CN107201442A - A kind of system and method for handling zinc leaching residue - Google Patents
A kind of system and method for handling zinc leaching residue Download PDFInfo
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- CN107201442A CN107201442A CN201710418451.0A CN201710418451A CN107201442A CN 107201442 A CN107201442 A CN 107201442A CN 201710418451 A CN201710418451 A CN 201710418451A CN 107201442 A CN107201442 A CN 107201442A
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/02—Roasting processes
- C22B1/08—Chloridising roasting
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/14—Agglomerating; Briquetting; Binding; Granulating
- C22B1/24—Binding; Briquetting ; Granulating
- C22B1/2406—Binding; Briquetting ; Granulating pelletizing
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/14—Agglomerating; Briquetting; Binding; Granulating
- C22B1/24—Binding; Briquetting ; Granulating
- C22B1/242—Binding; Briquetting ; Granulating with binders
- C22B1/243—Binding; Briquetting ; Granulating with binders inorganic
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B13/00—Obtaining lead
- C22B13/02—Obtaining lead by dry processes
- C22B13/025—Recovery from waste materials
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B15/00—Obtaining copper
- C22B15/0026—Pyrometallurgy
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B19/00—Obtaining zinc or zinc oxide
- C22B19/30—Obtaining zinc or zinc oxide from metallic residues or scraps
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B58/00—Obtaining gallium or indium
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/001—Dry processes
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- 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
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Abstract
The present invention relates to a kind of system and method for handling zinc leaching residue.In the system, mixing device has zinc leaching residue entrance, chlorinating agent entrance, reducing agent entrance, binding agent entrance, compound outlet；Press ball device has compound entrance, green-ball outlet, and compound entrance is connected with compound outlet；Chloridising roasting device includes preheating section, chlorination reaction section, iron reduction section successively, preheating section has green-ball entrance, chlorination reaction section is provided with flue, iron reduction section has metallized pellet outlet, and green-ball entrance is connected with green-ball outlet, separated between each region by baffle plate, so that each region forms closing space respectively, conveyer is provided with below baffle plate, conveyer includes controller, and controlling baffle plate lower end is opened or closed.The present invention can realize the separation of iron and other non-ferrous metals in zinc leaching residue at a lower temperature, shorten technological process, reduce production cost.
Description
Technical field
The present invention relates to metallurgical technology field, and in particular to a kind of system and method for processing zinc leaching residue.
Background technology
At present, the processing method of zinc leaching residue mainly includes high temperature reduction volatility process and aqueous solution lixiviation process.High temperature reduction is waved
Hair method is that coke powder is incorporated in zinc leaching residue as reducing agent, and high-temperature roasting or melting are carried out in rotary kiln or fuming furnace,
Make the reduction volatilizations such as valuable metal lead, zinc, silver, indium.Aqueous solution lixiviation process includes two kinds：Directly by zinc leaching residue acid or aqueous slkali
Leached；Zinc leaching residue pre- calcination between 500~700 DEG C, obtained slag leaches metal therein using acid or aqueous slkali again.
The advantage of high temperature reduction volatility process is can be while reclaim the lead in zinc leaching residue, zinc, indium etc., can be by these elements
All collect into zinc oxide fumes, but high energy consumption, and output containing scum due to being in melt state during volatilization zinc, melt
A large amount of silicate are mixed into body, cause the yield containing iron in scum relatively low.The advantage of aqueous solution lixiviation process is containing after leaching
The content of iron reaches 55wt% (wt% is mass percent) left and right in scum, but Zn content is higher in slag, generally 1wt% with
On, and it is main with the presence of zinc ferrite form, as iron-smelting raw material in use, zinc can be adversely affected to ironmaking processes.
When handling zinc leaching residue using hydrometallurgy, by the difference of leachate deferrization process, goethite process, red iron can be divided into
Ore deposit method and jarosite process etc..Wherein, jarosite process have that easy Precipitation, solubility are low, filterability is good, reagent consumption
Less, the low advantage of production cost, is widely used.Jarosite process is that to be formed selectively the ferro element in zinc lixiviating solution heavy
Form sediment, so as to reach iron, the purpose of zinc separation.Meanwhile, the valuable metal such as some zinc, lead, silver is with silicate and sulfuric acid
The form of salt enters iron vitriol slag.At present, the amount of iron vitriol slag is stored up more than 30,000,000 tons by China, and with annual 1000000 tons of speed
Degree increases, and huge potential pollution is produced to environment.Also, valuable metal loss is big, if iron vitriol slag presses averagely 5wt% containing zinc
Calculate, then the zinc amount of metal accumulated is more than 1,500,000 tons, and value is very high.Therefore, carrying out further investigation to zinc leaching residue has weight
Big meaning.
