CN205907313U - System for handle zinc leaching residue - Google Patents
System for handle zinc leaching residue Download PDFInfo
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- CN205907313U CN205907313U CN201620822264.XU CN201620822264U CN205907313U CN 205907313 U CN205907313 U CN 205907313U CN 201620822264 U CN201620822264 U CN 201620822264U CN 205907313 U CN205907313 U CN 205907313U
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- leaching residue
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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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The utility model discloses a system for handle zinc leaching residue, include: mix forming device, it has zinc leaching residue entry, reductant entry, flux entry and mixes the pelletizing export, the rotary hearth furnace forms intake zone, preheating zone, well warm area, high -temperature region and the ejection of compact in proper order along the stove bottom rotation direction in it and distinguishes, and the intake zone is provided with mixed pelletizing entry, and the high -temperature region is provided with the smoke and dust export, and ejection of compact district is provided with the metallized pellet export, the shrend device, it has metallized pellet entry and the broken material export of metallized pellet, the grinding magnetic separation unit, it has the broken material entry of metallized pellet, the export of metal iron powder and the export of magnetic separation tailing, floatation device, it has magnetic separation tailing entry, water glass entry, collector entry, foaming agent entry, the export of silver -colored concentrate and tailing export. This system can realize the plain comprehensive recovery utilization of zinc leaching residue chinese railway, lead, zinc and silver dollar.
Description
Technical field
The utility model belongs to metallurgical technology field, and specifically, the utility model is related to a kind of process zinc leaching residue
System.
Background technology
Zinc leaching residue is a kind of solid waste slag producing in Zinc Hydrometallurgy Process, containing zinc, lead, copper, iron, 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.
Utility model content
The utility model is intended at least solve one of technical problem in correlation technique to a certain extent.For this reason, this reality
Be to propose a kind of system processing zinc leaching residue with a new purpose, this system can realize iron in zinc leaching residue, lead,
Zinc and the comprehensive reutilization of silver element, thus realizing the recycling of zinc leaching residue, and adopt the present processes institute
Metal iron powder grade up to more than 90%, the rate of recovery of iron up to more than 90%, the rate of recovery of zinc lead up to more than 95%,
The rate of recovery of silver is up to more than 90%.
In one side of the present utility model, the utility model proposes a kind of system processing zinc leaching residue.According to this
The embodiment of utility model, this system includes:
Mixed-forming device, described mixed-forming device have zinc leaching residue entrance, reducing agent entrance, flux entrance and
Mixing pelletizing outlet；
Rotary hearth furnace, sequentially forms feed zone, preheating zone, middle warm area, high temperature along furnace bottom rotation direction in described rotary hearth furnace
Area and discharge zone, described feed zone is provided with mixing pelletizing entrance, and described high-temperature region is provided with flue dust outlet, and described discharge zone sets
It is equipped with metallized pellet outlet, described mixing pelletizing entrance is connected with the outlet of described mixing pelletizing；
Granulating unit, described granulating unit has metallized pellet entrance and the outlet of metallized pellet broken material, described gold
Belong to pellet entrance to be connected with the outlet of described metallized pellet；
Mill ore magnetic selection unit, described mill ore magnetic selection unit have metallized pellet broken material entrance, metal iron powder outlet and
Magnetic tailing exports, and described metallized pellet broken material entrance is connected with the outlet of described metallized pellet broken material；
Flotation unit, described flotation unit has magnetic tailing entrance, waterglass entrance, collecting agent entrance, foaming agent enter
Mouth, silver preparation concentrate outlet and mine tailing outlet, described magnetic tailing entrance is connected with the outlet of described magnetic tailing.
Thus, the system of the process zinc leaching residue according to the utility model embodiment is passed through using rotary hearth furnace to zinc leaching residue
Carry out reduction treatment with the mixing pelletizing of reducing agent and flux, by controlling rotary hearth furnace temperature so that mixing the lead in pelletizing
Compound and zinc compound are reduced to simple substance in the high-temperature region of rotary hearth furnace, and it is secondary that the elementary lead zinc of generation is volatized into flue
Oxidation, is recovered in the form of zinc oxide and lead oxide, and mixes and only have a small amount of silver compound to be reduced in pelletizing, mixes simultaneously
The iron compound closing in pelletizing carries out drastic reduction, and the iron granule agglomeration obtaining in high-temperature region, obtains metal
Pellet, then gained metallized pellet is supplied after granulating unit to mill ore magnetic selection device be separable obtain metallic iron and
Magnetic tailing containing silver compound, and will the magnetic tailing containing silver compound be obtained supply can obtaining to flotation unit
Separate and obtain silver preparation concentrate, that is, realize the recovery of silver element, and the application adds flux in dispensing, not only can significantly drop
The energy consumption of low reduction process, and the mobility of reduzate in rotary hearth furnace can be significantly improved, promote the metallic iron that generates by
Gradually agglomeration, thus improving the degree of metalization of metallized pellet, (degree of metalization is more than more than 35%, mfe more than 85%, tfe
30%), so can reduce zinc leaching residue processing cost while ensure that iron has the higher rate of recovery.Led to by this application
Cross to be combined with mill ore magnetic selection device and flotation unit using rotary hearth furnace and zinc leaching residue is processed, it is possible to achieve in zinc leaching residue
The comprehensive reutilization of iron, lead, zinc and silver element, thus realizing the recycling of zinc leaching residue, solves zinc in prior art
Leached mud bulk deposition takes up an area and pollutes a difficult problem for environment and processing procedure high energy consumption, and the system gained using the application
, up to more than 90%, up to more than 90%, the rate of recovery of zinc lead is up to more than 95%, silver-colored for the rate of recovery of iron for the grade of metal iron powder
The rate of recovery up to more than 90%.
