CN106435205A

CN106435205A - System and method of treating zinc leaching residues

Info

Publication number: CN106435205A
Application number: CN201611058837.7A
Authority: CN
Inventors: 吴道洪; 王健月; 古明远; 吴佩佩; 曹志成; 薛逊
Original assignee: Jiangsu Province Metallurgical Design Institute Co Ltd
Current assignee: Jiangsu Province Metallurgical Design Institute Co Ltd
Priority date: 2016-11-24
Filing date: 2016-11-24
Publication date: 2017-02-22

Abstract

The invention discloses a system and method of treating zinc leaching residues. The system comprises a zinc leaching residue fine grinding device, a reducing agent fine grinding device, a flux fine grinding device, a mixing device, a forming device, a drying device, a rotating bed, a water quenching device and an ore grinding-magnetic separation unit; the mixing device is provided with a fine zinc leaching residue inlet, a fine reducing agent inlet, a fine flux inlet and a mixture outlet; the forming device is provided with a mixture inlet and a hybrid pellet outlet; the drying device is provided with a hybrid pellet inlet and a dry pellet outlet; the rotating bed is provided with a dry pellet inlet, a lead-zinc-silver containing dust outlet and an iron containing high temperature roasting product outlet; the water quenching device is provided with an iron containing high temperature roasting product inlet and a water quenched material outlet; and the ore grinding-magnetic separation unit is provided with a water quenched material inlet, a metal iron powder outlet and a tailing outlet. With adoption of the system, valuable metal elements including lead, zinc, silver and iron in the zinc leaching residues can be comprehensively recovered and utilized, wherein the recovery rates of the lead and the zinc are above 95 percent, the recovery rate of the silver is about 90 percent, and the iron grade and the recovery rate of the metal iron powder are about 90 percent.

Description

The system and method processing zinc leaching residue

Technical field

The invention belongs to resource regeneration technical field, specifically, the present invention relates to a kind of process zinc leaching residue System and method.

Background technology

Zinc leaching residue is a kind of solid waste slag producing in Zinc Hydrometallurgy Process, containing zinc, lead, copper, ferrum, gallium, germanium, indium With valuable metal elements such as silver, there is great comprehensive utilization value.Currently, main to the technique of zinc hydrometallurgy leaching residue treating There are wet processing, thermal process, floatation process, selecting smelting combination technique etc..In actual production process, no matter adopt thermal process Or wet processing all exists, and process conditions are harsh, refractory consumption rate is big, equipment investment and maintenance cost is high, working environment The shortcomings of difference, high energy consumption.Additionally, being difficult to reclaim according to valuable metal in single floatation process then slag, waste residue is secondary to utilize effect Really undesirable.

Therefore, the existing technology to zinc hydrometallurgy leaching residue treating is further improved.

Content of the invention

It is contemplated that at least solving one of technical problem in correlation technique to a certain extent.For this reason, the present invention One purpose is to propose a kind of system and method processing zinc leaching residue, can realize lead zinc in zinc leaching residue using this system The comprehensive reutilization of silver-colored ferrum valuable metal element, wherein, lead, the response rate of zinc are more than 95%, and the response rate of silver is 90% Left and right), the Iron grade of gained metal iron powder and the response rate are 90% about.

In one aspect of the invention, the present invention proposes a kind of system processing zinc leaching residue.Reality according to the present invention Apply example, described system includes：

Zinc leaching residue fine mill, described zinc leaching residue fine mill has zinc leaching residue entrance and zinc leaching residue fines goes out Mouthful；

Reducing agent fine mill, described reducing agent fine mill has reducing agent entrance and the outlet of reducing agent fines；

Flux fine mill, described flux fine mill has flux entrance and the outlet of flux fines；

Mixing arrangement, described mixing arrangement has zinc leaching residue fines entrance, reducing agent fines entrance, flux fines enter Mouth and mixed material outlet, described zinc leaching residue fines entrance is connected with the outlet of described zinc leaching residue, and described reducing agent fines enters Mouth is connected with the outlet of described reducing agent fines, and described flux fines entrance is connected with the outlet of described flux fines；

Shaped device, described shaped device has mixed material entrance and mixing pelletizing outlet, described mixed material entrance It is connected with the outlet of described mixed material；

Drying device, described drying device has mixing pelletizing entrance and pelletizing outlet is dried, described mixing pelletizing entrance It is connected with described mixing pelletizing outlet；

Revolving bed, described revolving bed have be dried pelletizing entrance, leaded zinc-silver flue dust outlet and iron content high-temperature roasting product Outlet, described be dried pelletizing entrance with described be dried pelletizing outlet be connected；

Granulating unit, described granulating unit has iron content high-temperature roasting product inlet and the outlet of water quenching material, and described iron content is high Warm product of roasting entrance is connected with described iron content high-temperature roasting product exit；

Ore grinding-magnetic separating unit, described ore grinding-magnetic separating unit has water quenching material entrance, metal iron powder outlet and mine tailing outlet.

Thus, the system of process zinc leaching residue according to embodiments of the present invention is passed through zinc leaching residue, reducing agent and is fluxed Agent is levigate in fine mill respectively, molding in mixing and shaped device in mixing arrangement, can significantly increase zinc leaching residue, also The former dose of contact area and flux three between, so that zinc leaching residue, reducing agent and flux three are fully contacted, carries The reaction rate of correlated response in high follow-up revolving bed, meanwhile, by zinc leaching residue is levigate, can significantly reduce follow-up rotation Reduction temperature in bed, thus reduce system energy consumption；Secondly mixing pelletizing obtained above is dried, can remove mixed Close pelletizing in moisture, dredging ball interior aperture, improve spheroid mechanical strength, then by gained be dried pelletizing supply to In revolving bed, there is pyrolytic reaction in reducing agent in revolving bed first, generates CO, H₂Deng reducibility gas, do not produce nitrogen oxidation , then there is reduction reaction in the dusty gass such as thing, and due to being anoxic condition in revolving bed, with the carrying out of reaction, CO is dense Degree improve constantly, such that it is able to remarkably promote the carrying out of reduction reaction, the lead zinc-silver wherein in zinc leaching residue with flue dust form from Revolving bed is recycled (lead, the response rate of zinc are more than 95%, and the response rate of silver is 90% about) after discharging, then will Obtained iron content high-temperature roasting product supplies successively can efficiently separate to granulating unit, ore grinding-concentration equipment and obtains gold Belong to iron powder (Iron grade of metal iron powder and the response rate are 90% about), thus having reclaimed the ferrum element in zinc leaching residue.Thus, Can realize the comprehensive reutilization of lead zinc-silver ferrum valuable metal element in zinc leaching residue using this system, process is simple simultaneously, Energy consumption is low.

In addition, the system processing zinc leaching residue according to the above embodiment of the present invention, can also have the skill added as follows Art feature：

In some embodiments of the invention, described shaped device is ball press or pelletizer.Thus, it is possible to significantly increase Contact area between zinc leaching residue, reducing agent and flux three is so that zinc leaching residue, reducing agent and flux three are abundant Contact, such that it is able to improve the reaction rate of correlated response in follow-up revolving bed.

In some embodiments of the invention, described ore grinding-magnetic separating unit includes being sequentially connected primary grinding device, one Stages of magnetic separation device, secondary grinding device and two-stage nitration concentration equipment.Thus, it is possible to significantly improve the response rate of metallic iron.

In some embodiments of the invention, described primary grinding device and described secondary grinding device are separately Rod mill or ball mill.Thus, it is possible to improve the response rate of metallic iron further.

In some embodiments of the invention, a described stages of magnetic separation device and described two-stage nitration concentration equipment are separately Magnetic separator or magnetic separation tube.Thus, it is possible to improve the response rate of metallic iron further.