The content of the invention
The present invention is intended to provide a kind of system and method for handling zinc leaching residue, the present invention can be realized at a lower temperature
The separation of iron and other non-ferrous metals in zinc leaching residue, shortens technological process, reduces production cost.
The invention provides a kind of system for handling zinc leaching residue, including mixing device, press ball device, chloridising roasting device.
There is the mixing device zinc leaching residue entrance, chlorinating agent entrance, reducing agent entrance, binding agent entrance, compound to go out
Mouthful.
The press ball device has compound entrance, green-ball outlet；The compound entrance is mixed with the mixing device
Close material outlet connection.
The chloridising roasting device includes preheating section, chlorination reaction section, iron reduction section successively, and the preheating section has green-ball
Entrance, the chlorination reaction section is provided with flue, and the iron reduction section has metallized pellet outlet, the green-ball entrance and institute
State the green-ball outlet connection of press ball device.
Separated between the preheating section and chlorination reaction section by baffle plate, by keeping off between the chlorination reaction Duan Yutie reduction sections
Plate is separated so that the preheating section, chlorination reaction section, iron reduction section form closing space respectively.It is provided with below the baffle plate
Conveyer, the conveyer includes controller, controls the baffle plate lower end to open or close.
Further, in addition to cooling device and mill ore magnetic selection device；The cooling device have metallized pellet entrance,
Metallized pellet outlet is cooled down, the metallized pellet entrance is connected with the metallized pellet outlet of the chloridising roasting device；
The mill ore magnetic selection device has cooling metallized pellet entrance, an iron outlet, the cooling metallized pellet entrance with it is described cold
But the cooling metallized pellet outlet connection of device.
It is preferred that, one end of the conveyer is connected with the green-ball outlet of the press ball device, is received by the green-ball
The green-ball for exporting discharge is simultaneously sent into the chloridising roasting device by the green-ball entrance, the other end of the conveyer with
Metallized pellet outlet connection, exports metallized pellet.
It is preferred that, the angle of the baffle plate and vertical direction is 0~15 °.
It is preferred that, the flue is located at the top of chlorination reaction section, and close to the iron reduction section.
The invention also provides a kind of method that utilization said system handles zinc leaching residue, including step：
By zinc leaching residue, chlorinating agent, reducing agent, binding agent according to quality proportioning be 100：(15~20)：(10~15)：(5~
10) send into the mixing device and be well mixed, obtain compound.
The compound is sent into compacting in the press ball device and obtains green-ball.
Water content is sent into the chloridising roasting device for the 8~20wt% green-ball, the transmission dress is placed in
Put, the green-ball sequentially pass through the preheating section, chlorination reaction section, iron reduction section preheated, chlorination reaction, iron reduction instead
Should, metal chloride and metallized pellet are obtained, the metal chloride is delivered in the flue and collected.
Further, the metallized pellet is sent into the mill ore magnetic selection device, is handled through mill ore magnetic selection and reclaim iron.
It is preferred that, granularity≤3mm of the zinc leaching residue.The chlorinating agent is from one in sodium chloride, calcium chloride, potassium chloride
Kind or several mixtures, the mesh of the granularity of the chlorinating agent≤200.The reducing agent selects anthracite, the grain of the reducing agent
Degree≤3mm.The binding agent selects inorganic binder.
It is preferred that, the water content of the green-ball is 10~15wt%.
It is preferred that, temperature≤500 DEG C of the warm, the time is 3~5min.The chlorination reaction temperature is 700
~800 DEG C, the time is 15~20min.The iron reduction reaction temperature is 1000~1200 DEG C, and the time is 20~25min.
The present invention handles the green-ball containing zinc leaching residue using the method for chloridising roasting, and strictly each stage is reacted in control
Temperature and time, the separation of non-ferrous metal and iron in zinc leaching residue can be realized at a lower temperature, reduce energy consumption of reaction.
