CN103898335A - System for processing zinc roasting ore - Google Patents
System for processing zinc roasting ore Download PDFInfo
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- CN103898335A CN103898335A CN201410111767.1A CN201410111767A CN103898335A CN 103898335 A CN103898335 A CN 103898335A CN 201410111767 A CN201410111767 A CN 201410111767A CN 103898335 A CN103898335 A CN 103898335A
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Abstract
The invention discloses a system for processing zinc roasting ore. The system comprises a neutral leaching device, a first thickening device, a neutralization device, a second thickening device, a high acid leaching device, a third thickening device, an ultra-acid leaching device, a fourth thickening device, a first washing and filtering device, a spraying and iron removing device, a classifying device, a fifth thickening device, and a second washing and filtering device. According the embodiment of the invention, the system for processing the zinc roasting ore can significantly improve the recycling rate of valuable metals.
Description
Technical field
The present invention relates to field of metallurgy, particularly, the present invention relates to a kind of system of processing zinc roasted ore.
Background technology
The leading technique of current zinc hydrometallurgy is divided into the large class of direct leaching two of sulfuric acid+leaching and zinc ore concentrate, wherein sulfuric acid+leaching comprises that again conventional two sections of leachings and hot acid leach, for the difference of heavy iron method, hot acid leaches and has derived again the techniques such as jarosite process, goethite process, hematite process.The direct leaching of zinc ore concentrate comprises that pressure leaching and normal pressure oxygen soak two kinds.All there is the deficiency of self in various technique above.
Summary of the invention
The present invention is intended to one of solve the problems of the technologies described above at least to a certain extent.For this reason, one object of the present invention is to propose a kind of system of processing zinc roasted ore, and this system can significantly improve the recovery utilization rate of valuable metal.
In one aspect of the invention, the present invention proposes a kind of system of processing zinc roasted ore.Obtain embodiment according to the present invention, this system comprises:
Neutral leaching device, described neutral leaching device is for mixing zinc roasted ore and carrying out neutrality and leach processing with oxygenant and electrolytic solution;
The first dense device, described the first dense device is connected with described neutral leaching device, for the neutral leach liquor obtaining is carried out to the first dense processing, to obtain respectively the first supernatant liquor and the first end liquid;
Neutralizing treatment device, described neutralizing treatment device is connected with described the first dense device, for described the first end liquid obtaining is carried out to neutralizing treatment;
The second dense device, described the second dense device is connected with described neutralizing treatment device, carries out the second dense processing for the solution of the process neutralizing treatment to obtaining, to obtain respectively the second supernatant liquor and the second end liquid;
Peracid leaching device, described peracid leaching device is connected with described the second dense device, for described the second end liquid obtaining is carried out to high Ore Leaching processing;
The 3rd dense device, described the 3rd dense device is connected with described peracid leaching device, for the solution of the high Ore Leaching processing of the process obtaining is carried out to the 3rd dense processing, to obtain respectively the 3rd supernatant liquor and the 3rd end liquid;
Super acid leaching device, described super acid leaching device is connected with described the 3rd dense device, leaches processing for described the 3rd end liquid obtaining being carried out to super acid;
The 4th dense device, described the 4th dense device is connected with described super acid leaching device, carries out the 4th dense processing, to obtain respectively the 4th supernatant liquor and the 4th end liquid for the obtained solution that leaching is processed through super acid;
The first washing and filtering device, described the first washing and filtering device is connected with described the 4th dense device, for described the 4th end liquid obtaining is carried out to the first washing and filtering, to obtain respectively plumbous silver-colored slag and the first filtrate;
Spray deironing apparatus, described spray Chen Tie device is connected with described the second dense device, is suitable for utilizing zinc roasted ore and/or zinc oxide fumes to described the second supernatant liquor is sprayed to deironing processing, to obtain iron ore slurry;
Sorting equipment, described sorting equipment is connected with described spray deironing apparatus, for described iron ore slurry is carried out to stage treatment, to obtain respectively coarse sand and mixing solutions;
The 5th dense device, described the 5th dense device is connected with described sorting equipment, for described mixing solutions being carried out to the 5th dense processing, to obtain respectively the 5th supernatant liquor and the 5th end liquid; And
The second washing and filtering device, described the second washing and filtering device is connected with described the 5th dense device, carries out the second washing and filtering for described the 5th end liquid, to obtain scum and the second filtrate.
Leach treatment process and can significantly improve scum quality using zinc roasted ore or oxygenant flue dust as the neutralizing agent of spray deironing treating processes by employing super acid according to the system of the processing zinc roasted ore of the embodiment of the present invention, and significantly reduce plumbous silver-colored slag slag rate, in the plumbous silver-colored slag of gained, plumbous silver is of high grade simultaneously, in addition, obtain plumbous silver-colored slag and can deliver to plumbous reduction furnace for smelting direct production lead bullion, thereby can realize plumbous zinc complementation, wet fire is compatible, the technique object of energy-saving and emission-reduction, open up new way for reducing zinc hydrometallurgy production cost, realize smelting waste slag innoxious, the object of resource utilization, promote the lifting of Business Economic Benefit.
