CN207904338U - The device of dearsenification and/or antimony from flue dust - Google Patents
The device of dearsenification and/or antimony from flue dust Download PDFInfo
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- CN207904338U CN207904338U CN201721200235.0U CN201721200235U CN207904338U CN 207904338 U CN207904338 U CN 207904338U CN 201721200235 U CN201721200235 U CN 201721200235U CN 207904338 U CN207904338 U CN 207904338U
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- flue dust
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- heating response
- response device
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- 239000003500 flue dust Substances 0.000 title claims abstract description 35
- WATWJIUSRGPENY-UHFFFAOYSA-N antimony atom Chemical compound [Sb] WATWJIUSRGPENY-UHFFFAOYSA-N 0.000 title abstract description 16
- 229910052787 antimony Inorganic materials 0.000 title abstract description 15
- 238000010438 heat treatment Methods 0.000 claims abstract description 36
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 24
- 238000000034 method Methods 0.000 claims abstract description 23
- 230000004044 response Effects 0.000 claims abstract description 17
- 238000002844 melting Methods 0.000 claims abstract description 8
- 230000008018 melting Effects 0.000 claims abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 5
- 230000008569 process Effects 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 10
- 239000011230 binding agent Substances 0.000 claims description 8
- 239000012530 fluid Substances 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 6
- 230000003134 recirculating effect Effects 0.000 claims description 5
- 238000004064 recycling Methods 0.000 claims description 4
- 238000000889 atomisation Methods 0.000 claims description 3
- 150000001722 carbon compounds Chemical class 0.000 claims description 3
- 238000005188 flotation Methods 0.000 claims description 2
- 230000008676 import Effects 0.000 claims description 2
- 239000011343 solid material Substances 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 31
- 239000002245 particle Substances 0.000 description 18
- 239000012071 phase Substances 0.000 description 16
- 229910052785 arsenic Inorganic materials 0.000 description 15
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 15
- 239000000047 product Substances 0.000 description 13
- 239000007787 solid Substances 0.000 description 13
- 239000010949 copper Substances 0.000 description 12
- 239000002893 slag Substances 0.000 description 12
- 229910052802 copper Inorganic materials 0.000 description 11
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 10
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 9
- 238000002485 combustion reaction Methods 0.000 description 8
- 239000012535 impurity Substances 0.000 description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical group [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 6
- 239000005864 Sulphur Substances 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- 239000000428 dust Substances 0.000 description 6
- 239000004576 sand Substances 0.000 description 6
- 238000005469 granulation Methods 0.000 description 5
- 230000003179 granulation Effects 0.000 description 5
- 229910052751 metal Inorganic materials 0.000 description 5
- 239000002184 metal Substances 0.000 description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 5
- 239000002912 waste gas Substances 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 238000001354 calcination Methods 0.000 description 3
- 238000004581 coalescence Methods 0.000 description 3
- 239000002826 coolant Substances 0.000 description 3
- 238000005243 fluidization Methods 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000003723 Smelting Methods 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- HAYXDMNJJFVXCI-UHFFFAOYSA-N arsenic(5+) Chemical compound [As+5] HAYXDMNJJFVXCI-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000007499 fusion processing Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- -1 sulphur compound Chemical class 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- LULLIKNODDLMDQ-UHFFFAOYSA-N arsenic(3+) Chemical compound [As+3] LULLIKNODDLMDQ-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000440 bentonite Substances 0.000 description 1
- 229910000278 bentonite Inorganic materials 0.000 description 1
- SVPXDRXYRYOSEX-UHFFFAOYSA-N bentoquatam Chemical compound O.O=[Si]=O.O=[Al]O[Al]=O SVPXDRXYRYOSEX-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052797 bismuth Inorganic materials 0.000 description 1
- JCXGWMGPZLAOME-UHFFFAOYSA-N bismuth atom Chemical compound [Bi] JCXGWMGPZLAOME-UHFFFAOYSA-N 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012717 electrostatic precipitator Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 230000003694 hair properties Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000009853 pyrometallurgy Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011268 retreatment Methods 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- JBQYATWDVHIOAR-UHFFFAOYSA-N tellanylidenegermanium Chemical compound [Te]=[Ge] JBQYATWDVHIOAR-UHFFFAOYSA-N 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
Landscapes
- Manufacture And Refinement Of Metals (AREA)
Abstract
The utility model is related to the dearsenification from flue dust and/or the devices of antimony.Provide a kind of device of flue dust of the processing from pyrometallurgical method; include by melting reactor that float product heats, the equipment of adding carbonaceous reducing agent, by heating response device that the flue dust heats together with the carbonaceous reducing agent and the separator for detaching volatile component; it is characterized in that the device further includes micronizer; the micronizer is used to the flue dust being granulated before introducing the reactor, which contains the first charging gear that water is added in float product.