In the method for the present invention, chlorinating agent is added in the feed, the synthetical recovery of various metals can be achieved so that zinc leaching residue
In copper can also generate chlorination copper fumes and be volatized into flue, so as to realize the separation of iron and lead, zinc, indium, copper, obtain pure
The higher iron powder of degree, and traditional carbonaceous reduction reaction is to be difficult to efficiently separating for copper and iron.Also, chlorinating agent plus
Enter to reduce the consumption of reducing agent coal dust, and the reduction of coal dust contributes to the progress of chlorination reaction.Meanwhile, chlorination is anti-
The temperature reduction answered, realizes energy-saving purpose.
Also, the present invention is sent directly into progress chloridising roasting processing in chloridising roasting device using by qualified aqueous green-ball
Zinc leaching residue, is technically a kind of breakthrough, can be by strictly controlling the temperature and time in chloridising roasting each stage to reach this hair
The purpose of bright separating valuable metals, eliminates drying unit, so as to shorten technique stream compared with traditional dry bulb enters stove roasting
Journey, reduces production cost.
Brief description of the drawings
Fig. 1 is the system schematic of processing zinc leaching residue in the embodiment of the present invention.
Fig. 2 is the method flow schematic diagram of processing zinc leaching residue in the embodiment of the present invention.
Reference in accompanying drawing is as follows：
100- mixing devices；
200- press ball devices；
300- chloridising roastings device, 301- preheating sections, 302- chlorination reactions section, 303- iron reduction section, 304- flues, 305-
Baffle plate, 306- conveyers；
400- mill ore magnetic selection devices.
Embodiment
Below in conjunction with drawings and examples, the embodiment to the present invention is described in more details, so as to energy
Enough more fully understand the solution of the present invention and the advantage of its various aspects.However, specific embodiments described below and reality
Apply the purpose that example is only explanation, rather than limitation of the present invention.
By Fig. 1, the system of processing zinc leaching residue proposed by the present invention, including mixing device 100, press ball device 200, chlorination roasting
Burn device 300.
Mixing device 100 is used for mixed material, obtains compound, it has zinc leaching residue entrance, chlorinating agent entrance, reducing agent
Entrance, binding agent entrance, compound outlet.
Press ball device 200 be used for by compound it is compressing, its have compound entrance, green-ball outlet.Wherein, compound
Entrance is connected with the compound outlet of mixing device 100.
Chloridising roasting device 300 includes preheating section 301, chlorination reaction section 302, the iron reduction section 303 being sequentially connected, and is used for
Receive the green-ball exported by press ball device 200 and chloridising roasting processing is carried out to green-ball.Also, preheating section 301 and chlorination reaction
Baffle plate 305 is provided between section 302, baffle plate 305 is provided between chlorination reaction section 302 and iron reduction section 303.In the present invention,
The setting of baffle plate 305 to form closing respectively between preheating section 301, chlorination reaction section 302,303 3 regions of iron reduction section
Space.
The lower section of baffle plate 305 is provided with conveyer 306, for placing and transmitting material.Wherein, the upper end of baffle plate 305
On the inwall for being fixed on the top of chloridising roasting device 300, the lower end of baffle plate 305 is connected with conveyer 306.It is excellent as the present invention
The embodiment of choosing, baffle plate 305 and the angle of vertical direction are 0~15 °.Controller is provided with conveyer 306, for controlling
Open or close in the lower end of baffle plate 305 processed.
When green-ball is entered in chlorination reaction section 302 by preheating section 301, baffle plate 305 is opened, and green-ball enters chlorination reaction section
302, closed by finishing rear baffle, controller of the process on conveyer 306, which is realized, to be automatically controlled.After chlorination reaction
Obtained pelletizing enters the process of iron reduction section 303 as above.
Preheating section 301 is provided with green-ball entrance, and the green-ball entrance is connected with the green-ball outlet of press ball device 200, for connecing
Receive the green-ball exported by press ball device 200.Chlorination reaction section 302 is provided with flue 304.It is used as currently preferred embodiment party
Formula, flue is arranged on the top of chlorination reaction section 302, also, in the position close to iron reduction section 303, is easy to recovery chlorination anti-
Answer the metal chloride flue dust that process is obtained.Metallized pellet outlet is provided with iron reduction section 303, for exporting green-ball through chlorine
Change the metallized pellet obtained after calcination process.