In addition, according to the utility model above-described embodiment process zinc leaching residue system can also have as follows add
Technical characteristic:
Optional, described mixed-forming device is ball press or pelletizer.
Optional, primary grinding equipment that described mill ore magnetic selection unit includes being sequentially connected, a stages of magnetic separation equipment, two sections of mills
Ore deposit equipment and two stages of magnetic separation equipment.Thus, it is possible to significantly improve the rate of recovery of iron.
Optional, described primary grinding equipment and described secondary grinding equipment are separately rod mill or ball mill.
Thus, it is possible to improve the rate of recovery of iron further.
Optional, a described stages of magnetic separation equipment and described two stages of magnetic separation equipment are separately magnetic separator or magnetic separation tube.
Thus, it is possible to improve the rate of recovery of iron further.
Additional aspect of the present utility model and advantage will be set forth in part in the description, partly will be from explained below
In become obvious, or recognized by practice of the present utility model.
Brief description
Above-mentioned and/or additional aspect of the present utility model and advantage will from reference to the description to embodiment for the accompanying drawings below
Become obvious and easy to understand, wherein:
Fig. 1 is the system structure diagram of the process zinc leaching residue according to one embodiment of the utility model；
Fig. 2 be according to the utility model further embodiment process zinc leaching residue system in rotary hearth furnace structural representation
Figure；
Fig. 3 is that the system of the process zinc leaching residue using one embodiment of the utility model is implemented to process the side of zinc leaching residue
Method schematic flow sheet.
Specific embodiment
Embodiment of the present utility model is described below in detail, the example of described embodiment is shown in the drawings, wherein ad initio
To the element that same or similar label represents same or similar element or has same or like function eventually.Below by ginseng
The embodiment examining Description of Drawings is exemplary it is intended to be used for explaining the utility model, and it is not intended that to the utility model
Restriction.
In the utility model, unless otherwise clearly defined and limited, term " installation ", " being connected ", " connection ", " Gu
Fixed " etc. term should be interpreted broadly, for example, it may be being fixedly connected or being detachably connected or integral；Can be
It is mechanically connected or electrically connect；Can be to be joined directly together it is also possible to be indirectly connected to by intermediary, can be two
The connection of element internal or the interaction relationship of two elements, limit unless otherwise clear and definite.Common skill for this area
For art personnel, concrete meaning in the utility model for the above-mentioned term can be understood as the case may be.
In one side of the present utility model, the utility model proposes a kind of system processing zinc leaching residue.According to this
The embodiment of utility model, with reference to Fig. 1 and Fig. 2, this system includes: mixed-forming device 100, rotary hearth furnace 200, granulating unit
300th, mill ore magnetic selection unit 400 and flotation unit 500.
According to embodiment of the present utility model, mixed-forming device 100 has zinc leaching residue entrance 101, reducing agent entrance
102nd, flux entrance 103 and mixing pelletizing outlet 104, and be suitable to be mixed into zinc leaching residue with reducing agent, flux
Type, obtains mixing pelletizing.Specifically, zinc leaching residue is the solid slag producing in Zinc Hydrometallurgy Process, and wherein contains big
The valuable metal elements such as the zinc of amount, lead, copper, iron, gallium, germanium, indium and silver, have great comprehensive utilization value.Inventor finds,
By adding flux in dispensing, the energy consumption of sequential reduction process not only can be significantly reduced, and can significantly improve and turn
The mobility of reduzate in the stove of bottom, promotes the metallic iron gradually agglomeration generating, thus improving the metal of metallized pellet
Rate (degree of metalization is more than 85%, tfe and is more than 35%, mfe more than 30%), and then zinc leaching residue processing cost can reduced
While ensure that iron has the higher rate of recovery.
According to an embodiment of the present utility model, zinc leaching residue and reducing agent, the mixed-forming of flux ratio simultaneously
It is not particularly limited, those skilled in the art can be selected according to actual needs, concrete according to one of the present utility model
Embodiment, zinc leaching residue can be (70～90): (15～20): (5～10) are mixed according to mass ratio with reducing agent, flux
Synthesis type.Inventor finds, if reducing agent addition amount is too high, can lead to the wasting of resources；And reducing agent addition amount is too low, can cause
Reduction is thorough, and if flux addition is too high, pellets can be led to, thus corroding rotary hearth furnace refractory material；And if helping
Flux addition is too low, and facilitation is inconspicuous, is unfavorable for sequential reduction.
According to further embodiment of the present utility model, the particular type of reducing agent is not particularly restricted, this area skill
Art personnel can be selected according to actual needs, and according to a specific embodiment of the present utility model, reducing agent can be choosing
At least one from semi-coke and coke.Inventor is had been surprisingly found that by many experiments, is substantially better than it using such reducing agent
His type significantly improves the reduction efficiency of lead zinc-iron, thus ensureing that lead zinc-silver has the high rate of recovery.