In another aspect of the invention, the present invention proposes a kind of system using above-mentioned process zinc leaching residue and processes zinc The method of leached mud, according to embodiments of the invention, the method includes：

(1) zinc leaching residue is supplied and carry out levigate process to described zinc leaching residue fine mill, obtain zinc to leach Slag fines；

(2) reducing agent is supplied and carry out levigate process to described reducing agent fine mill, to obtain reducing agent fines；

(3) flux is supplied and carry out levigate process to described flux fine mill, to obtain flux fines；

(4) described zinc leaching residue fines, described reducing agent fines and described flux fines are supplied to described mixing dress Carry out mixed processing, to obtain mixed material in putting；

(5) described mixed material is supplied and carry out forming processes to described shaped device, to obtain mixing pelletizing；

(6) described mixing pelletizing is supplied and be dried process to described drying device, to obtain pelletizing is dried；

(7) by described pelletizing is dried and supplies carry out reduction treatment to described revolving bed to obtain leaded zinc-silver flue dust With iron content high-temperature roasting product；

(8) described iron content high-temperature roasting product is supplied and carry out Water Quenching to described granulating unit, to obtain water Quench material；

(9) described water quenching material is supplied and carry out ore grinding-magnetic separation process to described ore grinding-magnetic separating unit, to obtain gold Belong to iron powder and mine tailing.

Thus, the method for process zinc leaching residue according to embodiments of the present invention is passed through zinc leaching residue, reducing agent and is fluxed Agent is levigate in fine mill respectively, molding in mixing and shaped device in mixing arrangement, can significantly increase zinc leaching residue, also The former dose of contact area and flux three between, so that zinc leaching residue, reducing agent and flux three are fully contacted, carries The reaction rate of correlated response in high follow-up revolving bed, meanwhile, by zinc leaching residue is levigate, can significantly reduce follow-up rotation Reduction temperature in bed, thus reduce system energy consumption；Secondly mixing pelletizing obtained above is dried, can remove mixed Close pelletizing in moisture, dredging ball interior aperture, improve spheroid mechanical strength, then by gained be dried pelletizing supply to In revolving bed, there is pyrolytic reaction in reducing agent in revolving bed first, generates CO, H₂Deng reducibility gas, do not produce nitrogen oxidation , then there is reduction reaction in the dusty gass such as thing, and due to being anoxic condition in revolving bed, with the carrying out of reaction, CO is dense Degree improve constantly, such that it is able to remarkably promote the carrying out of reduction reaction, the lead zinc-silver wherein in zinc leaching residue with flue dust form from Revolving bed is recycled (lead, the response rate of zinc are more than 95%, and the response rate of silver is 90% about) after discharging, then will Obtained iron content high-temperature roasting product supplies successively can efficiently separate to granulating unit, ore grinding-concentration equipment and obtains gold Belong to iron powder (Iron grade of metal iron powder and the response rate are 90% about), thus having reclaimed the ferrum element in zinc leaching residue.Thus, Can realize the comprehensive reutilization of lead zinc-silver ferrum valuable metal element in zinc leaching residue using the method, process is simple simultaneously, Energy consumption is low.

In addition, the method processing zinc leaching residue according to the above embodiment of the present invention can also have the technology added as follows Feature：

In some embodiments of the invention, in step (2), described reducing agent be in brown coal and jet coal extremely Few one kind.Thus, it is possible to significantly improve the efficiency of reduction reaction in revolving bed, and economic and environment-friendly.

In some embodiments of the invention, in step (3), described flux is selected from quick lime, limestone, carbonic acid At least one in calcium and dolomite.Thus, advantageously reduce the energy consumption of revolving bed.

In some embodiments of the invention, described zinc leaching residue fines, described reducing agent fines and described flux are thin Separately not higher than 10 microns of the particle diameter of material.Thus, it is possible to significantly increase zinc leaching residue, reducing agent and flux three it Between contact area so that zinc leaching residue, reducing agent and flux three are fully contacted, such that it is able to improve in follow-up revolving bed The reaction rate of correlated response.

In some embodiments of the invention, in step (4), by described zinc leaching residue fines, described reducing agent fines With described flux fines according to mass ratio be (70～90)：(10～15)：(5～10) are mixed.Thus, it is possible to significantly carry The response rate of lead zinc-silver ferrum in high zinc leaching residue.

In some embodiments of the invention, in step (7), the temperature of described reduction treatment is Celsius for 900～1050 Degree, the time is 30～40 minutes.Thus, it is possible to improve the reaction rate of reduction reaction in revolving bed further, improve has simultaneously The response rate of the elements such as valency metallic lead, zinc, silver and ferrum.

In some embodiments of the invention, step (9) is carried out according to the following step：(9-1) described water quenching material is supplied Carry out primary grinding process to primary grinding device, to obtain primary grinding material；(9-2) described primary grinding material is supplied Carry out a stages of magnetic separation process to a stages of magnetic separation device, to obtain one section of metal iron powder and described mine tailing；(9-3) by described one Section metal iron powder supplies and carries out secondary grinding process to secondary grinding device, to obtain secondary grinding material；(9-4) will be described Secondary grinding material supplies and carries out two stages of magnetic separation process to two-stage nitration concentration equipment, to obtain described metal iron powder and described tail Ore deposit, thus, it is possible to significantly improve the response rate of metallic iron.

In some embodiments of the invention, in step (9-1), in described primary grinding material, particle diameter is not higher than 0.074mm accounts for 70～80%.Thus, it is possible to improve the response rate of metallic iron further.

In some embodiments of the invention, in step (9-2), the magnetic field intensity that a described stages of magnetic separation is processed is 1600 ～1800Oe.Thus, it is possible to improve the response rate of metallic iron further.

In some embodiments of the invention, in step (9-3), in described secondary grinding material, particle diameter is not higher than 0.074mm accounts for 80～90%.Thus, it is possible to improve the response rate of metallic iron further.

In some embodiments of the invention, in step (9-4), the magnetic field intensity that described two stages of magnetic separation are processed is 800 ～1200Oe.Thus, it is possible to improve the response rate of metallic iron further.

The additional aspect of the present invention and advantage will be set forth in part in the description, and partly will become from the following description Obtain substantially, or recognized by the practice of the present invention.

Brief description

The above-mentioned and/or additional aspect of the present invention and advantage will become from reference to the description to embodiment for the accompanying drawings below Substantially and easy to understand, wherein：

Fig. 1 is the system structure diagram processing zinc leaching residue according to an embodiment of the invention；

Fig. 2 is the system structure diagram of the process zinc leaching residue according to further embodiment of the present invention；

Fig. 3 is the method flow schematic diagram processing zinc leaching residue according to an embodiment of the invention；

Fig. 4 is the method flow schematic diagram of the process zinc leaching residue according to further embodiment of the present invention；

Fig. 5 is the system structure diagram of the process zinc leaching residue according to another embodiment of the present invention；

Fig. 6 is the system structure diagram of the process zinc leaching residue of comparative example 1-3.

Specific embodiment

Embodiments of the invention are described below in detail, the example of described embodiment is shown in the drawings, wherein from start to finish The element that same or similar label represents same or similar element or has same or like function.Below with reference to attached The embodiment of figure description is exemplary it is intended to be used for explaining the present invention, and is not considered as limiting the invention.

In the present invention, unless otherwise clearly defined and limited, term " installation ", " being connected ", " connection ", " fixation " etc. Term should be interpreted broadly, for example, it may be being fixedly connected or being detachably connected or integral；Can be that machinery connects Connect or electrically connect；Can be to be joined directly together it is also possible to be indirectly connected to by intermediary, can be in two elements The connection in portion or the interaction relationship of two elements, limit unless otherwise clear and definite.For those of ordinary skill in the art For, above-mentioned term concrete meaning in the present invention can be understood as the case may be.