As the preferred embodiment of the invention, one end of conveyer 306 is connected with the green-ball outlet of press ball device 200,
The green-ball of green-ball outlet discharge is placed on conveyer 306, is forwarded by conveyer 306, green-ball is entered via green-ball
In mouth feeding chloridising roasting device 300, the chloridising roasting processing of green-ball is carried out.Also, the other end and metal of conveyer 306
Pellet outlet connection, for exporting metallized pellet.That is, in the preferred embodiment of the invention, conveyer 306 is located at gear
Plate lower end and through among chloridising roasting device 300, for preheating section 301, chlorination reaction section 302, iron reduction section 303 it
Between transmit material, and do not influence regional to form independent and closing space.
In different embodiments of the invention, the system also includes cooling device and (selects and do not show in conventional chilling device, figure
Go out) and mill ore magnetic selection device 400, cooling device, which is used to receiving metallized pellet, to be cooled down, and is then fed into mill ore magnetic selection device
Mill ore magnetic selection obtains metallic iron in 400.Wherein, cooling device has metallized pellet entrance, the outlet of cooling metallized pellet, gold
Category pellet entrance is connected with the metallized pellet outlet of chloridising roasting device 300.Mill ore magnetic selection device 400 has cooling metal
The cooling metallized pellet outlet of pellet entrance, iron outlet, cooling metallized pellet entrance and cooling device is connected.
In the present invention, preheating section 301, chlorination reaction section 302, iron reduction section 303, flue 304, baffle plate 305, biography are not limited
The quantity of device 306 is sent, can realize that the purpose of the present invention is defined.
The invention also provides a kind of method for handling zinc leaching residue, as shown in Fig. 2 being one of embodiment of the invention
Schematic flow sheet, including step：
(1) raw material is mixed
By zinc leaching residue, chlorinating agent, reducing agent, binding agent according to quality proportioning be 100：(15~20)：(10~15)：(5~
10) it is well mixed in feeding mixing device 100, obtains compound.It is preferred that, in addition to step：Zinc leaching residue is dried, crushed,
It is sized to granularity≤3mm.It is preferred that, the zinc leaching residue granularity of selection is the mesh of 325 mesh~200 so that the lead that contains in zinc leaching residue,
The non-ferrous metals such as zinc, copper, indium are fully contacted with chlorinating agent, promote the progress of follow-up chlorination reaction.
In the present invention, the composition of zinc leaching residue is：All iron content is 28~35.5wt%, and Zn content is 16~18wt%, lead
Content is 1.0~3.5wt%, and copper content is 0.5~1.5wt%, and indium content is 0.15~0.28wt%.
In the present invention, chlorinating agent need to be crushed to the mesh of granularity≤200.Wherein, the preferred sodium chloride of chlorinating agent (801 DEG C of fusing point),
One or more of mixtures in calcium chloride (782 DEG C of fusing point) or potassium chloride (771 DEG C of fusing point).
Reducing agent need to be crushed to granularity≤3mm.In the present invention, the preferred anthracite of reducing agent.Binding agent selects inorganic bond
Agent.Wherein, the preferred bentonite of binding agent.
(2) green-ball is prepared
Suppressed in the compound feeding press ball device 200 that above-mentioned steps are obtained, obtain green-ball.The green-ball be containing
The aqueous green-ball of chlorinating agent and reducing agent.
(3) green-ball carries out chloridising roasting processing
The qualified green-ball of water content is sent directly into chloridising roasting device 300 without drying and processing and carried out at chloridising roasting
Reason.Green-ball is placed on conveyer 306, is transferred into successively in preheating section 301, chlorination reaction section 302, iron reduction section 303,
Preheated respectively, chlorination reaction, iron reduction reaction, obtain metal chloride and metallized pellet.Wherein, metal chloride is in
Flue dust shape volatilizees, and is collected in flue 304.Metallized pellet is sent into mill ore magnetic selection device 400 and ground after cooling
Ore deposit magnetic separation is handled, isolated metallic iron and tailings.That is, the separation of iron and other non-ferrous metals in zinc leaching residue is realized.
In the step, the water content for controlling green-ball is 8~20wt%.It is preferred that, control the water content of green-ball for 10~
15wt%.The satisfactory green-ball of water content is sent directly into chloridising roasting device 300 and carries out chloridising roasting, it is necessary to strict control
Green-ball processed is in chlorination reaction 302 residence times of section and temperature.On the one hand, the temperature of control chlorination reaction section 302 is unsuitable too high,
Prevent green pellet cracking；On the other hand, the moisture in control green-ball slowly is evaporated to form wet atmosphere so that chlorinating agent and moisture
Vapor reaction generation hydrogen chloride gas in atmosphere, it is ensured that the supply in chlorination reaction chlorine source, hydrogen chloride gas more holds than chlorine
Easily reacted with metal oxide, so as to promote the progress of non-ferrous metal chlorination reaction.In chlorination reaction process, in zinc leaching residue
The metals such as the zinc, lead, indium, the copper that contain form corresponding chloride flue dust and volatilized, and are collected in flue 304, from
And realize the separation of non-ferrous metal and metallic iron.