According to another embodiment of the present utility model, the particular type of flux is not particularly restricted, this area skill
Art personnel can be selected according to actual needs, and according to a specific embodiment of the present utility model, flux can be choosing
At least one in consisting of quicklime, lime stone, calcium carbonate and dolomite.Inventor is had been surprisingly found that by many experiments, using this
Class flux can be substantially better than the energy consumption that other types reduce reduction process, thus fall while ensureing the ferro element rate of recovery
The processing cost of low zinc leaching residue.
According to embodiment of the present utility model, with reference to Fig. 2, in rotary hearth furnace 200 along furnace bottom rotation direction sequentially form into
Material area 21, preheating zone 22, middle warm area 23, high-temperature region 24 and discharge zone 25, feed zone 21 is provided with mixing pelletizing entrance 201, high
Warm area 24 is provided with flue dust outlet 202, and discharge zone 25 is provided with metallized pellet outlet 203, and mixing pelletizing enters 201 mouthfuls and mixing
Pelletizing outlet 104 be connected, and be suitable to by obtained above mixing pelletizing supply to rotary hearth furnace feed zone so that mixing pelletizing according to
Secondary preheating zone through rotary hearth furnace, middle warm area and high-temperature region are reduced, the flue dust containing zinc oxide and lead oxide obtaining from
High-temperature region is discharged, and obtains metallized pellet and discharges from discharge zone.Specifically, feed zone in gentle high-temperature region thermal-radiating work
It is maintained at 700～900 DEG C with lower temperature, mixing pelletizing enters into feed zone and preheated, being rotated into then as furnace bottom
To middle warm area, mix pelletizing and carry out prereduction in middle warm area, wherein a small amount of lead zinc compound reduces, and remaining lead zinc impregnation
Compound in high-temperature region thoroughly reduction and flue is volatized into by secondary oxidation with simple substance form, obtain containing zinc oxide and oxygen
The flue dust changing lead is recovered (rate of recovery of lead zinc is more than 95%) from high-temperature region discharge, and during this, silver compound
Can reduce on a small quantity with having and oxidation of volatilizing carries out in flue dust, major part is still existed with silver oxide and silver sulfide form, and mixes ball
The high-temperature region of the iron compound in group carries out drastic reduction, the continuous agglomeration of the iron granule obtaining, and obtains the ball that metallizes
Group discharges from high-temperature region.
Inventor finds, by being reduced to the mixing pelletizing of zinc leaching residue and reducing agent and flux using rotary hearth furnace
Process, by control rotary hearth furnace temperature so that mixing pelletizing in lead compound and zinc compound rotary hearth furnace high-temperature region quilt
It is reduced to simple substance, the elementary lead zinc of generation is volatized into flue by secondary oxidation, is recovered in the form of zinc oxide and lead oxide,
And mix and in pelletizing, only have a small amount of silver compound to be reduced, the iron compound in mixing pelletizing carries out depth in high-temperature region simultaneously
Reduction, and the iron granule agglomeration obtaining, obtain metallized pellet, such that it is able to realize iron lead zinc in zinc leaching residue
Effective recovery.
According to an embodiment of the present utility model, the temperature of middle warm area and high-temperature region is not particularly restricted, this area
Technical staff can be selected according to actual needs, according to a specific embodiment of the present utility model, the temperature of middle warm area
Can be 1100～1200 degrees Celsius, the temperature of high-temperature region can be 1200～1350 degrees Celsius.Inventors be surprised to learn that, adopt
This temperature can be significantly better than the rate of recovery that other temperature improve lead zinc-iron, and most of silver is still deposited with compound form
Such that it is able to significantly improve the yield of silver in follow-up floatation process.
According to embodiment of the present utility model, granulating unit 300 has metallized pellet entrance 301 and metallized pellet breaks
Particle outlet 302, metallized pellet entrance 301 is connected with metallized pellet outlet 203, and is suitable to metallization obtained above
Pelletizing carries out Water Quenching, obtains metallized pellet broken material.Thus, it is possible to the metallized pellet of big particle diameter is broken into granule
The metallized pellet broken material in footpath, thus simplify follow-up Grinding procedure.
According to embodiment of the present utility model, mill ore magnetic selection unit 400 has metallized pellet broken material entrance 401, gold
Belong to iron powder outlet 402 and magnetic tailing outlet 403, metallized pellet broken material entrance 401 and the outlet of metallized pellet broken material
302 are connected, and are suitable to for metallized pellet broken material obtained above to carry out two stage grinding magnetic separation, obtain metal iron powder and magnetic separation
Mine tailing.Specifically, mill ore magnetic selection unit includes being sequentially connected primary grinding equipment, a stages of magnetic separation equipment, secondary grinding equipment
With two stages of magnetic separation equipment, and primary grinding equipment and secondary grinding equipment can be separately rod mill or ball mill,
One stages of magnetic separation equipment and two stages of magnetic separation equipment can be separately magnetic separator or magnetic separation tube.
According to an embodiment of the present utility model, during secondary grinding magnetic separation primary grinding fineness be 0.074mm with
Under account for 70～80%, a stages of magnetic separation intensity is 1600～1800oe, secondary grinding fineness be below 0.074mm account for 80～
90%, two stages of magnetic separation intensity are 800～1200oe.Inventors be surprised to learn that, this mill ore magnetic selection condition can be significantly better than other
Condition improves the separative efficiency of metallic iron and magnetic tailing, and ensures that metallic iron has the high rate of recovery and grade.