Description
Technical field
The utility model is related to the dearsenification from flue dust and/or the devices of antimony.
Background technology
Copper (Cu), nickel (Ni), zinc (Zn) or similar non-ferrous metal are obtained from sulfide ore.These metals itself
It is valuable product, can be further processed in various ways, but to be further processed, is necessary for being that very pure form is deposited
.Such purity is generated by pyrometallurgical method.Pyrometallurgy can be regarded as or oxygen is added by oxidizing process
Heating to ore or has been obtained metal and does further heat treatment by oxygen-free atmosphere heating in reduction method, that is, stove.
Now as an example with Copper Ores melting, typical pyrometallurgical method is briefly described：Generally use sulphide flotation
The concentrate of Product Form makees initial substance.These float products generally comprise that about one third is copper, in addition one third is
Iron and remaining one third are sulphur.Also include a variety of other elements of low concentration, especially arsenic (As), antimony (Sb), bismuth (Bi), cadmium
(Cd) and lead (Pb).When implementing pyrometallurgical method, three phases, i.e. matte phase, slag phase and exhaust gas phase can be obtained.Exhaust gas phase is not
Only there is flue dust containing gaseous compound.Impurity in the distribution of each phase is obtained by the balanced reaction carried out.
In the first processing step by selective oxidation reaction makes a part of iron be separated from copper concentrate obtain it is molten
Slag phase.At a temperature of being significantly higher than 1000 DEG C, then the iron of oxidation is set to become liquid slag by the way that sand is added.
The accumulation of valuable product copper is in matte phase and number is also above its number in the slag phase isolated.
Due to high temperature, impurity especially arsenic and antimony are to be discharged in gaseous form.Exhaust gas containing heavy metal then must be at least
Partly discharged from these impurity in waste heat boiler and the cleaning of electric power exhaust gas.In processing procedure, by condensing again
And form particle.Together with entrained particles included in exhaust gas, they form so-called flue dust.
In addition to already mentioned impurity, copper (20-30% w/w) of these flue dusts also containing higher amount.At raising
Efficiency is managed, thus flue dust itself have to be also provided to fusion process to isolate valuable product copper.Simultaneously, it is necessary to
Carry out enrichment of such fusion process to avoid impurity.
Such flue dust Retreatment method is described in 10 2,010 011 242 A1 of DE, according to the patent, these
Temperature of the dust containing arsenic and/or antimony between 500-1000 DEG C is handled under an inert atmosphere and by the way that sulphur is added, thus
Solid phase is detached with gas phase.Then the gas phase is further cleaned.
The method is related to untreated flue dust and is recycled to smelting furnace.However, arsenic and/or the higher (2- of antimony content
It is particularly difficult to implement when 10%w/w).Since chemical reaction is a balanced reaction, contained arsenic and the entrance of antimony part are molten
Slag.But the arsenic of high-content and/or antimony can make this slag be no longer able to easily dispose or even cannot in slag
It is used for road construction as valuable product, but harmful waste must be used as to dispose.If contained in recirculating gas duct dust
The arsenic of 2-10%w/w, impurity collect the slag phase in smelting furnace, will produce described tired in terms of slag disposition or slag utilization
It is difficult.
Therefore, the purpose of this utility model is to provide a kind of device of processing flue dust so that contained valuable production
Object such as copper is recycled from flue dust and toxic impurity especially arsenic and antimony is removed, and the slag obtained in a furnace is suitble to use
In road construction.
Utility model content
The utility model provides a kind of device of flue dust of the processing from pyrometallurgical method, which includes that will float
Select melting reactor that product heats, the equipment of adding carbonaceous reducing agent, by the flue dust and the carbonaceous reducing agent one
The separator for playing the heating response device of heating and detaching volatile component, it is characterised in that the device further includes that micronized is set
Standby, which is used to the flue dust being granulated before introducing the reactor, which contains
The first charging gear of water is added in float product.
The device of flue dust of the processing from pyrometallurgical method described in the utility model is arranged to processing and contains 2-
10wt% arsenic and the/flue dust of antimony, the melting reactor are configured to will to contain at least 20wt% copper and at least
The float product of 20wt% sulphur is heated to temperature and is higher than 1000 DEG C, and first charging gear is arranged in float product
The water of its total weight 3-25wt% is added.