In one aspect of the invention, the present invention proposes a kind of system processing zinc leaching residue.Reality according to the present invention Apply example, with reference to Fig. 1, this system includes：Zinc leaching residue fine mill 100, reducing agent fine mill 200, flux fine mill 300th, mixing arrangement 400, shaped device 500, drying device 600, revolving bed 700, granulating unit 800 and ore grinding-magnetic separating unit 900.

According to embodiments of the invention, zinc leaching residue fine mill 100 has zinc leaching residue entrance 101 and zinc leaching residue is thin Material outlet 102, and be suitable to for zinc leaching residue to carry out levigate process, to obtain zinc leaching residue fines.Thus, it is possible to significantly increase Contact area between zinc leaching residue, reducing agent and flux three in subsequent process so that zinc leaching residue, reducing agent and Flux three be fully contacted, and improves the reaction rate of correlated response in follow-up revolving bed, passes through zinc leaching residue is levigate simultaneously, The reduction temperature in follow-up revolving bed can be significantly reduced, thus reducing system energy consumption.

According to one embodiment of present invention, the particle diameter of zinc leaching residue fines is not particularly restricted, people in the art Member can be selected according to actual needs, and according to a specific embodiment of the present invention, the particle diameter of zinc leaching residue fines is permissible Not higher than 10 microns.Thus, the reaction rate during sequential reduction not only can be significantly improved, and system energy can be reduced Consumption.

According to embodiments of the invention, reducing agent fine mill 200 has reducing agent entrance 201 and the outlet of reducing agent fines 202, and be suitable to for reducing agent to carry out levigate process, to obtain reducing agent fines.Thus, it is possible to increase subsequent process further The contact area of middle zinc leaching residue, reducing agent and flux three, improves the reaction rate of correlated response in follow-up revolving bed.

According to one embodiment of present invention, the particular type of reducing agent is not particularly restricted, those skilled in the art Can be selected according to actual needs, according to a specific embodiment of the present invention, reducing agent can be selected from brown coal and length At least one in flame coal.Inventor finds, can be substantially better than other types using such reducing agent and improve in revolving bed also The efficiency of former reaction, and economic and environment-friendly.

According to still a further embodiment, the particle diameter of reducing agent fines is not particularly restricted, people in the art Member can be selected according to actual needs, and according to a specific embodiment of the present invention, the particle diameter of reducing agent fines can not Higher than 10 microns.Thus, it is possible to improve the reaction rate during sequential reduction further.

According to embodiments of the invention, flux fine mill 300 has flux entrance 301 and the outlet of flux fines 302, and be suitable to for flux to carry out levigate process, to obtain flux fines.Thus, it is possible to increase subsequent process further The contact area of middle zinc leaching residue, reducing agent and flux three, improves the reaction rate of correlated response in follow-up revolving bed.

According to one embodiment of present invention, the particular type of flux is not particularly restricted, those skilled in the art Can be selected according to actual needs, according to a specific embodiment of the present invention, flux can be selected from quick lime, stone At least one in lime stone, Calcium Carbonate and dolomite.Inventor finds, can be significantly better than other types using such flux Reduce the energy consumption in revolving bed.

According to still a further embodiment, the particle diameter of flux fines is not particularly restricted, people in the art Member can be selected according to actual needs, and according to a specific embodiment of the present invention, the particle diameter of flux fines can be Not higher than 10 microns.Thus, it is possible to further improve sequential reduction during reaction rate and system energy is greatly lowered Consumption.

According to embodiments of the invention, mixing arrangement 400 has zinc leaching residue fines entrance 401, reducing agent fines entrance 402nd, flux fines entrance 403 and mixed material outlet 404, zinc leaching residue fines entrance 401 and the outlet of zinc leaching residue fines 102 are connected, and reducing agent fines entrance 402 is connected with reducing agent fines outlet 202, and flux fines entrance 403 is thin with flux Material outlet 302 is connected, and is suitable to for zinc leaching residue fines, reducing agent fines and flux fines to carry out mixed processing, so that To mixed material.Thus, it is possible to significantly increase contact area between zinc leaching residue, reducing agent and flux three so that zinc Leached mud, reducing agent and flux three are fully contacted, such that it is able to improve the reaction rate of correlated response in follow-up revolving bed.

According to one embodiment of present invention, the mixed proportion of zinc leaching residue fines, reducing agent fines and flux fines It is not particularly restricted, those skilled in the art can be selected according to actual needs, according to the present invention is specifically real Apply example, zinc leaching residue fines, reducing agent fines and flux fines can be (70～90) according to mass ratio：(10～15)：(5 ～10) mixed.Inventor finds, when the mass ratio of reducing agent fines and zinc leaching residue fines is too high, can cause to reduce The waste of agent fines；And when the mass ratio of reducing agent fines and zinc leaching residue fines is too low, then can cause zinc leaching residue fines Reduction is not thorough, thus reducing the comprehensive reutilization rate of valuable metal element；And flux fines and zinc leaching residue fines The too high too low comprehensive reutilization rate that all can reduce valuable metal element of mass ratio, specifically：When flux fines is soaked with zinc Slag tap fines mass ratio too high when, whole reaction can be led in revolving bed excessively violent, pellets, be unfavorable for discharging； And when the mass ratio of flux fines and zinc leaching residue fines is too low, then can lead to flux can not effectively facilitate react into OK.

According to embodiments of the invention, shaped device 500 has mixed material entrance 501 and mixing pelletizing outlet 502, mixes Close material inlet 501 to be connected with mixed material outlet 404, and be suitable to for mixed material to carry out forming processes, to be mixed Pelletizing.Thus, it is possible to increase contact area between zinc leaching residue, reducing agent and flux three so that zinc leaching residue, reduction Agent and flux three are fully contacted, such that it is able to improve the reaction rate of correlated response in follow-up revolving bed.Specifically, molding Device can be ball press or pelletizer.It should be noted that those skilled in the art can be according to actual needs to mixing ball The particle diameter of group is selected.

According to embodiments of the invention, drying device 600 has mixing pelletizing entrance 601 and pelletizing outlet 602 is dried, and mixes Close pelletizing entrance 601 to be connected with mixing pelletizing outlet 502, and be suitable to mixing pelletizing is dried process, to obtain drying Pelletizing.Thus, it is possible to remove the moisture in mixing pelletizing, the aperture of dredging ball interior, improve the mechanical strength of spheroid.

According to embodiments of the invention, revolving bed 700 have be dried pelletizing entrance 701, leaded zinc-silver flue dust export 702 and Iron content high-temperature roasting product exit 703, pelletizing entrance 701 is dried, and outlet 602 is connected with pelletizing is dried, and is suitable to pelletizing will be dried Carry out reduction treatment, to obtain leaded zinc-silver flue dust and iron content high-temperature roasting product.Specifically, in revolving bed, material is equal Even be distributed on rotating material bed, material bed with furnace bottom machine rotate, furnace wall is installed multiple regenerative radiant tube burners, burner exists Radiation combustion inner pipe, radiates tube wall radiant heating material up and down by siege, is conducive to the material in revolving bed to be heated evenly, Thus increasing reaction rate, and end part of radiant tube is used for recovered flue gas sensible heat equipped with heat storage, and the heat being reclaimed can be used for Warm-up combustion-supporting air and low-calorie fuel gas, thus, can significantly reduce revolving bed energy consumption, adopt heat accumulation type radiant tube spoke simultaneously Penetrate heating, the utilization ratio of reducing agent can be improved, thus reducing the consumption of reducing agent, cost-effective, and reducing agent is in rotation There is pyrolytic reaction in rotated bed first, generate CO, H₂Deng material, do not produce the dusty gass such as nitrogen oxides, then reduce Reaction, due to being anoxic condition in revolving bed, with the carrying out of reaction, CO concentration improves constantly, and promotes entering of reduction reaction OK, such that it is able to realize the efficient utilization of reducing agent, (lead, the response rate of zinc are more than 95%, silver to obtain leaded zinc-silver flue dust The response rate is 90% about) and iron content high-temperature roasting product.