In an embodiment of the present invention, the temperature of control green-ball into chloridising roasting device 300 is not higher than 500 DEG C, i.e., pre-
Temperature≤500 DEG C of hot arc 301, can prevent aqueous green-ball from bursting.Also, green-ball is controlled in the stop of preheating section 301
Between be 3~5min.
In chlorination reaction process, control chlorination reaction section 302 temperature be 700~800 DEG C, the residence time be 15~
20min.In the temperature range, the solid chlorinating agent in green-ball reaches and volatilized after fusing point, the water produced with green-ball heating evaporation
Vapor reaction generates hydrogen chloride gas.Because the moisture in green-ball is constantly evaporated, newly-generated hydrogen chloride gas constantly with
Chlorination reaction occurs for the oxide of lead, zinc, copper, indium in zinc leaching residue etc., generates corresponding chloride flue dust, is volatized into flue
304 are collected.Meanwhile, the iron in zinc leaching residue is present in solid pelletizing, so as to realize the separation of iron and other metals.
In the present invention, the temperature for controlling iron reduction section 303 is 1000~1200 DEG C, and the residence time is 20~25min, it is ensured that
The abundant reduction of ferriferous oxide.
By above-mentioned chloridising roasting processing procedure, volatility >=97.24% of lead in aqueous green-ball, the volatility of zinc >=
98.38%, volatility >=81.52% of copper, volatility >=96.28% of indium.In obtained metallized pellet, full Iron grade ＞
35%, degree of metalization >=76%.The Iron grade ＞ 96.25% that metallized pellet is reclaimed through mill ore magnetic selection, iron recovery ＞
96.85%.
Embodiment 1
The composition of zinc leaching residue that the present embodiment is selected is：All iron content is 32.52wt%, and Zn content is 16.02wt%, lead
Content is 3.30wt%, and indium content is 0.20wt%, and copper content is 0.80wt%.Granularity≤3mm of zinc leaching residue.Chlorinating agent is selected
Calcium chloride, particle size reduction to≤200 mesh.Reducing agent selects Ningxia coal (fixed carbon 82.56wt%, volatile matter 6.49wt%, ash content
10.02wt%, moisture 0.93wt%, sulphur 0.51wt%), particle size reduction to≤3mm.Binding agent selects bentonite.By zinc leaching residue,
Calcium chloride, Ningxia coal, bentonite are according to 100：15：10：5 ratio carries out pressure ball after fully mixing, and it is 10% to obtain water content
Green-ball.Green-ball is sent into chloridizing roaster, charging temperature is 480 DEG C, the preheating section residence time is 3min, chlorination reaction section
Temperature is 780 DEG C, and the residence time is 15min.In chlorination reaction section, the heated volatilization of calcium chloride, evaporates with green-ball at such a temperature
The oxide and hydrogen chloride gas of lead, zinc, indium, copper etc. occur in the vapor reaction generation hydrogen chloride gas of generation, zinc leaching residue
Chlorination reaction generates metal chloride flue dust, is volatized into flue, realizes the separation with iron.Wherein, the volatility of lead is
97.28%, the volatility of zinc is 98.38%, and the volatility of copper is 81.52%, and the volatility of indium is 96.30%.Green-ball is through chlorine
Change and pelletizing is obtained after reaction, and enter iron reduction section, temperature control is at 1100 DEG C, and the recovery time is 20min, and ferriferous oxide is gone back
Original, obtains metallized pellet.It is 96.56% that metallized pellet carries out mill ore magnetic selection and obtains full Iron grade after cooling, and iron is reclaimed
Rate is 97.85% metallic iron.
