CN109420662A - A kind of system of municipal administration and metallurgical difficult solid waste collaboration resource utilization - Google Patents
A kind of system of municipal administration and metallurgical difficult solid waste collaboration resource utilization Download PDFInfo
- Publication number
- CN109420662A CN109420662A CN201710744572.4A CN201710744572A CN109420662A CN 109420662 A CN109420662 A CN 109420662A CN 201710744572 A CN201710744572 A CN 201710744572A CN 109420662 A CN109420662 A CN 109420662A
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- Prior art keywords
- gas
- calciner
- conveying device
- section
- mineral aggregate
- Prior art date
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Links
- 239000002910 solid waste Substances 0.000 title claims abstract description 24
- 229910052500 inorganic mineral Inorganic materials 0.000 claims abstract description 120
- 239000011707 mineral Substances 0.000 claims abstract description 120
- 238000001035 drying Methods 0.000 claims abstract description 117
- 239000000428 dust Substances 0.000 claims abstract description 103
- 238000002156 mixing Methods 0.000 claims abstract description 52
- 239000010881 fly ash Substances 0.000 claims abstract description 34
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims abstract description 20
- 229910052725 zinc Inorganic materials 0.000 claims abstract description 20
- 239000011701 zinc Substances 0.000 claims abstract description 20
- 238000005272 metallurgy Methods 0.000 claims abstract description 17
- 239000007789 gas Substances 0.000 claims description 324
- 238000001816 cooling Methods 0.000 claims description 135
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 130
- 239000003546 flue gas Substances 0.000 claims description 128
- 239000007921 spray Substances 0.000 claims description 115
- 230000005540 biological transmission Effects 0.000 claims description 109
- 239000000843 powder Substances 0.000 claims description 90
- 238000005453 pelletization Methods 0.000 claims description 79
- 239000007788 liquid Substances 0.000 claims description 76
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 62
- 238000004064 recycling Methods 0.000 claims description 49
- 239000000463 material Substances 0.000 claims description 48
- 229910052751 metal Inorganic materials 0.000 claims description 40
- 239000002184 metal Substances 0.000 claims description 40
- 238000005422 blasting Methods 0.000 claims description 37
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 35
- 238000003825 pressing Methods 0.000 claims description 30
- 238000006386 neutralization reaction Methods 0.000 claims description 27
- 239000000654 additive Substances 0.000 claims description 25
- 230000000996 additive effect Effects 0.000 claims description 25
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 24
- 239000002585 base Substances 0.000 claims description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 23
- 239000007787 solid Substances 0.000 claims description 21
- 239000003513 alkali Substances 0.000 claims description 20
- 238000011282 treatment Methods 0.000 claims description 20
- 239000003517 fume Substances 0.000 claims description 18
- 238000000746 purification Methods 0.000 claims description 18
- 238000011084 recovery Methods 0.000 claims description 16
- 239000000779 smoke Substances 0.000 claims description 14
- 229910052742 iron Inorganic materials 0.000 claims description 12
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 10
- 229910052802 copper Inorganic materials 0.000 claims description 10
- 239000010949 copper Substances 0.000 claims description 10
- 239000002737 fuel gas Substances 0.000 claims description 8
- 239000003245 coal Substances 0.000 claims description 7
- 238000005260 corrosion Methods 0.000 claims description 7
- 239000000919 ceramic Substances 0.000 claims description 5
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- 241001062472 Stokellia anisodon Species 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 40
- 238000005660 chlorination reaction Methods 0.000 abstract description 20
- 229910001385 heavy metal Inorganic materials 0.000 abstract description 7
- 239000012320 chlorinating reagent Substances 0.000 abstract description 2
- 235000010755 mineral Nutrition 0.000 description 101
- 239000011812 mixed powder Substances 0.000 description 25
- 238000004140 cleaning Methods 0.000 description 16
- 239000002817 coal dust Substances 0.000 description 15
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 14
- 239000000460 chlorine Substances 0.000 description 14
- 229910052801 chlorine Inorganic materials 0.000 description 14
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 description 12
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 10
- 239000011324 bead Substances 0.000 description 10
- 230000029087 digestion Effects 0.000 description 10