According to one embodiment of present invention, the condition of reduction treatment is not particularly restricted, and those skilled in the art can To be selected according to actual needs, according to a specific embodiment of the present invention, the temperature of reduction treatment can for 900～ 1050 degrees Celsius, the time can be 30～40 minutes.Inventor finds, can be significantly better than other using this reduction treatment condition Improve the response rate of lead zinc-silver ferrum in zinc leaching residue.

According to embodiments of the invention, granulating unit 800 has iron content high-temperature roasting product inlet 801 and the outlet of water quenching material 802, iron content high-temperature roasting product inlet 801 is connected with iron content high-temperature roasting product exit 703, and is suitable to iron content high-temperature roasting Product carries out Water Quenching, to obtain water quenching material.Thus, it is possible to significantly improve the grinding efficiency in subsequent process.

According to embodiments of the invention, ore grinding-magnetic separating unit 900 has water quenching material entrance 901, metal iron powder outlet 902 Export 903 with mine tailing, water quenching material entrance 901 is connected with water quenching material outlet 802, and is suitable to carry out water quenching material at ore grinding-magnetic separation Reason, to obtain metal iron powder and mine tailing.Thus, it is possible to realize the recycling of ferrum element in zinc leaching residue, and gained gold Belonging to the Iron grade of iron powder and the response rate is 90% about.

According to one embodiment of present invention, with reference to Fig. 2, ore grinding-magnetic separating unit 900 can include a section being sequentially connected Ore grinding device 91, a stages of magnetic separation device 92, secondary grinding device 93 and two-stage nitration concentration equipment 94.

According to one embodiment of present invention, water quenching material entrance 901 is arranged on primary grinding device 91, and one section of mill Ore deposit device 91 is additionally provided with primary grinding material outlet 911, primary grinding device 91 is suitable to carry out water quenching material at primary grinding Reason, to obtain primary grinding material.Thus, it is possible to significantly improve the response rate of ferrum element in zinc leaching residue.

According to one embodiment of present invention, the particle diameter of primary grinding material is not particularly restricted, those skilled in the art Can be selected according to actual needs.According to a specific embodiment of the present invention, in primary grinding material, particle diameter is not higher than 0.074mm can account for 70～80%.Inventor finds, in primary grinding material, the accounting of particle diameter not higher than 0.074mm is crossed and exceeded The response rate of ferrum element in zinc leaching residue all can be reduced when low.Specifically：When in primary grinding material, particle diameter is not higher than 0.074mm's It is impossible to realize the monomer dissociation of mineral when accounting is too low, and too high then waste energy, and mineral granularity is meticulous is unfavorable for follow-up magnetic Choosing is processed.

According to another specific embodiment of the present invention, a stages of magnetic separation device 92 can be provided with primary grinding material entrance 921st, one section of metal iron powder outlet 922 and mine tailing outlet 903, primary grinding material entrance 921 exports 911 phases with primary grinding material Even, the primary grinding material that a stages of magnetic separation device 92 is suitable to obtain above-mentioned primary grinding device 91 carries out a stages of magnetic separation process, with Just one section of metal iron powder and mine tailing are obtained.Thus, it is possible to improve the recovery utilization rate of ferrum element in zinc leaching residue further.

According to one embodiment of present invention, the condition that a stages of magnetic separation is processed is not particularly restricted, people in the art Member can be selected according to actual needs.The magnetic field intensity being processed according to a specific embodiment of the present invention, a stages of magnetic separation Can be 1600～1800Oe.Inventor finds, the magnetic field intensity that a stages of magnetic separation is processed is too high to lead to one section of metallic iron of gained Grade powder is relatively low, too low, is unable to one section of metal iron powder of efficient recovery, thus affecting the recovery utilization rate of ferrum element.

According to another specific embodiment of the present invention, secondary grinding device 93 can be provided with one section of metal iron powder and enter Mouth 931 and secondary grinding material outlet 932, one section of metal iron powder entrance 931 exports 922 with one section of sulfur-bearing metal iron powder and is connected, and It is suitable to the one section of metal iron powder obtaining in a stages of magnetic separation device be carried out secondary grinding process, to obtain secondary grinding material.By This, can improve the recovery utilization rate of ferrum element in zinc leaching residue further.

According to one embodiment of present invention, the particle diameter of secondary grinding material is not particularly restricted, those skilled in the art Can be selected according to actual needs.According to a specific embodiment of the present invention, in secondary grinding material, particle diameter is not higher than 0.074mm accounts for 80～90%.Inventor finds, when in secondary grinding material, the accounting of particle diameter not higher than 0.074mm is too high too low The response rate of ferrum element in zinc leaching residue all can be reduced.Specifically：When in secondary grinding material, particle diameter is not higher than the accounting of 0.074mm It is impossible to realize the monomer dissociation of mineral when too low, and too high then waste energy, and mineral granularity is meticulous is unfavorable at follow-up magnetic separation Reason.

According to another specific embodiment of the present invention, metal iron powder outlet 902 and mine tailing outlet 903 can be arranged on two On stages of magnetic separation device 94, and secondary grinding material entrance 941 can be provided with two-stage nitration concentration equipment 94, secondary grinding material entrance 941 are connected with secondary grinding material outlet 932, and are suitable to for the secondary grinding material obtaining in above-mentioned secondary grinding device to carry out two-stage nitration Magnetic separation is processed, to obtain metal iron powder and mine tailing.Thus, it is possible to improve the recycling of ferrum element in zinc leaching residue further Rate.

According to still another embodiment of the invention, the condition that two stages of magnetic separation are processed is not particularly restricted, art technology Personnel can be selected according to actual needs.According to a specific embodiment of the present invention, the magnetic field that two stages of magnetic separation are processed is strong Degree can be 800～1200Oe.Inventor finds, the magnetic field intensity that two stages of magnetic separation are processed is too high to lead to gained metal iron powder product Position is relatively low, too low, is unable to efficient recovery metal iron powder, thus affecting the recovery utilization rate of ferrum element.In an experiment, inventor Find that the purpose that a stages of magnetic separation is processed is the ferrum element reclaiming as far as possible in metallized pellet, and the purpose that two stages of magnetic separation are processed is Obtain the higher concentrate of Iron grade, thus, inventor has been surprisingly found that through many experiments, the magnetic field intensity processing when two stages of magnetic separation The recovery utilization rate of ferrum element can be effectively improved during the magnetic field intensity processing less than a stages of magnetic separation.

According to still a further embodiment, the particular type of primary grinding device 91 and secondary grinding device 93 is not It is particularly limited, those skilled in the art can be selected according to actual needs.According to a specific embodiment of the present invention, Primary grinding device 91 and secondary grinding device 93 can be separately rod mill or ball mill.Thus, it is possible to further Improve the recovery utilization rate of ferrum element in zinc leaching residue.

According to still another embodiment of the invention, the particular type of a stages of magnetic separation device 92 and two-stage nitration concentration equipment 94 is not It is particularly limited, those skilled in the art can be selected according to actual needs.According to a specific embodiment of the present invention, One stages of magnetic separation device 92 and two-stage nitration concentration equipment 94 can be separately magnetic separator or magnetic separation tube.Thus, it is possible to further Improve the recovery utilization rate of ferrum element in zinc leaching residue.