In the device of the utility model, reducing agent is added in flue dust and by the mixing of flue dust and reducing agent
Object heats jointly, thus isolates volatile components.It is conclusive that carbon compound, which is added as reducing agent,.The device includes
It will be heated to the melting reaction that temperature is higher than 1000 DEG C containing at least float product of 20wt% copper and at least 20wt% sulphur
Device, the equipment for adding carbonaceous reducing agent by heating response device that the flue dust heats together with the reducing agent and will wave
The separator of hair property component separation.The device is characterized in that the flue dust is granulated before introducing the reactor
Equipment, the equipment contain the first charging gear that its total weight 3-25wt% water is added in float product.The advantages of this device
It is the arsenic and antimony that high level can be also removed under conditions of no significant increase slag load.Meanwhile including it is valuable
The rate of recovery of metal is very high, thus can dramatically increase the efficiency of the present apparatus.
Preferably, the heating response device is fluid bed or rotary kiln, since it may ensure that best mass transfer and heat transfer.
Particularly preferably use recirculating fluidized bed because in recirculating fluidized bed close phase and it is disposed thereon there is also
Temperature difference between the gas zone of grain can be with very little.According to the utility model, the temperature difference is not more than 20 DEG C, particularly preferably in 0-
Between 10 DEG C.The small one side of the temperature difference ensures temperature necessary to removing arsenic and/or antimony.On the other hand, other solids are not up to
Fusion temperature, to avoid the formation of coalescence.This coalescence can damage the present apparatus, because they can cause particle size uneven
It is even, thus again it is impossible to ensure that all particles are in fluid bed fluidization.
To ensure reliable operation, when especially with fluid bed, have further been discovered that advantageous way is first by flue
Dust granulating.In general, flue dust is mainly to exist with the grain size less than 10 μm.In the micronized stage, size 100-500 is generated
μm particle (60-100wt% based on particle).Step is set to simplify because of particle size uniformity and because being relatively large in diameter, this is advantageous
In heat treatment.In a fluidized bed, all particles can reliably fluidization on an equal basis.
In addition advantageous way be granulation process and/or with carbon compound conduct has been added in binder mixed process
Reducing agent.
The advantages of reducing agent is added is to ensure that the fabulous mass transfer between reducing agent and flue dust.And it need not be subsequent
Mixed effect is considered in heating process, especially in a fluidized bed.Therefore, using solid carbonaceous reductant, especially coal and/or life
Substance or the like is desirable.
Preferably, the device of the utility model contains carries out granulated processed granulation dress to the flue dust before heating
It sets.The granular mass generated can be improved by binder, and flue will not be generated again because of particle fragmentation by thereby guaranteeing that
Dust, this flue dust are discharged via exhaust gas.Particularly, in bed process, the stability of particle is decisive, to ensure
All particles have the similar residence time in a fluidized bed, to reliably isolate arsenic and/or antimony or the like.
It is proved that real at a temperature of granulation step preferably should be at a temperature of between 20-200 DEG C, preferably 40-120 DEG C
It applies, because the stability of particle is especially high under this condition.Make granulation in 20 Hes it is preferred, therefore, that the granulating device contains
The heating element carried out at a temperature of between 200 DEG C.
The heating response device is designed as heating and is carried out under inertia or reducing atmosphere.
The use of the advantages of inert atmosphere is that process conditions can be adjusted very well.
And with reducing atmosphere can cause must use less carbon containing reducer, or at least partly carbon containing reducer be with
What gaseous state rather than solid-state form introduced.Particularly suitable the utility model is to use carbon monoxide (CO) and/or methane (CH4) or
Analog is as reducing agent.
Preferably, the heating response device is designed as heating carries out at a temperature of between 500 and 1200 DEG C.It is preferred that
Implement at a temperature of between 750-950 DEG C.At these tem-peratures, it can be ensured that high tumble, without fusing and therefore caused
The phenomenon that grain coalescence.
To improve treatment effeciency, another advantageous way is that recycling at least part is hot after heating and is recycled into
Grain process and/or heating process.For this purpose, gained calcine is cooled down.Preferably, the temperature being cooled between 100-200 DEG C
Degree.
Suitable coolant includes gaseous state and liquid coolant.Although heat transfer coefficient is relatively low and thermal capacity is relatively low, use
Gaseous coolant especially air is desirable, because the gas can be also used in heating stepses, such as is made in bed process
Be preheating fluidizing gas for heating, thus can reduce the further of energy and input and/or the air can be in atomization process
In be used for temperature adjust.