According to embodiment of the present utility model, flotation unit 500 have magnetic tailing entrance 501, waterglass entrance 502,
Collecting agent entrance 503, foaming agent entrance 504, silver preparation concentrate outlet 505 and mine tailing outlet 506, magnetic tailing entrance 501 and magnetic separation
Mine tailing outlet 403 is connected, and is suitable to magnetic tailing and waterglass, collecting agent and the foaming agent obtaining above-mentioned mill ore magnetic selection process
Mixing carries out flotation, obtains silver preparation concentrate and mine tailing.Thus, by magnetic tailing obtained above is carried out flotation process, permissible
Effectively reclaim the silver element in zinc leaching residue, and the rate of recovery of silver may be up to more than 90%.Specifically, foaming agent can be 2#
Oil.
According to an embodiment of the present utility model, magnetic tailing is with waterglass, collecting agent and foaming agent mixed proportion simultaneously
It is not particularly limited, those skilled in the art can be selected according to actual needs, concrete according to one of the present utility model
Embodiment, based on magnetic tailing per ton, the consumption of waterglass can be 200～400g, the consumption of collecting agent can for 90～
150g, the consumption of foaming agent can be 20～50g.Inventor finds, various medicament additions are too low, all can lead to floatation indicators
Decline, waterglass is as inhibitor, if addition is too high, suppression can be produced to silver, be unfavorable for the carrying out of floatation process, and collecting
The purpose of agent is the silver mineral in collecting ore pulp, if addition is too high, can bring the impurity in ore pulp into concentrate, cause silver preparation concentrate
The decline of grade, and if foaming agent addition is too high, can cause run mortise phenomenon, make foam in a large number from ore pulp overflow, cause silver
The loss of mineral.
According to further embodiment of the present utility model, the particular type of collecting agent is not particularly restricted, this area skill
Art personnel can be selected according to actual needs, and according to a specific embodiment of the present utility model, collecting agent can be fourth
Amido black medicine and the confection of thio-alcohol medicine.Inventor finds, the selectivity of butylamine black powder is stronger, the collecting of thio-alcohol medicament
Property stronger, if using single butylamine black powder or thio-alcohol medicament as collecting agent cannot ensure gained silver preparation concentrate grade and
Yield, and inventor is had been surprisingly found that by many experiments, permissible using the confection containing butylamine black powder and thio-alcohol medicine
Significantly improve grade and the yield of gained silver preparation concentrate.
According to another embodiment of the present utility model, the composition containing butylamine black powder and the confection of thio-alcohol medicine
It is not particularly restricted, those skilled in the art can be selected according to actual needs, had according to one of the present utility model
Body embodiment, in confection, butylamine black powder can be (1:1)～(3:1) with the mass ratio of thio-alcohol medicine.Invention human hair
Existing, the selectivity of butylamine black powder is stronger, and the collecting performance of thio-alcohol medicine is stronger, if the ratio of butylamine black powder is too high, can make
Become the grade of flotation concentrate higher, but the rate of recovery is relatively low；If thio-alcohol drug ratios are too high, the grade of flotation concentrate can be caused
Relatively low, and the rate of recovery is higher.Thus, by by butylamine black powder and thio-alcohol medicine according to this ratio mix and match using can be
Ensure that it has the higher rate of recovery while improving Floatation Concentrate Grade.
The system of the process zinc leaching residue according to the utility model embodiment is passed through and to go back to zinc leaching residue using rotary hearth furnace
The former dose of mixing pelletizing with flux carries out reduction treatment, by controlling rotary hearth furnace temperature so that the leaded in mixing pelletizing is closed
Thing and zinc compound are reduced to simple substance in the high-temperature region of rotary hearth furnace, and the elementary lead zinc of generation is volatized into flue by secondary oxygen
Change, be recovered in the form of zinc oxide and lead oxide, and mix and in pelletizing, only have a small amount of silver compound to be reduced, mix simultaneously
Iron compound in pelletizing carries out drastic reduction, and the iron granule agglomeration obtaining in high-temperature region, is metallized
Pelletizing, then gained metallized pellet being supplied after granulating unit to mill ore magnetic selection device is separable to obtain metallic iron and contain
There is the magnetic tailing of silver compound, and will the magnetic tailing containing silver compound be obtained supply being divided to flotation unit
From obtaining silver preparation concentrate, that is, realize the recovery of silver element, and the application adds flux in dispensing, not only can significantly reduce
The energy consumption of reduction process, and the mobility of reduzate in rotary hearth furnace can be significantly improved, promote the metallic iron generating gradually
Agglomeration, thus improving the degree of metalization of metallized pellet, (degree of metalization is more than more than 35%, mfe more than 85%, tfe
30%), so can reduce zinc leaching residue processing cost while ensure that iron has the higher rate of recovery.Led to by this application
Cross to be combined with mill ore magnetic selection device and flotation unit using rotary hearth furnace and zinc leaching residue is processed, it is possible to achieve in zinc leaching residue
The comprehensive reutilization of iron, lead, zinc and silver element, thus realizing the recycling of zinc leaching residue, solves zinc in prior art
Leached mud bulk deposition takes up an area and pollutes a difficult problem for environment and processing procedure high energy consumption, and the system gained using the application
, up to more than 90%, up to more than 90%, the rate of recovery of zinc lead is up to more than 95%, silver-colored for the rate of recovery of iron for the grade of metal iron powder
The rate of recovery up to more than 90%.