The system of process zinc leaching residue according to embodiments of the present invention is passed through by zinc leaching residue, reducing agent and flux respectively Molding in mixing and shaped device in levigate in fine mill, mixing arrangement, can significantly increase zinc leaching residue, reducing agent and Contact area between flux three, so that zinc leaching residue, reducing agent and flux three are fully contacted, improves follow-up The reaction rate of correlated response in revolving bed, by zinc leaching residue is levigate, can significantly reduce in follow-up revolving bed meanwhile Reduction temperature, thus reduce system energy consumption；Secondly mixing pelletizing obtained above is dried, mixing pelletizing can be removed In moisture, dredging ball interior aperture, improve spheroid mechanical strength, then gained is dried pelletizing and supplies to revolving bed In, there is pyrolytic reaction in reducing agent in revolving bed, generate CO, H first₂Deng reducibility gas, do not produce the dirts such as nitrogen oxides , then there is reduction reaction in dye gas, and due to being anoxic condition in revolving bed, with the carrying out of reaction, CO concentration is continuous Improve, such that it is able to remarkably promote the carrying out of reduction reaction, the lead zinc-silver wherein in zinc leaching residue is with flue dust form from revolving bed (lead, the response rate of zinc are more than 95%, and the response rate of silver is 90% about) is recycled after discharge, then will be obtained Iron content high-temperature roasting product supply successively can efficiently separate to granulating unit, ore grinding-concentration equipment and obtain metal iron powder (Iron grade of metal iron powder and the response rate are 90% about), thus reclaimed the ferrum element in zinc leaching residue.Thus, using this System can realize the comprehensive reutilization of lead zinc-silver ferrum valuable metal element in zinc leaching residue, process is simple simultaneously, and energy consumption is low.

As described above, the system of process zinc leaching residue according to embodiments of the present invention can have the advantages that selected from following at least One of：

The system of process zinc leaching residue according to embodiments of the present invention can be used for the waste residues of volatile matter such as multiple leaded, zinc, Metallurgical dust sludge etc., applied range；

The system of process zinc leaching residue according to embodiments of the present invention utilizes revolving bed-mill ore magnetic selection flow processing zinc to leach Slag, by zinc leaching residue is levigate, reduces reduction temperature it is achieved that the synthetical recovery of ferrum, lead, zinc and silver；

The system of process zinc leaching residue according to embodiments of the present invention adopts heat accumulation type radiant tube mode of heating, improves coal Utilization ratio reduce coal consumption, cost-effective, be prevented effectively from simultaneously burner blocking；

The processing procedure process is simple of the system of process zinc leaching residue according to embodiments of the present invention it is easy to operation it is easy to Large-scale production, effectively achieves the recycling of valuable metal element resource.

In another aspect of the invention, the present invention proposes a kind of system using above-mentioned process zinc leaching residue and processes zinc The method of leached mud.According to embodiments of the invention, with reference to Fig. 3, the method includes：

S100：Zinc leaching residue is supplied to zinc leaching residue fine mill, carries out levigate process

In this step, zinc leaching residue is supplied to zinc leaching residue fine mill, carries out levigate process, to obtain zinc leaching Slag tap fines.Thus, it is possible to significantly increase the contact surface between zinc leaching residue in subsequent process, reducing agent and flux three Long-pending, so that zinc leaching residue, reducing agent and flux three are fully contacted, improve the reaction of correlated response in follow-up revolving bed Speed, passing through zinc leaching residue is levigate simultaneously, can significantly reducing the reduction temperature in follow-up revolving bed, thus reducing system Energy consumption.

S200：Reducing agent is supplied to reducing agent fine mill, carries out levigate process

In this step, reducing agent is supplied to reducing agent fine mill, carries out levigate process, so that it is thin to obtain reducing agent Material.Thus, it is possible to increase the contact area of zinc leaching residue, reducing agent and flux three in subsequent process further, after raising The reaction rate of correlated response in continuous revolving bed.

S300：Flux is supplied to flux fine mill, carries out levigate process

In this step, flux is supplied to flux fine mill, carries out levigate process, so that it is thin to obtain flux Material.Thus, it is possible to increase the contact area of zinc leaching residue, reducing agent and flux three in subsequent process further, after raising The reaction rate of correlated response in continuous revolving bed.

According to still a further embodiment, the particle diameter of flux fines is not particularly restricted, people in the art Member can be selected according to actual needs, and according to a specific embodiment of the present invention, the particle diameter of flux fines can be Not higher than 10 microns.Thus, it is possible to further improve sequential reduction during reaction rate and system energy is greatly lowered Consumption.S400：Zinc leaching residue fines, reducing agent fines and flux fines are supplied and carries out mixed processing to mixing arrangement

In this step, zinc leaching residue fines, reducing agent fines and flux fines are supplied and is mixed to mixing arrangement Conjunction is processed, to obtain mixed material.Thus, it is possible to significantly increase connecing between zinc leaching residue, reducing agent and flux three Contacting surface is amassed so that zinc leaching residue, reducing agent and flux three are fully contacted, related anti-in follow-up revolving bed such that it is able to improve The reaction rate answered.

According to one embodiment of present invention, the mixed proportion of zinc leaching residue fines, reducing agent fines and flux fines It is not particularly restricted, those skilled in the art can be selected according to actual needs, according to the present invention is specifically real Apply example, zinc leaching residue fines, reducing agent fines and flux fines can be (70～90) according to mass ratio：(10～15)：(5 ～10) mixed.Inventor finds, when the mass ratio of reducing agent fines and zinc leaching residue fines is too high, can cause to reduce The waste of agent fines；And when the mass ratio of reducing agent fines and zinc leaching residue fines is too low, then can cause zinc leaching residue fines Reduction is not thorough, thus reducing the comprehensive reutilization rate of valuable metal element.And flux fines and zinc leaching residue fines The too high too low comprehensive reutilization rate that all can reduce valuable metal element of mass ratio, specifically：When flux fines is soaked with zinc Slag tap fines mass ratio too high when, whole reaction can be led in revolving bed excessively violent, pellets, be unfavorable for discharging； And when the mass ratio of flux fines and zinc leaching residue fines is too low, then can lead to flux can not effectively facilitate react into OK.

S500：Mixed material is supplied and carries out forming processes to shaped device

In this step, mixed material is supplied to shaped device, carries out forming processes, to obtain mixing pelletizing.By This, can increase the contact area between zinc leaching residue, reducing agent and flux three so that zinc leaching residue, reducing agent and help Flux three be fully contacted, such that it is able to improve the reaction rate of correlated response in follow-up revolving bed.Specifically, shaped device can Think ball press or pelletizer.It should be noted that those skilled in the art can be according to actual needs to the grain mixing pelletizing Footpath is selected.

S600：Mixing pelletizing is supplied to drying device, is dried process

In this step, mixing pelletizing is supplied to drying device, is dried process, to obtain pelletizing is dried.By This, can remove the moisture in mixing pelletizing, the aperture of dredging ball interior, improve the mechanical strength of spheroid.