- 238000009851 ferrous metallurgy Methods 0.000 description 10
- 239000012065 filter cake Substances 0.000 description 10
- 239000000706 filtrate Substances 0.000 description 10
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical group [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 8
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 7
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 7
- 239000004615 ingredient Substances 0.000 description 7
- 229910000831 Steel Inorganic materials 0.000 description 6
- 238000007605 air drying Methods 0.000 description 6
- 239000011133 lead Substances 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 239000010813 municipal solid waste Substances 0.000 description 6
- 239000010959 steel Substances 0.000 description 6
- 239000011592 zinc chloride Substances 0.000 description 6
- 235000005074 zinc chloride Nutrition 0.000 description 6
- 239000001110 calcium chloride Substances 0.000 description 5
- 229910001628 calcium chloride Inorganic materials 0.000 description 5
- 235000019504 cigarettes Nutrition 0.000 description 5
- 239000000567 combustion gas Substances 0.000 description 5
- ORTQZVOHEJQUHG-UHFFFAOYSA-L copper(II) chloride Chemical compound Cl[Cu]Cl ORTQZVOHEJQUHG-UHFFFAOYSA-L 0.000 description 5
- 238000001914 filtration Methods 0.000 description 5
- 239000012535 impurity Substances 0.000 description 5
- HWSZZLVAJGOAAY-UHFFFAOYSA-L lead(II) chloride Chemical compound Cl[Pb]Cl HWSZZLVAJGOAAY-UHFFFAOYSA-L 0.000 description 5
- 239000002956 ash Substances 0.000 description 4
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- -1 ferrous metals Chemical class 0.000 description 4
- 239000011521 glass Substances 0.000 description 4
- 229910001510 metal chloride Inorganic materials 0.000 description 4
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 3
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 3
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 3
- 229910052783 alkali metal Inorganic materials 0.000 description 3
- 150000001340 alkali metals Chemical class 0.000 description 3
- 239000000440 bentonite Substances 0.000 description 3
- 229910000278 bentonite Inorganic materials 0.000 description 3
- SVPXDRXYRYOSEX-UHFFFAOYSA-N bentoquatam Chemical group O.O=[Si]=O.O=[Al]O[Al]=O SVPXDRXYRYOSEX-UHFFFAOYSA-N 0.000 description 3
- 150000001805 chlorine compounds Chemical class 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000012528 membrane Substances 0.000 description 3
- 239000008188 pellet Substances 0.000 description 3
- 229910052700 potassium Inorganic materials 0.000 description 3
- 239000011591 potassium Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- 229910052708 sodium Inorganic materials 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 2
- 239000003963 antioxidant agent Substances 0.000 description 2
- 230000003078 antioxidant effect Effects 0.000 description 2
- 235000006708 antioxidants Nutrition 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000003500 flue dust Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000005469 granulation Methods 0.000 description 2
- 230000003179 granulation Effects 0.000 description 2
- 229910000765 intermetallic Inorganic materials 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 230000035939 shock Effects 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- 238000011105 stabilization Methods 0.000 description 2
- 238000004781 supercooling Methods 0.000 description 2
- 238000004056 waste incineration Methods 0.000 description 2
- 229910000906 Bronze Inorganic materials 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 239000010974 bronze Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 125000001309 chloro group Chemical group Cl* 0.000 description 1
- 239000002361 compost Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- KUNSUQLRTQLHQQ-UHFFFAOYSA-N copper tin Chemical compound [Cu].[Sn] KUNSUQLRTQLHQQ-UHFFFAOYSA-N 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000001079 digestive effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 235000011389 fruit/vegetable juice Nutrition 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- JQJCSZOEVBFDKO-UHFFFAOYSA-N lead zinc Chemical compound [Zn].[Pb] JQJCSZOEVBFDKO-UHFFFAOYSA-N 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000024121 nodulation Effects 0.000 description 1
- 238000009856 non-ferrous metallurgy Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000008961 swelling Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/60—Combinations of devices covered by groups B01D46/00 and B01D47/00
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/001—Dry processes
- C22B7/002—Dry processes by treating with halogens, sulfur or compounds thereof; by carburising, by treating with hydrogen (hydriding)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2247/00—Details relating to the separation of dispersed particles from gases, air or vapours by liquid as separating agent