Embodiment 2
The composition of zinc leaching residue that the present embodiment is selected is：All iron content is 35.08wt%, and Zn content is 16.28wt%, lead
Content is 2.20wt%, and indium content is 0.25wt%, and copper content is 1.20wt%.Granularity≤3mm of zinc leaching residue.Chlorinating agent is selected
Calcium chloride, particle size reduction to≤200 mesh.Reducing agent selects Ningxia coal (fixed carbon 82.56wt%, volatile matter 6.49wt%, ash content
10.02wt%, moisture 0.93wt%, sulphur 0.51wt%), particle size reduction to≤3mm.Binding agent selects bentonite.By zinc leaching residue,
Calcium chloride, Ningxia coal, bentonite are according to 100：15：10：5 ratio carries out pressure ball after fully mixing, and it is 12% to obtain water content
Green-ball.Green-ball is sent into chloridizing roaster, charging temperature is 500 DEG C, the preheating section residence time is 5min, chlorination reaction section
Temperature is 800 DEG C, and the residence time is 20min.In chlorination reaction section, the heated volatilization of calcium chloride, evaporates with green-ball at such a temperature
The oxide and hydrogen chloride gas of lead, zinc, indium, copper etc. occur in the vapor reaction generation hydrogen chloride gas of generation, zinc leaching residue
Chlorination reaction generates metal chloride flue dust, is volatized into flue, realizes the separation with iron.Wherein, the volatility of lead is
98.02%, the volatility of zinc is 98.62%, and the volatility of copper is 81.76%, and the volatility of indium is 96.66%.Green-ball is through chlorine
Change and pelletizing is obtained after reaction, and enter iron reduction section, temperature control is at 1100 DEG C, and the recovery time is 20min, and ferriferous oxide is gone back
Original, obtains metallized pellet.It is 97.28% that metallized pellet carries out mill ore magnetic selection and obtains full Iron grade after cooling, and iron is reclaimed
Rate is 98.08% metallic iron.
Embodiment 3
The composition of zinc leaching residue that the present embodiment is selected is：All iron content is 30.76wt%, and Zn content is 17.86wt%, lead
Content is 3.54wt%, and indium content is 0.23wt%, and copper content is 1.09wt%.Granularity≤3mm of zinc leaching residue.Chlorinating agent is selected
Potassium chloride, particle size reduction to≤200 mesh.Reducing agent selects Ningxia coal (fixed carbon 82.56wt%, volatile matter 6.49wt%, ash content
10.02wt%, moisture 0.93wt%, sulphur 0.51wt%), particle size reduction to≤3mm.Binding agent selects bentonite.By zinc leaching residue,
Calcium chloride, Ningxia coal, bentonite are according to 100：20：15：10 ratio carries out pressure ball after fully mixing, and obtains water content and is
15wt% green-ball.Green-ball is sent into chloridizing roaster, charging temperature is 490 DEG C, the preheating section residence time is 5min, chlorination
Conversion zone temperature is 770 DEG C, and the residence time is 20min.In chlorination reaction section, the heated volatilization of potassium chloride at such a temperature, with life
The oxide and hydrogen chloride gas of lead, zinc, indium, copper etc. in the vapor reaction generation hydrogen chloride gas that ball evaporation is produced, zinc leaching residue
Chlorination reaction generation metal chloride flue dust occurs for body, is volatized into flue, realizes the separation with iron.Wherein, the volatilization of lead
Rate is 97.98%, and the volatility of zinc is 98.56%, and the volatility of copper is 81.66%, and the volatility of indium is 96.72%.Green-ball
Pelletizing is obtained after chlorination reaction, and enters iron reduction section, temperature control is at 1000 DEG C, and the recovery time is 25min, ferriferous oxide
It is reduced, obtains metallized pellet.It is 96.30%, iron that metallized pellet carries out mill ore magnetic selection and obtains full Iron grade after cooling
The rate of recovery is 97.02% metallic iron.
Finally it should be noted that：Obviously, above-described embodiment is only intended to clearly illustrate example of the present invention, and simultaneously
The non-restriction to embodiment.For those of ordinary skill in the field, it can also do on the basis of the above description
Go out other various forms of changes or variation.There is no necessity and possibility to exhaust all the enbodiments.And thus drawn
Among the obvious changes or variations that Shen goes out is still in protection scope of the present invention.