S700：Carry out reduction treatment by pelletizing being dried and supplying to revolving bed

In this step, carry out reduction treatment by pelletizing being dried and supplying to revolving bed, so as to obtain leaded zinc-silver flue dust and Iron content high-temperature roasting product.Specifically, in revolving bed, material is evenly distributed on rotating material bed, and material bed rotates with furnace bottom machine, Multiple regenerative radiant tube burners are installed on furnace wall, burner, in radiation combustion inner pipe, radiates tube wall up and down by siege Radiant heating material, is conducive to the material in revolving bed to be heated evenly, thus increasing reaction rate, and end part of radiant tube equipped with Heat storage is used for recovered flue gas sensible heat, and the heat being reclaimed can be used for warm-up combustion-supporting air and low-calorie fuel gas, thus, can Significantly reduce revolving bed energy consumption, adopting heat accumulation type radiant tube radiant heating simultaneously, the utilization ratio of reducing agent being improved, thus dropping The low consumption of reducing agent, cost-effective, and there is pyrolytic reaction in reducing agent in revolving bed, generate CO, H first₂Deng thing Matter, does not produce the dusty gass such as nitrogen oxides, and then reduction reaction occurs, due to being anoxic condition in revolving bed, with reaction Carrying out, CO concentration improve constantly, promote the carrying out of reduction reaction, such that it is able to realize the efficient utilization of reducing agent, obtain Leaded zinc-silver flue dust (lead, the response rate of zinc are more than 95%, and the response rate of silver is 90% about) and iron content high-temperature roasting product.

S800：Iron content high-temperature roasting product is supplied and carries out Water Quenching to granulating unit

In this step, iron content high-temperature roasting product is supplied to granulating unit, carries out Water Quenching, to obtain water quenching Material.Thus, it is possible to significantly improve the grinding efficiency in subsequent process.

S900：Water quenching material is supplied and carries out ore grinding-magnetic separation process to ore grinding-magnetic separating unit

In this step, water quenching material is supplied and carries out ore grinding-magnetic separation process to ore grinding-magnetic separating unit, to obtain metal Iron powder and mine tailing.Thus, it is possible to realize the recycling of ferrum element in zinc leaching residue, and the Iron grade of gained metal iron powder and The response rate is 90% about.

According to one embodiment of present invention, with reference to Fig. 4, step S900 can be carried out according to the following step：

S910：Water quenching material is supplied to primary grinding device, carries out primary grinding process

In this step, water quenching material is supplied to primary grinding device, carries out primary grinding process, to obtain one section of mill Mineral aggregate.Thus, it is possible to significantly improve the response rate of ferrum element in zinc leaching residue.

S920：Primary grinding material is supplied to a stages of magnetic separation device, carries out a stages of magnetic separation process

In this step, primary grinding material is supplied to a stages of magnetic separation device, carries out a stages of magnetic separation process, to obtain one Section metal iron powder and mine tailing.Thus, it is possible to improve the recovery utilization rate of ferrum element in zinc leaching residue further.

S930：One section of metal iron powder is supplied to secondary grinding device, carries out secondary grinding process

In this step, one section of metal iron powder is supplied to secondary grinding device, carries out secondary grinding process, to obtain Secondary grinding material.Thus, it is possible to improve the recovery utilization rate of ferrum element in zinc leaching residue further.

S940：Secondary grinding material is supplied and carries out two stages of magnetic separation process to two-stage nitration concentration equipment

In this step, secondary grinding material is supplied to two-stage nitration concentration equipment, carries out two stages of magnetic separation process, to obtain gold Belong to iron powder and mine tailing.Thus, it is possible to improve the recovery utilization rate of ferrum element in zinc leaching residue further.

According to still a further embodiment, the particular type of primary grinding device and secondary grinding device is not subject to spy Do not limit, those skilled in the art can be selected according to actual needs.According to a specific embodiment of the present invention, one section Ore grinding device and secondary grinding device can be separately rod mill or ball mill.Thus, it is possible to improve zinc leaching further Slag tap the recovery utilization rate of middle ferrum element.

According to still another embodiment of the invention, the particular type of a stages of magnetic separation device and two-stage nitration concentration equipment is not subject to spy Do not limit, those skilled in the art can be selected according to actual needs.According to a specific embodiment of the present invention, one section Concentration equipment and two-stage nitration concentration equipment can be separately magnetic separator or magnetic separation tube.Thus, it is possible to improve zinc leaching further Slag tap the recovery utilization rate of middle ferrum element.

The method of process zinc leaching residue according to embodiments of the present invention is passed through by zinc leaching residue, reducing agent and flux respectively Molding in mixing and shaped device in levigate in fine mill, mixing arrangement, can significantly increase zinc leaching residue, reducing agent and Contact area between flux three, so that zinc leaching residue, reducing agent and flux three are fully contacted, improves follow-up The reaction rate of correlated response in revolving bed, by zinc leaching residue is levigate, can significantly reduce in follow-up revolving bed meanwhile Reduction temperature, thus reduce system energy consumption；Secondly mixing pelletizing obtained above is dried, mixing pelletizing can be removed In moisture, dredging ball interior aperture, improve spheroid mechanical strength, then gained is dried pelletizing and supplies to revolving bed In, there is pyrolytic reaction in reducing agent in revolving bed, generate CO, H first₂Deng reducibility gas, do not produce the dirts such as nitrogen oxides , then there is reduction reaction in dye gas, and due to being anoxic condition in revolving bed, with the carrying out of reaction, CO concentration is continuous Improve, such that it is able to remarkably promote the carrying out of reduction reaction, the lead zinc-silver wherein in zinc leaching residue is with flue dust form from revolving bed (lead, the response rate of zinc are more than 95%, and the response rate of silver is 90% about) is recycled after discharge, then will be obtained Iron content high-temperature roasting product supply successively can efficiently separate to granulating unit, ore grinding-concentration equipment and obtain metal iron powder (Iron grade of metal iron powder and the response rate are 90% about), thus reclaimed the ferrum element in zinc leaching residue.Thus, using this Method can realize the comprehensive reutilization of lead zinc-silver ferrum valuable metal element in zinc leaching residue, process is simple simultaneously, and energy consumption is low.

Below with reference to specific embodiment, present invention is described, it should be noted that these embodiments are only to describe Property, and limit the present invention never in any form.

Embodiment 1

The consisting of of zinc leaching residue：Full weight of iron fraction is 20.12wt%, and Zn mass fraction is 14.87wt%, Pb mass Fraction is 3.34wt%, and Ag mass fraction is 0.012wt%；Brown coal selected by reducing agent, and constituent is：Fixed carbon 31.28wt%, volatile matters 27.13wt%, ash 12.6wt%；Limestone selected by flux.With reference to Fig. 5, follow these steps to into Row is processed：

(1) above-mentioned zinc leaching residue is supplied and carry out levigate process to zinc leaching residue fine mill, obtain zinc leaching residue thin Material, not higher than 10 microns of the particle diameter of zinc leaching residue fines；

(2) above-mentioned brown coal are supplied and carry out levigate process to reducing agent fine mill, obtain brown coal fines, brown coal fines Not higher than 10 microns of particle diameter；

(3) above-mentioned limestone is supplied and carry out levigate process to flux fine mill, obtain limestone fines, Calx Not higher than 10 microns of the particle diameter of stone fines；

(4) above-mentioned zinc leaching residue fines, brown coal fines and limestone fines are supplied to mixing arrangement according to mass ratio 80：12：8 ratio mixing carries out mixed processing, obtains mixed material；

(5) said mixture material is supplied and carry out forming processes to shaped device, obtain mixing pelletizing；

(6) above-mentioned mixing pelletizing is supplied and be dried process to drying device, obtain pelletizing is dried；

(7) by above-mentioned pelletizing is dried and supplies carry out reduction treatment to revolving bed, the temperature of reduction treatment is 900～1050 Degree Celsius, reduce 30～40 minutes, you can reclaiming lead, zinc, silver etc. in the leaded zinc-silver flue dust from revolving bed top duct has Valency metal, discharges iron content high-temperature roasting product from revolving bed after end to be restored, is analyzed through the composition to flue dust, lead, Zinc, the silver-colored response rate are all more than 95%；

(8) above-mentioned iron content high-temperature roasting product is supplied and carry out Water Quenching to granulating unit, obtain water quenching material；

(9) above-mentioned water quenching material is supplied and carry out primary grinding process to primary grinding device, obtain primary grinding material, one In section ore grinding material, particle diameter not higher than 0.074mm's accounts for 70～80%；Then above-mentioned primary grinding material is supplied and fill to a stages of magnetic separation Carrying out a stages of magnetic separation process in putting, obtain one section of metal iron powder and mine tailing, the magnetic field intensity that a stages of magnetic separation is processed is 1600～ 1800Oe；Then above-mentioned one section of metal iron powder is supplied and carry out secondary grinding process to secondary grinding device, obtain two-stage nitration mill Mineral aggregate, in secondary grinding material, particle diameter not higher than 0.074mm's accounts for 80～90%；Finally above-mentioned secondary grinding material is supplied to two-stage nitration Carrying out two stages of magnetic separation process in concentration equipment, obtain metal iron powder and mine tailing, the magnetic field intensity that two stages of magnetic separation are processed is 800～ 1200Oe, obtains metal iron powder and mine tailing, the Iron grade of the metal iron powder of gained and the response rate are 90% about.