Understand for convenience, real to the system of the process zinc leaching residue using the utility model embodiment below with reference to Fig. 3
The method applying process zinc leaching residue is described in detail.According to embodiment of the present utility model, the method includes:
S100: zinc leaching residue and reducing agent, flux are carried out mixed-forming
In this step, zinc leaching residue and reducing agent, flux are carried out mixed-forming, obtain mixing pelletizing.Specifically, zinc
Leached mud be Zinc Hydrometallurgy Process in produce solid slag, and wherein contain substantial amounts of zinc, lead, copper, iron, gallium, germanium, indium and
The valuable metal element such as silver, has great comprehensive utilization value.Inventor finds, by adding flux in dispensing, no
The energy consumption of sequential reduction process only can be significantly reduced, and the mobility of reduzate in rotary hearth furnace can be significantly improved, promote
Enter the metallic iron gradually agglomeration of generation, thus improve metallized pellet degree of metalization (degree of metalization be more than 85%, tfe
It is more than 30% more than 35%, mfe), and then can ensure while reducing zinc leaching residue processing cost that iron has higher returning
Yield.
According to an embodiment of the present utility model, zinc leaching residue and reducing agent, the mixed-forming of flux ratio simultaneously
It is not particularly limited, those skilled in the art can be selected according to actual needs, concrete according to one of the present utility model
Embodiment, zinc leaching residue can be (70～90): (15～20): (5～10) are mixed according to mass ratio with reducing agent, flux
Synthesis type.Inventor finds, if reducing agent addition amount is too high, can lead to the wasting of resources；And reducing agent addition amount is too low, can cause
Reduction is thorough, and if flux addition is too high, pellets can be led to, thus corroding rotary hearth furnace refractory material；And if helping
Flux addition is too low, and facilitation is inconspicuous, is unfavorable for sequential reduction.
According to further embodiment of the present utility model, the particular type of reducing agent is not particularly restricted, this area skill
Art personnel can be selected according to actual needs, and according to a specific embodiment of the present utility model, reducing agent can be choosing
At least one from semi-coke and coke.Inventor is had been surprisingly found that by many experiments, is substantially better than it using such reducing agent
His type significantly improves the reduction efficiency of lead zinc-iron, thus ensureing that lead zinc-silver has the high rate of recovery.
According to another embodiment of the present utility model, the particular type of flux is not particularly restricted, this area skill
Art personnel can be selected according to actual needs, and according to a specific embodiment of the present utility model, flux can be choosing
At least one in consisting of quicklime, lime stone, calcium carbonate and dolomite.Inventor is had been surprisingly found that by many experiments, using this
Class flux can be substantially better than the energy consumption that other types reduce reduction process, thus fall while ensureing the ferro element rate of recovery
The processing cost of low zinc leaching residue.
S200: mixing pelletizing is supplied feed zone to rotary hearth furnace so that mixing pelletizing sequentially passes through the preheating of rotary hearth furnace
Area, middle warm area and high-temperature region are reduced
In this step, by obtained above mixing pelletizing supply to rotary hearth furnace feed zone so that mixing pelletizing warp successively
Preheating zone, middle warm area and the high-temperature region of crossing rotary hearth furnace are reduced, and the flue dust containing zinc oxide and lead oxide obtaining is from high temperature
Area discharges, and obtains metallized pellet and discharges from discharge zone.Specifically, feed zone in gentle high-temperature region heat radiation in the presence of
Temperature is maintained at 700～900 DEG C, and mixing pelletizing enters into feed zone and preheated, then as in being rotated into of furnace bottom
Warm area, mixing pelletizing carries out prereduction in middle warm area, and wherein a small amount of lead zinc compound reduces, and remaining lead zinc compound
In high-temperature region thoroughly reduction and flue is volatized into by secondary oxidation with simple substance form, obtain containing zinc oxide and lead oxide
Flue dust discharge from high-temperature region and be recovered (rate of recovery of lead zinc be more than 95%), and should during, silver compound also can be with
The oxidation that reduces on a small quantity and volatilize is had to carry out in flue dust, major part is still existed with silver oxide and silver sulfide form, and mixes in pelletizing
The high-temperature region of iron compound carry out drastic reduction, the continuous agglomeration of the iron granule obtaining, obtain metallized pellet from
High-temperature region is discharged.
Inventor finds, by being reduced to the mixing pelletizing of zinc leaching residue and reducing agent and flux using rotary hearth furnace
Process, by control rotary hearth furnace temperature so that mixing pelletizing in lead compound and zinc compound rotary hearth furnace high-temperature region quilt
It is reduced to simple substance, the elementary lead zinc of generation is volatized into flue by secondary oxidation, is recovered in the form of zinc oxide and lead oxide,
And mix and in pelletizing, only have a small amount of silver compound to be reduced, the iron compound in mixing pelletizing carries out depth in high-temperature region simultaneously
Reduction, and the iron granule agglomeration obtaining, obtain metallized pellet, such that it is able to realize iron lead zinc in zinc leaching residue
Effective recovery.
According to an embodiment of the present utility model, the temperature of middle warm area and high-temperature region is not particularly restricted, this area
Technical staff can be selected according to actual needs, according to a specific embodiment of the present utility model, the temperature of middle warm area
Can be 1100～1200 degrees Celsius, the temperature of high-temperature region can be 1200～1350 degrees Celsius.Inventors be surprised to learn that, adopt
This temperature can be significantly better than the rate of recovery that other temperature improve lead zinc-iron, and most of silver is still deposited with compound form
Such that it is able to significantly improve the yield of silver in follow-up floatation process.