- B01D2247/04—Regenerating the washing fluid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
-
- Y—GENERAL 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Abstract
The system of a kind of municipal administration and metallurgy difficult solid waste collaboration resource utilization, the system include: 1) proportioner: proportioner includes feed bin；2) mixing arrangement: feed bin is connect by the first mineral aggregate conveying device with mixing arrangement；3) damp mill: mixing arrangement is connect by third mineral aggregate conveying device with damp mill；4) pelletizer: damp mill is connect by the 4th mineral aggregate conveying device with pelletizer；5) drying device: pelletizer is connect by the 5th mineral aggregate conveying device with drying device；6) preheating device: drying device is connect by the 6th mineral aggregate conveying device with preheating device；7) calciner: preheating device is connect by the 7th mineral aggregate conveying device with calciner.The present invention using incineration of refuse flyash as chlorinating agent, using heavy metal metallurgies dust such as the leaded, zinc of high temperature chlorination roasting process.
Description
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 system for cooperateing with resource utilization, or make a kind of system 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 reclaimer is connected to chimney by the tenth gas transmission pipeline.Appoint
Selection of land is successively arranged deduster and/or corrosive resistant fan and/or purification device on the tenth gas transmission pipeline.Preferably, dedusting
Device 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 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) 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: mixed powder is delivered to damp mill by third mineral aggregate conveying device and carries out profit mill, after mixing profit is ground
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 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 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 recycles go back to the outlet of equipment receipts from high temperature section and is delivered to
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).
In the present invention, pelletizer is disk granulator or drum type brake pelletizer.
In the present invention, mineral aggregate conveying device (including the first mineral aggregate conveying device, the second mineral aggregate conveying device, third mine
Material conveying device, the 4th mineral aggregate conveying device, the 5th mineral aggregate conveying device, the 6th mineral aggregate conveying device, the 7th mineral aggregate conveying dress
Set, the 8th mineral aggregate conveying device, the 9th glass of mineral aggregate conveying device, the tenth glass of mineral aggregate conveying device, dust conveyer) it can be each
From being independently one of belt type conveyer, bucket conveyor, drum conveyor or plate chain type conveyer.
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: mixed powder is delivered to damp mill 5 by third mineral aggregate conveying device G3 and carries out profit mill, mixing 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: mixed powder is delivered to damp mill 5 by third mineral aggregate conveying device G3 and carries out profit mill, mixing 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 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；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 (10)
1. the system of a kind of municipal administration and the difficult solid waste collaboration resource utilization of metallurgy, the system include:
1) proportioner: proportioner includes feed bin (1)；
2) mixing arrangement (4): the discharge port of feed bin (1) passes through the charging of the first mineral aggregate conveying device (G1) and mixing arrangement (4)
Mouth connection；
3) damp mill (5): the discharge port of mixing arrangement (4) passes through the charging of third mineral aggregate conveying device (G3) and damp mill (5)
Mouth connection；
4) pelletizer (6): the discharge port of damp mill (5) passes through the feed inlet of the 4th mineral aggregate conveying device (G4) and pelletizer (6)
Connection；
5) drying device (7): the discharge port of pelletizer (6) by the 5th mineral aggregate conveying device (G5) and drying device (7) into
Material mouth connection；
6) preheating device (8): the discharge port of drying device (7) passes through the 6th mineral aggregate conveying device (G6) and preheating device (8)
Feed inlet connection；
7) calciner (9): the discharge port of preheating device (8) passes through the 7th mineral aggregate conveying device (G7) and calciner (9)
Feed inlet connection.