Embodiment 2

The consisting of of zinc leaching residue：Full weight of iron fraction is 21.58wt%, and Zn mass fraction is 15.64wt%, Pb mass Fraction is 3.85wt%, and Ag mass fraction is 0.015wt%；Jet coal selected by reducing agent, and constituent is：Fixed carbon 47.38wt%, volatile matters 44.60wt%, ash 4.39wt%；Quick lime selected by flux.With reference to Fig. 5, follow these steps to into Row is processed：

(2) above-mentioned jet coal is supplied and carry out levigate process to reducing agent fine mill, obtain jet coal fines, long flame Not higher than 10 microns of the particle diameter of coal fines；

(3) above-mentioned quick lime is supplied and carry out levigate process to flux fine mill, obtain quick lime fines, calculogenesis Not higher than 10 microns of the particle diameter of grey fines；

(4) above-mentioned zinc leaching residue fines, jet coal fines and quick lime fines are supplied to mixing arrangement according to quality Ratio 83：11：6 ratio mixing carries out mixed processing, obtains mixed material；

Embodiment 3

The consisting of of zinc leaching residue：Full weight of iron fraction is 22.72wt%, and Zn is 16.87wt%, and Pb is 4.13wt%, Ag is 0.016wt%；Semi-coke selected by reducing agent, and constituent is：Fixed carbon 85wt%, ash 10wt%；Stone selected by flux Lime stone.With reference to Fig. 3, it follow these steps to be processed：

1) above-mentioned zinc leaching residue is supplied and carry out levigate process to zinc leaching residue fine mill, obtain zinc leaching residue thin Material, not higher than 10 microns of the particle diameter of zinc leaching residue fines；

(2) above-mentioned semi-coke is supplied and carry out levigate process to reducing agent fine mill, obtain semi-coke fines, semi-coke fines Not higher than 10 microns of particle diameter；

(4) above-mentioned zinc leaching residue fines, semi-coke fines and limestone fines are supplied to mixing arrangement according to mass ratio 82：14：4 ratio mixing carries out mixed processing, obtains mixed material；

Comparative example 1

The consisting of of zinc leaching residue：Full weight of iron fraction is 20.12wt%, and Zn mass fraction is 14.87wt%, Pb mass Fraction is 3.34wt%, and Ag is 0.012wt%；Brown coal selected by reducing agent, and constituent is：Fixed carbon 31.28wt%, volatile matters 27.13wt%, ash 12.6wt%；Limestone selected by flux.With reference to Fig. 6, it follow these steps to be processed：

(1) above-mentioned zinc leaching residue is supplied and carry out break process to zinc leaching residue breaker, obtain zinc leaching residue and break Particle, the particle diameter of zinc leaching residue broken material is not higher than 1mm；

(2) above-mentioned brown coal are supplied and carry out break process to reducing agent breaker, obtain brown coal crushing material, brown coal break The particle diameter of particle is not higher than 1mm；

(3) above-mentioned limestone is supplied and carry out break process to flux breaker, obtain limestone crushing material, stone The particle diameter of lime stone broken material is not higher than 1mm；

(4) by above-mentioned zinc leaching residue broken material, brown coal crushing material and limestone crushing material supply to mixing arrangement according to Mass ratio 80：12：8 ratio mixing carries out mixed processing, obtains mixed material；

(7) by above-mentioned pelletizing is dried and supplies carry out reduction treatment to rotary hearth furnace, the temperature of reduction treatment is 1100～ 1200 degrees Celsius, reduce 30～40 minutes, you can in the leaded zinc-silver flue dust from rotary hearth furnace top duct, reclaim lead, zinc, silver Deng valuable metal, after end to be restored, discharge iron content high-temperature roasting product from revolving bed, be analyzed through the composition to flue dust, Lead, zinc, the silver-colored response rate are all more than 95%；

(9) above-mentioned water quenching material is supplied and carry out primary grinding process to primary grinding device, obtain primary grinding material, one In section ore grinding material, particle diameter not higher than 0.074mm's accounts for 70～80%；Then above-mentioned primary grinding material is supplied and fill to a stages of magnetic separation Carrying out a stages of magnetic separation process in putting, obtain one section of metal iron powder and mine tailing, the magnetic field intensity that a stages of magnetic separation is processed is 1600～ 1800Oe；Then above-mentioned one section of metal iron powder is supplied and carry out secondary grinding process to secondary grinding device, obtain two-stage nitration mill Mineral aggregate, in secondary grinding material, particle diameter not higher than 0.074mm's accounts for 80～90%；Finally above-mentioned secondary grinding material is supplied to two-stage nitration Carrying out two stages of magnetic separation process in concentration equipment, obtain metal iron powder and mine tailing, the magnetic field intensity that two stages of magnetic separation are processed is 800～ 1200Oe, the Iron grade of the metal iron powder of gained and the response rate are 90% about.

Comparative example 2

The consisting of of zinc leaching residue：Full weight of iron fraction is 21.58wt%, and Zn mass fraction is 15.64wt%, Pb mass Fraction is 3.85wt%, and Ag is 0.015wt%；Jet coal selected by reducing agent, and constituent is：Fixed carbon 47.38wt%, volatilization Divide 44.60wt%, ash 4.39wt%；Quick lime selected by flux.With reference to Fig. 6, it follow these steps to be processed：

(2) above-mentioned jet coal is supplied and carry out break process to reducing agent breaker, obtain jet coal broken material, long The particle diameter of flame coal broken material is not higher than 1mm；

(3) above-mentioned quick lime is supplied and carry out break process to flux breaker, obtain quick lime broken material, raw The particle diameter of Calx broken material is not higher than 1mm；

(4) above-mentioned zinc leaching residue broken material, above-mentioned jet coal broken material and above-mentioned quick lime broken material are supplied to mixing According to mass ratio 83 in device：11：6 ratio mixing carries out mixed processing, obtains mixed material,

Comparative example 3

The consisting of of zinc leaching residue：Full weight of iron fraction is 22.72wt%, and Zn mass fraction is 16.87wt%, Pb mass Fraction is 4.13wt%, and Ag is 0.016wt%；Semi-coke selected by reducing agent, and constituent is：Fixed carbon 85wt%, ash 10wt%；Limestone selected by flux.With reference to Fig. 6, it follow these steps to be processed：

(2) above-mentioned semi-coke is supplied and carry out break process to reducing agent breaker, obtain semi-coke broken material, semi-coke is broken The particle diameter of particle is not higher than 1mm；

(4) above-mentioned zinc leaching residue broken material, above-mentioned semi-coke broken material and above-mentioned limestone crushing material are supplied to mixing dress According to mass ratio 82 in putting：14：4 ratio mixing carries out mixed processing, obtains mixed material；