S300: metallized pellet is carried out Water Quenching
In this step, metallized pellet obtained above is carried out Water Quenching, obtain metallized pellet broken material.By
The metallized pellet of big particle diameter can be broken into the metallized pellet broken material of small particle, thus simplifying follow-up ore grinding work by this
Sequence.
S400: metallized pellet broken material is carried out two stage grinding magnetic separation
In this step, metallized pellet broken material obtained above is carried out two stage grinding magnetic separation, obtain metal iron powder and
Magnetic tailing.Specifically, in two stage grinding magnetic separation primary grinding fineness be below 0.074mm account for 70～80%, a stages of magnetic separation
Intensity be 1600～1800oe, secondary grinding fineness be below 0.074mm account for 80～90%, two stages of magnetic separation intensity be 800～
1200oe.Inventors be surprised to learn that, this mill ore magnetic selection condition can be significantly better than other conditions and improve metallic iron and magnetic tailing
Separative efficiency, and ensure that metallic iron has the high rate of recovery and grade.
S500: magnetic tailing is mixed with waterglass, collecting agent and foaming agent and carries out flotation
In this step, the magnetic tailing that above-mentioned mill ore magnetic selection process is obtained is mixed with waterglass, collecting agent and foaming agent
Carry out flotation, obtain silver preparation concentrate and mine tailing.Thus, by magnetic tailing obtained above is carried out flotation process, can be effective
Reclaim the silver element in zinc leaching residue, and the rate of recovery of silver may be up to more than 90%.Specifically, foaming agent can be 2# oil.
According to an embodiment of the present utility model, magnetic tailing is with waterglass, collecting agent and foaming agent mixed proportion simultaneously
It is not particularly limited, those skilled in the art can be selected according to actual needs, concrete according to one of the present utility model
Embodiment, based on magnetic tailing per ton, the consumption of waterglass can be 200～400g, the consumption of collecting agent can for 90～
150g, the consumption of foaming agent can be 20～50g.Inventor finds, various medicament additions are too low, all can lead to floatation indicators
Decline, waterglass is as inhibitor, if addition is too high, suppression can be produced to silver, be unfavorable for the carrying out of floatation process, and collecting
The purpose of agent is the silver mineral in collecting ore pulp, if addition is too high, can bring the impurity in ore pulp into concentrate, cause silver preparation concentrate
The decline of grade, and if foaming agent addition is too high, can cause run mortise phenomenon, make foam in a large number from ore pulp overflow, cause silver
The loss of mineral.
According to further embodiment of the present utility model, the particular type of collecting agent is not particularly restricted, this area skill
Art personnel can be selected according to actual needs, and according to a specific embodiment of the present utility model, collecting agent can be fourth
Amido black medicine and the confection of thio-alcohol medicine.Inventor finds, the selectivity of butylamine black powder is stronger, the collecting of thio-alcohol medicament
Property stronger, if using single butylamine black powder or thio-alcohol medicament as collecting agent cannot ensure gained silver preparation concentrate grade and
Yield, and inventor is had been surprisingly found that by many experiments, permissible using the confection containing butylamine black powder and thio-alcohol medicine
Significantly improve grade and the yield of gained silver preparation concentrate.
According to another embodiment of the present utility model, the composition containing butylamine black powder and the confection of thio-alcohol medicine
It is not particularly restricted, those skilled in the art can be selected according to actual needs, had according to one of the present utility model
Body embodiment, in confection, butylamine black powder can be (1:1)～(3:1) with the mass ratio of thio-alcohol medicine.Invention human hair
Existing, the selectivity of butylamine black powder is stronger, and the collecting performance of thio-alcohol medicine is stronger, if the ratio of butylamine black powder is too high, can make
Become the grade of flotation concentrate higher, but the rate of recovery is relatively low；If thio-alcohol drug ratios are too high, the grade of flotation concentrate can be caused
Relatively low, and the rate of recovery is higher.Thus, by by butylamine black powder and thio-alcohol medicine according to this ratio mix and match using can be
Ensure that it has the higher rate of recovery while improving Floatation Concentrate Grade.
Being passed through using the method that the system of the process zinc leaching residue of the utility model embodiment implements process zinc leaching residue will
Zinc leaching residue is supplied to rotary hearth furnace with the mixing pelletizing of reducing agent and flux, by controlling rotary hearth furnace temperature so that mixing
Lead compound in pelletizing and zinc compound are reduced to simple substance in the high-temperature region of rotary hearth furnace, and the elementary lead zinc of generation is volatized into
Flue, by secondary oxidation, is recovered in the form of zinc oxide and lead oxide, and mixes and only have a small amount of silver compound quilt in pelletizing
Reduction, the iron compound simultaneously mixing in pelletizing carries out drastic reduction in high-temperature region, and the iron granule obtaining assembles length
Greatly, obtain metallized pellet, then to carry out after gained metallized pellet water quenching mill ore magnetic selection be separable obtain metallic iron and
Magnetic tailing containing silver compound, and by obtain the magnetic tailing containing silver compound carry out flotation can obtain separate
To silver preparation concentrate, that is, realize the recovery of silver element, and the application adds flux in dispensing, reduction not only can be significantly reduced
The energy consumption of process, and the mobility of reduzate in rotary hearth furnace can be significantly improved, promote the metallic iron generating gradually to assemble
Grow up, thus improving the degree of metalization (degree of metalization is more than 85%, tfe and is more than 35%, mfe more than 30%) of metallized pellet,
And then can ensure that iron has the higher rate of recovery while reducing zinc leaching residue processing cost.Pass through to adopt by this application
The technique that rotary hearth furnace is combined with mill ore magnetic selection and flotation, it is possible to achieve in zinc leaching residue, the synthesis of iron, lead, zinc and silver element is returned
Receive and utilize, thus realizing the recycling of zinc leaching residue, solving zinc leaching residue bulk deposition in prior art and taking up an area and pollute
Environment and a difficult problem for processing procedure high energy consumption, and adopt the grade of the present processes gained metal iron powder up to 90% with
On, up to more than 90%, up to more than 95%, the rate of recovery of silver is up to more than 90% for the rate of recovery of zinc lead for the rate of recovery of iron.