2. system according to claim 1, it is characterised in that: the system further include:
8) cooling device (10): the discharge port of calciner (9) passes through the 8th mineral aggregate conveying device (G8) and cooling device (10)
Feed inlet connection；Preferably, the discharge port of cooling device (10) is connected to blast furnace by the 9th mineral aggregate conveying device (G9)
Smelt iron workshop；And/or
The system further include: 9) flue gas processing device (11): the exhanst gas outlet of calciner (9) passes through the 9th gas transmission pipeline
(L9) it is connect with the smoke inlet of flue gas processing device (11)；And/or
Proportioner include feed bin (1), vibration bucket (2), batcher (3), feed bin (1) include incineration of refuse flyash storehouse (101) and
Metallurgical dust storehouse (102), two vibration buckets (2) are separately positioned on incineration of refuse flyash storehouse (101) and metallurgical dust storehouse (102) are each
From discharge port lower section, batcher (3) setting vibration bucket (2) discharge port lower section；The discharge port of batcher (3) passes through the
One mineral aggregate conveying device (G1) is connect with the feed inlet of mixing arrangement (4).
3. system according to claim 1 or 2, it is characterised in that: the mixing arrangement (4) include digester (401) and
Intensive mixer (402)；The discharge port of batcher (3) passes through the charging of the first mineral aggregate conveying device (G1) and digester (401)
The discharge port of mouth connection, digester (401) is connected by the feed inlet of the second mineral aggregate conveying device (G2) and intensive mixer (402)
It connects, the discharge port of intensive mixer (402) is connect by third mineral aggregate conveying device (G3) with the feed inlet of damp mill (5)；With/
Or
The drying device (7) includes blasting drying period (701) and down-draft drying zone (702), is run along flying dust and dust
Direction, blasting drying period (701) are arranged in the upstream of down-draft drying zone (702).
4. system according to claim 2 or 3, it is characterised in that: cooling device (10) include 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 set gradually；And/or
The flue gas processing device (11) includes first segment spray (1101) and second segment spray (1102)；Along calciner
(9) direction of flue gas is discharged, first segment spray (1101) and second segment spray (1102) are set gradually；Or the fume treatment dress
Setting (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；Or
The flue gas processing device (11) includes high temperature section reclaimer (1103), middle-temperature section reclaimer (1104), low-temperature zone
Reclaimer (1105)；Along the direction of calciner (9) discharge flue gas, high temperature section reclaimer (1103), middle-temperature section recycling
Equipment (1104), low-temperature zone reclaimer (1105) are set gradually.
5. system according to claim 4, it is characterised in that: the system further include: second segment sprays the flue gas of (1102)
Outlet is connected to chimney (17) by the tenth gas transmission pipeline (L10)；Optionally, on the tenth gas transmission pipeline (L10) according to
It is secondary to be equipped with demister (14) and/or corrosive resistant fan (15) and/or purification device (16)；Or,
The exhanst gas outlet of low-temperature zone recycling (1105) is connected to chimney (17) by the tenth gas transmission pipeline (L10)；Optionally,
Deduster (22) and/or corrosive resistant fan (15) and/or purification device (16) are successively arranged on tenth gas transmission pipeline (L10)；
Preferably, deduster (22) is porous film dust-remover；
And/or
The system further include: the liquid outlet that first segment sprays (1101) passes through the first liquid transporting apparatus (Y1) and filter device
(19) it connects；Filter device (19) includes liquid outlet and solid outlet, and the liquid outlet of filter device (19) passes through the 4th liquid
Body conveying device (Y4) is connect with filter-pressing device (21)；The liquid outlet that second segment sprays (1102) is conveyed by second liquid to be filled
It sets (Y2) and is connected to acid-base neutralization device (20)；Preferably, the solid outlet of filter device (19) and filter-pressing device (21)
Solid outlet is delivered to valuable metal recovery device by the tenth mineral aggregate conveying device (G10)；Or
The recycling outlet connection copper recyclable device of high temperature section reclaimer (1103), the recycling of middle-temperature section reclaimer (1104) go out
Mouth connection lead recyclable device, the recycling outlet connection zinc recovering device of low-temperature zone reclaimer (1105)；Preferably, deduster
(22) dust outlet is connected to the feed inlet of intensive mixer (402) by dust conveyer (G11).