Conclusion：According to embodiment 1 and comparative example 1 it can be seen that processing not higher than 10 microns of particle diameter after fine grinding with revolving bed Zinc leaching residue is compared with the zinc leaching residue processing broken rear particle diameter not higher than 1mm with rotary hearth furnace, is reaching identical Product recycling Under conditions of rate, the reduction temperature of revolving bed reduces 150～300 degrees Celsius than the reduction temperature of rotary hearth furnace, namely fine grinding-rotation Rotated bed processes zinc leaching residue and can significantly reduce reduction treatment energy consumption with respect to broken-rotary hearth furnace process zinc leaching residue, cost-effective；

According to embodiment 2 and comparative example 2 it can be seen that process the zinc leaching of not higher than 10 microns of particle diameter after fine grinding with revolving bed Slag tap and compare with the zinc leaching residue processing broken rear particle diameter not higher than 1mm with rotary hearth furnace, reaching identical product recovery rate Under the conditions of, the reduction temperature of revolving bed reduces 150～300 degrees Celsius than the reduction temperature of rotary hearth furnace, namely fine grinding-revolving bed Process zinc leaching residue and can significantly reduce reduction treatment energy consumption with respect to broken-rotary hearth furnace process zinc leaching residue, cost-effective；

According to embodiment 3 and comparative example 3 it can be seen that process the zinc leaching of not higher than 10 microns of particle diameter after fine grinding with revolving bed Slag tap and compare with the zinc leaching residue processing broken rear particle diameter not higher than 1mm with rotary hearth furnace, reaching identical product recovery rate Under the conditions of, the reduction temperature of revolving bed reduces 150～300 degrees Celsius than the reduction temperature of rotary hearth furnace, namely fine grinding-revolving bed Process zinc leaching residue and can significantly reduce reduction treatment energy consumption with respect to broken-rotary hearth furnace process zinc leaching residue, cost-effective.

In the description of this specification, reference term " embodiment ", " some embodiments ", " example ", " specifically show The description of example " or " some examples " etc. means specific features, structure, material or the spy describing with reference to this embodiment or example Point is contained at least one embodiment or the example of the present invention.In this manual, to the schematic representation of above-mentioned term not Identical embodiment or example must be directed to.And, the specific features of description, structure, material or feature can be in office Combine in an appropriate manner in one or more embodiments or example.Additionally, in the case of not conflicting, the skill of this area The feature of the different embodiments described in this specification or example and different embodiment or example can be tied by art personnel Close and combine.

Although embodiments of the invention have been shown and described above it is to be understood that above-described embodiment is example Property it is impossible to be interpreted as limitation of the present invention, those of ordinary skill in the art within the scope of the invention can be to above-mentioned Embodiment is changed, changes, replacing and modification.

Claims

1. a kind of system processing zinc leaching residue is it is characterised in that include：

Zinc leaching residue fine mill, described zinc leaching residue fine mill has zinc leaching residue entrance and the outlet of zinc leaching residue fines；

Mixing arrangement, described mixing arrangement have zinc leaching residue fines entrance, reducing agent fines entrance, flux fines entrance and Mixed material exports, and described zinc leaching residue fines entrance is connected with the outlet of described zinc leaching residue fines, and described reducing agent fines enters Mouth is connected with the outlet of described reducing agent fines, and described flux fines entrance is connected with the outlet of described flux fines；

Shaped device, described shaped device has mixed material entrance and mixing pelletizing outlet, described mixed material entrance and institute State mixed material outlet to be connected；

Drying device, described drying device has mixing pelletizing entrance and pelletizing outlet is dried, described mixing pelletizing entrance and institute State mixing pelletizing outlet to be connected；

Revolving bed, described revolving bed have be dried pelletizing entrance, leaded zinc-silver flue dust outlet and iron content high-temperature roasting product exit, Described be dried pelletizing entrance with described be dried pelletizing outlet be connected；

Granulating unit, described granulating unit has iron content high-temperature roasting product inlet and the outlet of water quenching material, described iron content high temperature roasting Burn product inlet to be connected with described iron content high-temperature roasting product exit；

Ore grinding-magnetic separating unit, described ore grinding-magnetic separating unit has water quenching material entrance, metal iron powder outlet and mine tailing outlet, described Water quenching material entrance is connected with the outlet of described water quenching material.

2. system according to claim 1 is it is characterised in that described shaped device is ball press or pelletizer.

3. system according to claim 1 and 2 is it is characterised in that described ore grinding-magnetic separating unit includes being sequentially connected Section ore grinding device, a stages of magnetic separation device, secondary grinding device and two-stage nitration concentration equipment.

4. system according to claim 3 is it is characterised in that described primary grinding device and described secondary grinding device divide It independently is not rod mill or ball mill.

5. system according to claim 4 is it is characterised in that a described stages of magnetic separation device and described two-stage nitration concentration equipment divide It independently is not magnetic separator or magnetic separation tube.

6. the system any one of a kind of employing claim 1-5 processes the method for zinc leaching residue it is characterised in that wrapping Include：

(1) zinc leaching residue is supplied and carry out levigate process to described zinc leaching residue fine mill, so that it is thin to obtain zinc leaching residue Material；

(4) described zinc leaching residue fines, described reducing agent fines and described flux fines are supplied to described mixing arrangement Carry out mixed processing, to obtain mixed material；

(7) by described pelletizing is dried and supplies carry out reduction treatment to described revolving bed to obtain leaded zinc-silver flue dust and to contain Ferrum high-temperature roasting product；

(8) described iron content high-temperature roasting product is supplied and carry out Water Quenching to described granulating unit, to obtain water quenching material；

(9) described water quenching material is supplied and carry out ore grinding-magnetic separation process to described ore grinding-magnetic separating unit, to obtain metallic iron Powder and mine tailing.

7. method according to claim 6 is it is characterised in that in step (2), described reducing agent is selected from brown coal and length At least one in flame coal；

Optional, in step (3), described flux is at least in quick lime, limestone, Calcium Carbonate and dolomite Kind；

Optional, the particle diameter of described zinc leaching residue fines, described reducing agent fines and described flux fines is separately not Higher than 10 microns.

8. the method according to claim 6 or 7 is it is characterised in that in step (4), by described zinc leaching residue fines, institute Stating reducing agent fines and described flux fines according to mass ratio is (70～90)：(10～15)：(5～10) are mixed.

9. method according to claim 8 is it is characterised in that in step (7), the temperature of described reduction treatment is 900 ～1050 degrees Celsius, the time is 30～40 minutes.

10. method according to claim 5 is it is characterised in that step (9) is carried out according to the following step：

(9-1) described water quenching material is supplied and carry out primary grinding process to primary grinding device, to obtain primary grinding material；

(9-2) described primary grinding material is supplied and carry out a stages of magnetic separation process to a stages of magnetic separation device, to obtain one section of gold Belong to iron powder and described mine tailing；

(9-3) described one section of metal iron powder is supplied and carry out secondary grinding process to secondary grinding device, to obtain two-stage nitration Ore grinding material；

(9-4) described secondary grinding material is supplied and carry out two stages of magnetic separation process to two-stage nitration concentration equipment, to obtain described gold Belong to iron powder and described mine tailing,

Optional, in step (9-1), in described primary grinding material, particle diameter not higher than 0.074mm's accounts for 70～80%；

Optional, in step (9-2), the magnetic field intensity that a described stages of magnetic separation is processed is 1600～1800Oe；

Optional, in step (9-3), in described secondary grinding material, particle diameter not higher than 0.074mm's accounts for 80～90%；

Optional, in step (9-4), the magnetic field intensity that described two stages of magnetic separation are processed is 800～1200Oe.