receives outlet and is delivered to zinc recovering device;Preferably, the dust outlet of deduster (22) is connected by dust conveyer (G11) To the feed inlet of intensive mixer (402).
8. technique described in any one of -7 according to claim 1, it is characterised in that: the digester (401) is equipped with chlorination Object entrance (40101), powder are delivered to digester by the first mineral aggregate conveying device (G1) by the discharge port of batcher (3) (401) when carrying out digestion mixing, chloride is added or sprayed from chloride entrance (40101);Preferably, the chloride is Calcium chloride solution;And/or
The damp mill (5) is equipped with additive entrance (501), and mixed powder is conveyed by third mineral aggregate conveying device (G3) When carrying out profit mill to damp mill (5), additive is added from additive entrance (501);Preferably, the additive is swelling Soil;And/or
The acid-base neutralization device (20) is equipped with alkali entrance (2001), and acquired solution is defeated by second liquid conveying device (Y2) It send to acid-base neutralization device (20) when being neutralized, alkali is added from alkali entrance (2001);Preferably, the alkali is calcium hydroxide Solution.
9. the technique according to any one of claim 3-8, it is characterised in that: first gas conveyance conduit (L1) is equipped with First air blower (13), the cooling device (10) are cooling using air blast;4th gas transmission pipeline (L4) is equipped with the second drum Blower (12), the blasting drying period (701) use forced air drying;6th gas transmission pipeline (L6) is equipped with exhaust fan (18), the down-draft drying zone (702) is dry using exhausting;And/or
The calciner (9) is equipped with coal powder entrance (901) and/or fuel gas inlet (902), and the powder pelletizing after preheating is roasting When burning device (9) progress high temperature chlorination roasting, coal dust and/or combustion gas are sprayed into calciner (9).
10. technique according to claim 9, it is characterised in that: the exhanst gas outlet of calciner (9) and calciner (9) Feed inlet setting in the same side of calciner (9), the gas access of calciner (9) and the discharge port of calciner (9) The same side in calciner (9), flue gas and stream contrary are set;It is further preferred that exhanst gas outlet and the roasting of calciner (9) The gating location overlapping of device (9) is burnt, the gas access of calciner (9) is Chong Die with the discharge port position of calciner (9), Preferably, control is weakly reducing atmosphere in calciner (9);And/or
The system further includes airflow pipe (L11), and air is delivered to the conveying of the 8th gas by airflow pipe (L11) The gas access of pipeline (L8) or calciner (9).
11. technique according to claim 1 to 10, it is characterised in that: moisten mixed powder in step 3) When mill, additive is added, the weight of additive is 0.1-8%, the preferably 0.3-6% of mixed powder weight, more preferably 0.5-4%, further preferably 0.8-2%;And/or
Granulation obtains the diameter of powder pelletizing for 3-30mm, preferably 5-25mm, more preferably 6-20mm, further in step 4) Preferably 8-12mm;And/or
In step 7), powder pelletizing enter calciner (9) temperature be 300-1000 DEG C, preferably 400-900 DEG C, more preferably It is 500-800 DEG C, further preferably 550-700 DEG C;Temperature in calciner (9) is 1000-1600 DEG C, preferably 1100-1500 DEG C, more preferably 1150-1400 DEG C, further preferably 1200-1300 DEG C;Calciner (9) is to powder pelletizing The time for carrying out high temperature chlorination roasting is 0.2-5h, preferably 0.5-4h, more preferably 0.8-3h, further preferably 1-2h.
12. method described in 0 or 11 according to claim 1, it is by such as that wherein control, which is weakly reducing atmosphere, in calciner (9) What under type was realized: coal dust is sprayed into calciner (9).
CN201710743661.7A 2017-08-25 2017-08-25 A kind of technique of municipal administration and metallurgical difficult solid waste collaboration resource utilization Pending CN109423558A (en)

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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109852812A (en) * 2019-04-10 2019-06-07 华北理工大学 A method of processing copper ashes device and processing copper ashes
CN112126788A (en) * 2020-05-14 2020-12-25 中冶长天国际工程有限责任公司 Method for extracting nonferrous metals by using incineration fly ash of hazardous organic wastes
CN112695202A (en) * 2020-12-07 2021-04-23 北京首创环境科技有限公司 Method for cooperatively recovering nonferrous metals from household garbage incineration fly ash and slag
CN112877537A (en) * 2021-01-13 2021-06-01 何良东 Method and system for high-temperature chlorination treatment of solid waste
CN113172072A (en) * 2021-04-16 2021-07-27 中冶长天国际工程有限责任公司 Solid waste disposal process centering on sintering and pelletizing processes
CN113319999A (en) * 2021-07-03 2021-08-31 航天神禾(北京)环保有限公司 System and method for manufacturing ceramic product by using fly ash and ceramic product manufactured by system and method
CN113337717A (en) * 2021-06-11 2021-09-03 南昌航空大学 Method for separating and recovering valuable metals in electroplating sludge by adopting combined chlorinating agent
CN114774684A (en) * 2022-04-21 2022-07-22 宝武集团环境资源科技有限公司 Method and system for cooperatively treating waste incineration fly ash by using rotary hearth furnace

Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3773890A (en) * 1972-04-14 1973-11-20 Union Carbide Corp Process for extracting values from spent hydrodesulfurization catalysts
JP2004211114A (en) * 2002-12-27 2004-07-29 Mitsubishi Materials Corp Method of producing rubidium
CN101069807A (en) * 2007-03-26 2007-11-14 中南大学 Method for purifying vanadium-contained stone coal sodium calcinating smoke
CN101643853A (en) * 2009-06-22 2010-02-10 云南锡业集团(控股)有限责任公司 Method for extracting indium and recovering valuable metals from flue dust of tin
CN202219132U (en) * 2011-10-09 2012-05-16 常州寅盛药业有限公司 Tertiary hydrogen chloride absorption system
CN103215441A (en) * 2013-04-19 2013-07-24 首钢总公司 Method for treating grate furnace garbage incineration flyash by using metallurgical sintering process
CN103526042A (en) * 2013-10-25 2014-01-22 北京矿冶研究总院 Method for extracting gold and silver from gold concentrate
CN104164572A (en) * 2014-08-25 2014-11-26 北京矿冶研究总院 Method for recovering valuable metals in tailings
CN106086434A (en) * 2016-07-27 2016-11-09 郴州钖涛化工有限公司 A kind of containing arsenic pyrite cinder chlorinated gold extracting technique and flue gas heat method of comprehensive utilization
CN106702144A (en) * 2015-07-20 2017-05-24 北京中科云腾科技有限公司 Method for comprehensively recycling metal from mineral substances containing multi-metal
CN106964637A (en) * 2017-05-12 2017-07-21 中南大学 A kind of garbage flying ash and metallurgical dust recycling cleaning treatment technique
CN106995887A (en) * 2017-05-09 2017-08-01 刘慧南 A kind of technique and its system of copper sulfide production metallic copper or copper compound

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3773890A (en) * 1972-04-14 1973-11-20 Union Carbide Corp Process for extracting values from spent hydrodesulfurization catalysts
JP2004211114A (en) * 2002-12-27 2004-07-29 Mitsubishi Materials Corp Method of producing rubidium
CN101069807A (en) * 2007-03-26 2007-11-14 中南大学 Method for purifying vanadium-contained stone coal sodium calcinating smoke
CN101643853A (en) * 2009-06-22 2010-02-10 云南锡业集团(控股)有限责任公司 Method for extracting indium and recovering valuable metals from flue dust of tin
CN202219132U (en) * 2011-10-09 2012-05-16 常州寅盛药业有限公司 Tertiary hydrogen chloride absorption system
CN103215441A (en) * 2013-04-19 2013-07-24 首钢总公司 Method for treating grate furnace garbage incineration flyash by using metallurgical sintering process
CN103526042A (en) * 2013-10-25 2014-01-22 北京矿冶研究总院 Method for extracting gold and silver from gold concentrate
CN104164572A (en) * 2014-08-25 2014-11-26 北京矿冶研究总院 Method for recovering valuable metals in tailings
CN106702144A (en) * 2015-07-20 2017-05-24 北京中科云腾科技有限公司 Method for comprehensively recycling metal from mineral substances containing multi-metal
CN106086434A (en) * 2016-07-27 2016-11-09 郴州钖涛化工有限公司 A kind of containing arsenic pyrite cinder chlorinated gold extracting technique and flue gas heat method of comprehensive utilization
CN106995887A (en) * 2017-05-09 2017-08-01 刘慧南 A kind of technique and its system of copper sulfide production metallic copper or copper compound
CN106964637A (en) * 2017-05-12 2017-07-21 中南大学 A kind of garbage flying ash and metallurgical dust recycling cleaning treatment technique

Non-Patent Citations (5)

* Cited by examiner, † Cited by third party
Title
云锡中心试验所技术情报室 著: "《氯化冶金》", 31 January 1973 *
张鸿波 主编: "《固体废弃物处理》", 31 July 2013, 长春:吉林大学出版社 *
茹至刚 编著: "《环境保护与治理》", 30 September 1988, 北京:冶金工业出版社 *
顾国维 等主编: "《绿色技术及其应用》", 31 May 1999, 上海:同济大学出版社 *
高艳宏 主编: "《钢铁冶金实习教程》", 31 October 2015, 北京:冶金工业出版社 *

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109852812A (en) * 2019-04-10 2019-06-07 华北理工大学 A method of processing copper ashes device and processing copper ashes
CN109852812B (en) * 2019-04-10 2024-01-26 华北理工大学 Device for treating copper slag and method for treating copper slag
CN112126788A (en) * 2020-05-14 2020-12-25 中冶长天国际工程有限责任公司 Method for extracting nonferrous metals by using incineration fly ash of hazardous organic wastes
CN112695202A (en) * 2020-12-07 2021-04-23 北京首创环境科技有限公司 Method for cooperatively recovering nonferrous metals from household garbage incineration fly ash and slag
CN112877537A (en) * 2021-01-13 2021-06-01 何良东 Method and system for high-temperature chlorination treatment of solid waste
CN113172072A (en) * 2021-04-16 2021-07-27 中冶长天国际工程有限责任公司 Solid waste disposal process centering on sintering and pelletizing processes
CN113337717A (en) * 2021-06-11 2021-09-03 南昌航空大学 Method for separating and recovering valuable metals in electroplating sludge by adopting combined chlorinating agent
CN113319999A (en) * 2021-07-03 2021-08-31 航天神禾(北京)环保有限公司 System and method for manufacturing ceramic product by using fly ash and ceramic product manufactured by system and method
CN114774684A (en) * 2022-04-21 2022-07-22 宝武集团环境资源科技有限公司 Method and system for cooperatively treating waste incineration fly ash by using rotary hearth furnace
CN114774684B (en) * 2022-04-21 2024-06-11 宝武集团环境资源科技有限公司 Method and system for cooperatively disposing waste incineration fly ash by utilizing rotary hearth furnace

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