The exhaust gas being discharged from fluid bed furnace includes also CO and sulphur compound, preferably provides late combustion phase.Implemented
Late combustion phase makes the arsenic contained by only fraction be oxidized to arsenic (V) from As (III).Gained energy is micro- in preheating and upstream
Granulation can be all utilized.
In addition, obtaining solid particle in this late combustion phase, recycled in micronized and/or heating process, in this way
Wherein valuable product is still contained in and interior can recycle.It is useful for from institute it is preferred, therefore, that the device of the utility model contains
State the recovery line for recycling at least part heat in heating response device and being supplied to atomization process and/or heating response device.
Preferably, the device of the utility model contains the pipeline that exhaust gas is imported to the stage after combustion from heating response device, wherein,
The 0.1-30wt% of the arsenic contained in exhaust gas stages after combustion are oxidized to arsenic (V) by arsenic (III).
Preferably, the device of the utility model contains solid material that be transmitted to the melting from the heating response device anti-
Answer the feed pipeline of device.
Preferably, the feed pipeline contains at least one cooling device.
More purposes, feature, advantage and possible application of the utility model can also be from following exemplary embodiments
It is learned in the description of attached drawing.The form of description and combinations thereof of the feature and utility model itself that are described, independent of it
Whether be included in the claims.
Description of the drawings：
Fig. 1 shows the device that the downstream cooling of energy efficiency is improved by the band of the utility model, and
Fig. 2 shows the schematic diagrames of complete exhaust after-treatment.
Specific implementation mode
In Fig. 1, the flue dust containing arsenic and/or antimony imports micronizer 10 via pipeline 11.Solid form contains
Carbonaceous reducing agent such as coal or biomass can be added through pipeline 12.Binder can be further provided for micronizer via pipeline 13
10.The supply of certain several components can also be realized via common supply pipeline, can be mixed each other in advance in this way.If no
Carbon containing reducer is introduced here, then this addition must carry out afterwards.
The particle obtained in micronizer 10, a diameter of 100-500 μm of wherein 60-100wt%, through pipeline 14
It introduces reactor 20 and/or introduces venturi drier 93 through pipeline 34.Stream containing solid enters second point through pipeline 94
From such as cyclone of equipment 96.Charging is sent from the second separation equipment 96 through pipeline 15 to reactor.20 preferred design of reactor
At recirculating fluidized bed.In reactor 20, particle is heated to temperature, preferably 750-950 DEG C of temperature between 650-1000 DEG C
Degree.Fluidizing gas is introduced into reactor through pipeline 21.Gained process gas is discharged through pipeline 24.
Gaseous state carbon containing reducer such as CO and/or methane can also be introduced via pipeline 23.Meanwhile it also can be through not showing pipeline
It introduces carbonaceous solids material and enters reactor 20 as reducing agent.
20 energy for heating of input reactor can in an ordinary way realize that such as fluidizing gas can play combustion simultaneously
Expect gas, reaction reagent and/or energy carrier.
Obtained solid calcines sand and at least sizable part or can also be together with whole waste gas streams via pipe
Line 24 is discharged and is supplied to the first cyclone separator 90.
In this cyclone separator 90, solid and calcining sand in exhaust gas are at least partly recycled to reaction through pipeline 92
Device 20.Fraction solids stream is discharged into calcining sand cooler 30 through pipeline 22, wherein the heat part calcined is transferred to fluidizing gas
21.Final product is discharged through pipeline 25.
It still carries fine dust, particularly the hot waste gas of grain size≤50 μm particle is supplied to venturi drier 93 through pipeline 91.
In venturi drier 93, exhaust gas is further cooling and realizes solid and exhaust gas separation.Including heat in the offgas can be through
Unshowned hot material circulation moves on to the micronized stage 10.
Fig. 2 shows gained waste gas streams together with the complete last handling process of corresponding energy conception.
By flue dust through pipeline 11, carbonaceous solids reducing agent through pipeline 12 and binder (bentonite and/or other inorganic
Binder, cellulosic cpd and/or other organic binders) through the introducing micronizer 10 of pipeline 13.Herein, merge feed
And/or it is all possible to save reducing agent and/or the addition of binder.
After the 60-100wt% micronizeds of material are introduced into the particle of 100-500 μm of grain size, gained particle draws through pipeline 14
Enter reactor 20 and/or introduce Venturi tube drier 93 through pipeline 34, as Fig. 1 illustrates.
Reactor 20 is preferably designed in a circulating fluid bed reactor.Including the hot waste gas of fine dust is via pipeline 24
It is discharged and is supplied to after-combustion 40.