Below with reference to specific embodiment, the utility model is described, it should be noted that these embodiments are only
Descriptive, and limit the utility model never in any form.
Embodiment 1
The consisting of of zinc leaching residue: full weight of iron fraction is 20.08%, zn mass fraction is 14.85%, pb mass fraction
It is 0.012% for 3.24%, ag mass fraction, after first zinc leaching residue being dried, is crushed to below 1mm, then with after broken
Zinc leaching residue, semi-coke (fixed carbon 83%, ash content 9%), lime stone are primary raw material, according to weight proportion zinc leaching residue: semi-coke:
After the ratio mixing of lime stone=76:16:8, carry out pressure ball, obtain mixing pelletizing, then supply after the drying of this mixing pelletizing
To rotary hearth furnace, in control, the temperature of warm area is 1120～1160 degrees Celsius, and the temperature of high-temperature region is 1220～1300 degrees Celsius,
And reduce 30～40 minutes in rotary hearth furnace, the flue dust containing zinc oxide and lead oxide obtaining is discharged from high-temperature region, treat also
Discharge high-temperature metal pellet (degree of metalization is more than 85%) from rotary hearth furnace discharge zone after former end, enter through the composition to flue dust
Row analysis, the rate of recovery of lead zinc, all more than 95%, then, will carry out two sections of mills after the high-temperature metal being obtained pellet water quenching
Ore deposit magnetic separation, obtains metal iron powder and magnetic tailing, and wherein, the condition of two stage grinding magnetic separation is: first paragraph ore grinding, mog
Account for 70～80% for -0.074mm, the magnetic field intensity of magnetic separation is 1600～1800oe；Second segment ore grinding, mog be-
0.074mm accounts for 80～90%, and the magnetic field intensity of magnetic separation is 800～1200oe, the Iron grade of the metal iron powder of gained and the rate of recovery
For more than 90%, then, waterglass, collecting agent and foaming agent 2# oil in the magnetic tailing obtaining to mill ore magnetic selection, is successively added to enter
Row flotation, wherein, based on magnetic tailing per ton, waterglass consumption is 150g, and collecting agent is butylamine black powder and lauryl mercaptan
By 1:1 mass ratio mixing, consumption be 85g, 2# oil consumption be 40g, carry out one section of flotation, thus obtain can with silver preparation concentrate,
And the rate of recovery of silver is more than 90%.
Embodiment 2
The consisting of of zinc leaching residue: full weight of iron fraction is 21.54%, zn mass fraction is 15.62%, pb mass fraction
It is 0.015% for 3.89%, ag mass fraction, after first zinc leaching residue being dried, is crushed to below 1mm, then with after broken
Zinc leaching residue, coke (fixed carbon 77%, ash content 9%), quick lime are primary raw material, according to weight proportion zinc leaching residue: coke:
After the ratio mixing of quick lime=76:16:8, carry out pressure ball, obtain mixing pelletizing, then supply after the drying of this mixing pelletizing
To rotary hearth furnace, in control, the temperature of warm area is 1150～1180 degrees Celsius, and the temperature of high-temperature region is 1250～1320 degrees Celsius,
And reduce 30～40 minutes in rotary hearth furnace, the flue dust containing zinc oxide and lead oxide obtaining is discharged from high-temperature region, treat also
Discharge high-temperature metal pellet (degree of metalization is more than 85%) from rotary hearth furnace discharge zone after former end, enter through the composition to flue dust
Row analysis, the rate of recovery of lead zinc, all more than 95%, then, will carry out two sections of mills after the high-temperature metal being obtained pellet water quenching
Ore deposit magnetic separation, obtains metal iron powder and magnetic tailing, and wherein, the condition of two stage grinding magnetic separation is: first paragraph ore grinding, mog
Account for 70～80% for -0.074mm, the magnetic field intensity of magnetic separation is 1600～1800oe；Second segment ore grinding, mog be-
0.074mm accounts for 80～90%, and the magnetic field intensity of magnetic separation is 800～1200oe, the Iron grade of the metal iron powder of gained and the rate of recovery
For more than 90%, then, waterglass, collecting agent and foaming agent 2# oil in the magnetic tailing obtaining to mill ore magnetic selection, is successively added to enter
Row flotation, wherein, based on magnetic tailing per ton, waterglass consumption is 180g, and collecting agent is butylamine black powder and lauryl mercaptan
By 1:2 mass ratio mixing, consumption be 80g, 2# oil consumption be 35g, carry out one section of flotation, thus obtain can with silver preparation concentrate,
And the rate of recovery of silver is more than 90%.