6. system according to claim 5, it is characterised in that: the digester (401) is equipped with chloride entrance
(40101)；The damp mill (5) is equipped with additive entrance (501)；The first segment spray (1101) enters equipped with hydrochloric acid
Mouthful；The second segment spray (1102) is equipped with water inlet；The acid-base neutralization device (20) is equipped with alkali entrance (2001)；
And/or
The calciner (9) is equipped with coal powder entrance (901) and/or fuel gas inlet (902).
7. system according to claim 6, it is characterised in that: the system further include: air passes through first gas delivery pipe
Road (L1) is delivered to the air intake of cooling device (10), it is preferred that air passes through first gas conveyance conduit (L1) difference
The independent air intake for being delivered to High-temperature cooling section (1001), medium temperature cooling section (1002), sub-cooled section (1003)；High temperature
The gas vent of cooling section (1001) is connected to the gas access of preheating device (8) by second gas conveyance conduit (L2)；In
The gas vent of warm cooling section (1002) is entered by the gas that third gas conveyance conduit (L3) is connected to down-draft drying zone (702)
Mouthful；The gas vent of sub-cooled section (1003) is connected to blasting drying period (701) by the 4th gas transmission pipeline (L4)
Gas access；The gas vent of preheating device (8) connects the 5th gas transmission pipeline (L5)；The gas of down-draft drying zone (702)
The 6th gas transmission pipeline (L6) of outlet connection；The 7th gas transmission pipeline (L7) of body outlet connection of blasting drying period (701)；
5th gas transmission pipeline (L5), the 6th gas transmission pipeline (L6) and the 7th gas transmission pipeline (L7) merge after by the
Eight gas transmission pipelines (L8) are connected to the gas access of calciner (9)；The exhanst gas outlet of calciner (9) passes through the 9th gas
The smoke inlet of the smoke inlet or high temperature section reclaimer (1103) of body conveyance conduit (L9) and first segment spray (1101) connects
It connects；
Preferably, the exhanst gas outlet of calciner (9) and the feed inlet of calciner (9) are arranged in the same of calciner (9)
Side, the gas access of calciner (9) and the discharge port of calciner (9) are arranged in the same side of calciner (9)；It is more excellent
Choosing, the exhanst gas outlet of calciner (9) is Chong Die with the gating location of calciner (9), and the gas of calciner (9) enters
Mouth is Chong Die with the discharge port position of calciner (9).
8. system according to claim 7, it is characterised in that: the discharge port of acid-base neutralization device (20) passes through third liquid
Conveying device (Y3) is connected to chloride entrance (40101)；First segment sprays the hydrochloric acid entrance and hydrochloric acid conveying device of (1101)
(Y6) it connects；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 entered by the hydrochloric acid that the 5th liquid transporting apparatus (Y5) is connected to hydrochloric acid conveying device (Y6) or first segment spray (1101)
Mouthful.
9. system according to claim 7 or 8, it is characterised in that: 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)；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).
10. system according to claim 1 to 9, it is characterised in that: the vibration bucket (2) is vibration funnel；
The batcher (3) is constant feeder；Digester (401) position multistage digester, preferably two-stage digester or three-level
Digester；The drying device (7) is the trolley with grid section；Preheating device (8) position drying grate；The calciner
It (9) is one of shaft furnace, rotary hearth furnace, circular grate pelletizing machine, rotary kiln or belt type roasting machine；The flue gas processing device (11) is
Anti-corrosion flue gas processing device.
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