Most of exhaust gas is supplied to through pipeline 42 and cools down equipment 50 with heat recovery system and/or the exhaust gas of quenching.Part
The heat of recycling can use in the other places of the present apparatus, for example, reducing the energy requirement roasted in reactor 20.Still contain flue powder
The hot waste gas of dirt flows through pipeline 51 and is supplied to hot electrostatic precipitator such as electrofilter 60, and wherein, fine dust is separated,
And such as micronizer 10 can be recycled in the form of (not shown).It cleans in such a way and cooling exhaust gas is through pipeline
61 flow into another humid gas purification 70.In this way, including sulphur compound in the offgas can be detached and through pipeline 71
It is finally fed equipment 80 for producing sulfuric acid with 72, sulfuric acid can therefrom be discharged through pipeline 81.
Portion gas stream from humid gas clarifier 70 through pipeline 73 is supplied to heat recovery system 74 and through pipeline 75
Not shown pipeline is re-circulated into reactor.Due to this circulation loop, the sulfur content in system is continuously enriched with, in this way
Highly beneficial to producing the operation of downstream plant of sulfuric acid under conditions of corresponding control, especially discharging has and is sufficient for
Sulfuric acid plant high sulfur content (>5% (volume) SO2)。
Finally, solid portion, which is calcined, takes out from reactor 20 after sand is successfully heat-treated and is supplied to cooling through pipeline 23
Equipment 30 and/or as illustrated in Figure 1 from recirculation flow through be not shown pipeline take out.Preferably, cooling equipment 30 is designed as flowing
Change bed cooler, is advantageous because being proved preheating of the hot gas that will be obtained through the supply micronizer 10 of pipeline 31.With
This is corresponding, obtained hot gas, preferably hot-air, and the fluidisation pipeline 21 of reactor 20 can also be fed to through pipeline 32.
Calcining sand after cooling takes out through pipeline 33 from cooling stage 30.Then smeltery's extraction, which can be sent to, includes
The metal of value such as Cu, Ni etc..
Figure numbers list:
10 micronizers
11-15 pipelines
20 reactors
21-26 pipelines
30 cooling equipment
31-34 pipelines
40 after-combustion reactors
41,42 pipelines
50 heat recovery equipments
51 pipelines
60 gas-solid separation equipments
61 pipelines
70 moisture washers
71-73 pipelines
74 heat exchangers
75 pipelines
80 sulphuric acid devices
81 pipelines
93 Wen's driers
94-95 pipelines
96 cyclones
97 pipelines
Claims (10)
1. handling the device of the flue dust from pyrometallurgical method, which includes melting reactor, addition carbonaceous reducing agent
Equipment, detach by heating response device that the flue dust heats together with the carbonaceous reducing agent and by volatile component
Separator, it is characterised in that the device further includes micronizer, and the micronizer is for introducing the flue dust
It is granulated before the reactor, which contains the first charging gear, which is arranged in flotation
Water is added in product.
2. the apparatus according to claim 1, it is characterised in that the heating response device is fluid bed or rotary kiln.
3. the apparatus of claim 2, it is characterised in that the heating response device is recirculating fluidized bed.
4. the apparatus according to claim 1, it is characterised in that there are be granulated before heating to the flue dust
The granulating device of processing.
5. device according to claim 4, it is characterised in that in the granulating device there are by carbon compound and/
Or the second charging gear that binder is mixed with the flue dust.
6. according to claim 1-4 any one of them devices, it is characterised in that the heating response device be designed as heating be
It is carried out under inertia or reducing atmosphere.
7. according to claim 1-4 any one of them devices, it is characterised in that there are for from the heating response device
Recycling at least part heat and the recovery line for being supplied to atomization process and/or heating response device.
8. according to claim 1-4 any one of them devices, it is characterised in that exist to import exhaust gas from heating response device and fire
The pipeline in stage afterwards.
9. according to claim 1-4 any one of them devices, it is characterised in that there are solid material is anti-from the heating
Device is answered to be transmitted to the feed pipeline of the melting reactor.
10. device according to claim 9, it is characterised in that the feed pipeline contains at least one cooling device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721200235.0U CN207904338U (en) | 2017-09-19 | 2017-09-19 | The device of dearsenification and/or antimony from flue dust |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721200235.0U CN207904338U (en) | 2017-09-19 | 2017-09-19 | The device of dearsenification and/or antimony from flue dust |
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| CN114105111A (en) * | 2020-06-08 | 2022-03-01 | 美卓奥图泰芬兰有限公司 | Apparatus and method for treating solid material |
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