Claims (10)
1. a kind of system for handling zinc leaching residue, it is characterised in that the system includes mixing device, press ball device, chloridising roasting
Device；
The mixing device has zinc leaching residue entrance, chlorinating agent entrance, reducing agent entrance, binding agent entrance, compound outlet；
The press ball device has compound entrance, green-ball outlet；The compound of the compound entrance and the mixing device
Outlet connection；
The chloridising roasting device includes preheating section, chlorination reaction section, iron reduction section successively, and there is the preheating section green-ball to enter
Mouthful, chlorination reaction section is provided with flue, and the iron reduction section has a metallized pellet outlet, the green-ball entrance with it is described
The green-ball outlet connection of press ball device；
The preheating section and chlorination reaction section between separated by baffle plate, between the chlorination reaction Duan Yutie reduction sections by baffle plate every
Open so that the preheating section, chlorination reaction section, iron reduction section form closing space respectively；Transmission is provided with below the baffle plate
Device, the conveyer includes controller, controls the baffle plate lower end to open or close.
2. system according to claim 1, it is characterised in that also including cooling device and mill ore magnetic selection device；It is described cold
But device has metallized pellet entrance, the outlet of cooling metallized pellet, the metallized pellet entrance and the chloridising roasting
The metallized pellet outlet connection of device；The mill ore magnetic selection device has cooling metallized pellet entrance, iron outlet, described cold
But metallized pellet entrance is connected with the cooling metallized pellet outlet of the cooling device.
3. system according to claim 1, it is characterised in that one end of the conveyer and the life of the press ball device
Ball outlet connection, receives and exports the green-ball of discharge by the green-ball and send into the chloridising roasting device by the green-ball entrance
In, the other end of the conveyer is connected with metallized pellet outlet, exports metallized pellet.
4. system according to claim 1, it is characterised in that the baffle plate and the angle of vertical direction are 0~15 °.
5. system according to claim 1, it is characterised in that the flue is located at the top of chlorination reaction section, and
Close to the iron reduction section.
6. the method that a kind of any described systems of utilization claim 1-5 handle zinc leaching residue, it is characterised in that including step：
By zinc leaching residue, chlorinating agent, reducing agent, binding agent according to quality proportioning be 100：(15~20)：(10~15)：(5~10)
Send into the mixing device and be well mixed, obtain compound；
The compound is sent into compacting in the press ball device and obtains green-ball；
Water content is sent into the chloridising roasting device for the 8~20wt% green-ball, is placed on the conveyer,
The green-ball sequentially pass through the preheating section, chlorination reaction section, iron reduction section preheated, chlorination reaction, iron reduction reaction, obtain
To metal chloride and metallized pellet, the metal chloride is delivered in the flue and collected.
7. method according to claim 6, it is characterised in that the metallized pellet is sent into the mill ore magnetic selection device
In, handled through mill ore magnetic selection and reclaim iron.
8. method according to claim 6, it is characterised in that granularity≤3mm of the zinc leaching residue；The grain of the chlorinating agent
Spend≤200 mesh；Granularity≤3mm of the reducing agent.
9. method according to claim 6, it is characterised in that the water content of the green-ball is 10~15wt%.
10. method according to claim 6, it is characterised in that temperature≤500 DEG C of the warm, the time is 3~
5min；The chlorination reaction temperature is 700~800 DEG C, and the time is 15~20min；The iron reduction reaction temperature be 1000~
1200 DEG C, the time is 20~25min.
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| CN201710418451.0A CN107201442A (en) | 2017-06-06 | 2017-06-06 | A kind of system and method for handling zinc leaching residue |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111979422A (en) * | 2020-07-09 | 2020-11-24 | 有研资源环境技术研究院(北京)有限公司 | Method for comprehensively recovering valuable metals in goethite slag |
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| CN206828593U (en) * | 2017-06-06 | 2018-01-02 | 江苏省冶金设计院有限公司 | A kind of system for handling zinc leaching residue |
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| DE2603096A1 (en) * | 1975-01-28 | 1976-07-29 | Kowa Seiko Co Ltd | PROCEDURE FOR DUST RECYCLING |
| CN101787434A (en) * | 2010-02-23 | 2010-07-28 | 吕伟鹏 | Method for recovering iron and tin-lead-zinc from magnetic separation waste residue by rotary kiln through deoxygenation, chloridization and oxidation |
| CN101886176A (en) * | 2010-07-10 | 2010-11-17 | 吕伟鹏 | Method for reducing, chloridizing, oxidizing and recovering iron, tin, lead and zinc in waste magnetic separation dreg in rotary kiln without pelletizing |
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| CN111979422A (en) * | 2020-07-09 | 2020-11-24 | 有研资源环境技术研究院(北京)有限公司 | Method for comprehensively recovering valuable metals in goethite slag |
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