Embodiment 3
The consisting of of zinc leaching residue: full weight of iron fraction is 22.72%, zn mass fraction is 16.87%, pb mass fraction
It is 0.016% for 4.13%, ag mass fraction, after first zinc leaching residue being dried, is crushed to below 1mm, then with after broken
Zinc leaching residue, semi-coke (fixed carbon 85%, ash content 10%), lime stone are primary raw material, according to weight proportion zinc leaching residue: blue
Charcoal: after the ratio mixing of lime stone=76:16:8, carry out pressure ball, obtain mixing pelletizing, then supply after the drying of this mixing pelletizing
To rotary hearth furnace, in control, the temperature of warm area is 1130～1200 degrees Celsius, and the temperature of high-temperature region is Celsius for 1200～1350
Degree, and reduce 30～40 minutes in rotary hearth furnace, the flue dust containing zinc oxide and lead oxide obtaining is discharged from high-temperature region, treats
Reduction discharges high-temperature metal pellet (degree of metalization is more than 85%) from rotary hearth furnace discharge zone, through the composition to flue dust after terminating
It is analyzed, the rate of recovery of lead zinc, all more than 95%, then, carries out two sections by after the high-temperature metal being obtained pellet water quenching
Mill ore magnetic selection, obtains metal iron powder and magnetic tailing, and wherein, the condition of two stage grinding magnetic separation is: first paragraph ore grinding, mog
Account for 70～80% for -0.074mm, the magnetic field intensity of magnetic separation is 1600～1800oe；Second segment ore grinding, mog be-
0.074mm accounts for 80～90%, and the magnetic field intensity of magnetic separation is 800～1200oe, the Iron grade of the metal iron powder of gained and the rate of recovery
For more than 90%, then, waterglass, collecting agent and foaming agent 2# oil in the magnetic tailing obtaining to mill ore magnetic selection, is successively added to enter
Row flotation, wherein, based on magnetic tailing per ton, waterglass consumption is 200g, and collecting agent is butylamine black powder and lauryl mercaptan
By 1:3 mass ratio mixing, consumption be 90g, 2# oil consumption be 40g, carry out one section of flotation, thus obtain can with silver preparation concentrate,
And the rate of recovery of silver is more than 90%.
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 of the present utility model or example.In this manual, the schematic table to above-mentioned term
State and be necessarily directed to identical embodiment or example.And, the specific features of description, structure, material or feature are permissible
Any one or more embodiments or example combine in an appropriate manner.Additionally, in the case of not conflicting, this area
Technical staff the feature of the different embodiments described in this specification or example and different embodiment or example can be entered
Row combines and combines.
Although of the present utility model embodiment has been shown and described above it is to be understood that above-described embodiment is
Exemplary it is impossible to be interpreted as that those of ordinary skill in the art is in scope of the present utility model to restriction of the present utility model
Interior above-described embodiment can be changed, change, replacing and modification.
Claims (5)
1. a kind of system processing zinc leaching residue is it is characterised in that include:
Mixed-forming device, described mixed-forming device has zinc leaching residue entrance, reducing agent entrance, flux entrance and mixing
Pelletizing exports；
Rotary hearth furnace, in described rotary hearth furnace along furnace bottom rotation direction sequentially form feed zone, preheating zone, middle warm area, high-temperature region and
Discharge zone, described feed zone is provided with mixing pelletizing entrance, and described high-temperature region is provided with flue dust outlet, and described discharge zone is provided with
Metallized pellet exports, and described mixing pelletizing entrance is connected with the outlet of described mixing pelletizing；
Granulating unit, described granulating unit has metallized pellet entrance and the outlet of metallized pellet broken material, described metallization
Pelletizing entrance is connected with the outlet of described metallized pellet；
Mill ore magnetic selection unit, described mill ore magnetic selection unit has metallized pellet broken material entrance, metal iron powder outlet and magnetic separation
Mine tailing exports, and described metallized pellet broken material entrance is connected with the outlet of described metallized pellet broken material；
Flotation unit, described flotation unit has magnetic tailing entrance, waterglass entrance, collecting agent entrance, foaming agent entrance, silver
Concentrate outlet and mine tailing outlet, described magnetic tailing entrance is connected with the outlet of described magnetic tailing.
2. system according to claim 1 is it is characterised in that described mixed-forming device is ball press or pelletizer.
3. system according to claim 1 and 2 is it is characterised in that described mill ore magnetic selection unit includes being sequentially connected
Section grinding attachment, a stages of magnetic separation equipment, secondary grinding equipment and two stages of magnetic separation equipment.
4. system according to claim 3 is it is characterised in that described primary grinding equipment and described secondary grinding equipment divide
It independently is not rod mill or ball mill.
5. system according to claim 3 is it is characterised in that a described stages of magnetic separation equipment and described two stages of magnetic separation equipment divide
It independently is not magnetic separator or magnetic separation tube.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620822264.XU CN205907313U (en) | 2016-08-01 | 2016-08-01 | System for handle zinc leaching residue |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620822264.XU CN205907313U (en) | 2016-08-01 | 2016-08-01 | System for handle zinc leaching residue |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106244801A (en) * | 2016-08-01 | 2016-12-21 | 江苏省冶金设计院有限公司 | Process the method and system of zinc leaching residue |
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| CN106244801A (en) * | 2016-08-01 | 2016-12-21 | 江苏省冶金设计院有限公司 | Process the method and system of zinc leaching residue |
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