In addition, the system of processing zinc roasted ore according to the above embodiment of the present invention can also have following additional technical characterictic:
In some embodiments of the invention, the system of described processing zinc roasted ore further comprises: refining plant, described refining plant is connected with described the first dense device, for described the first supernatant liquor is carried out to purifying treatment.Thus, can significantly improve the recovery utilization rate of valuable metal.
In some embodiments of the invention, described the 3rd dense device is connected with described neutralizing treatment device respectively with described sorting equipment, for described the 3rd supernatant liquor and described coarse sand are returned and carry out described neutralizing treatment.Thus, can further improve the recovery utilization rate of valuable metal.
In some embodiments of the invention, described the 4th dense device is connected with described peracid leaching device respectively with described the first washing device, for described the 4th supernatant liquor and described the first filtrate returning are carried out to described high Ore Leaching processing.Thus, can further improve the recovery utilization rate of valuable metal.
In some embodiments of the invention, described the 5th dense device is connected with described neutral leaching device respectively with described the second washing and filtering device, for described the 5th supernatant liquor and described the second filtrate returning are carried out to the described neutral processing of leaching.Thus, can further improve the recovery utilization rate of valuable metal.
Additional aspect of the present invention and advantage in the following description part provide, and part will become obviously from the following description, or recognize by practice of the present invention.
Accompanying drawing explanation
Above-mentioned and/or additional aspect of the present invention and advantage accompanying drawing below combination is understood becoming the description of embodiment obviously and easily, wherein:
Fig. 1 is the structural representation of processing according to an embodiment of the invention the system of zinc roasted ore;
Fig. 2 is the structural representation of the system of the processing zinc roasted ore of another embodiment according to the present invention;
Fig. 3 is the structural representation of the system of the processing zinc roasted ore of another embodiment according to the present invention;
Fig. 4 utilizes the system of the processing zinc roasted ore of one embodiment of the invention to process the schematic flow sheet of the method for zinc roasted ore;
Fig. 5 utilizes the system of the processing zinc roasted ore of another embodiment of the present invention to process the schematic flow sheet of the method for zinc roasted ore;
Fig. 6 utilizes the system of the processing zinc roasted ore of another embodiment of the present invention to process the schematic flow sheet of the method for zinc roasted ore.
Embodiment
Describe embodiments of the invention below in detail, the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has the element of identical or similar functions from start to finish.Be exemplary below by the embodiment being described with reference to the drawings, be intended to for explaining the present invention, and can not be interpreted as limitation of the present invention.
In description of the invention, it will be appreciated that, term " first ", " second " be only for describing object, and can not be interpreted as indication or hint relative importance or the implicit quantity that indicates indicated technical characterictic.Thus, one or more these features can be expressed or impliedly be comprised to the feature that is limited with " first ", " second ".In description of the invention, the implication of " multiple " is two or more, unless otherwise expressly limited specifically.
In the present invention, unless otherwise clearly defined and limited, the terms such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, and for example, can be to be fixedly connected with, and can be also to removably connect, or connect integratedly; Can be mechanical connection, can be also electrical connection; Can be to be directly connected, also can indirectly be connected by intermediary, can be the connection of two element internals.For the ordinary skill in the art, can understand as the case may be above-mentioned term concrete meaning in the present invention.
In one aspect of the invention, the present invention proposes a kind of system of processing zinc roasted ore.System below with reference to the processing zinc roasted ore of Fig. 1-3 pair embodiment of the present invention is described in detail.According to embodiments of the invention, this system comprises:
Neutral leaching device 100: according to embodiments of the invention, neutral leaching device 100 is for zinc roasted ore being mixed with oxygenant and electrolytic solution and carrying out neutrality leaching processing, thereby can obtain neutral leach liquor.According to embodiments of the invention, the composition of zinc roasted ore is also not particularly limited, according to a particular embodiment of the invention, zinc roasted ore can be zinc, the cadmium of 0.1～0.5wt%, the lead of 1～3wt%, the copper of 0.2～1.0wt%, the iron of 8～20wt%, the sulphur of 0.1～2.5wt%, the calcium oxide of 0.5～1.0wt%, the magnesium oxide of 0.5～1.0wt%, the silicon-dioxide of 1.0～5.0wt% and a small amount of arsenic, silver, fluorine, chlorine, indium, germanium, cobalt and the nickel etc. that contain 45～55wt%.
According to embodiments of the invention, the particular type of oxygenant is also not particularly limited, and according to a particular embodiment of the invention, oxygenant can be for being selected from least one in manganese ore powder, potassium permanganate, air and oxygen.According to embodiments of the invention, the particular type of electrolytic solution is also not particularly limited, and according to a particular embodiment of the invention, electrolytic solution can be zinc electrolysis waste solution.According to a particular embodiment of the invention, Zn in zinc electrolysis waste solution
2+concentration can be 45-55g/L, H
2sO
4concentration can be 160-180g/L.According to embodiments of the invention, the condition that neutral leaching is processed is also not particularly limited, according to a particular embodiment of the invention, neutral leaching processed and can under the terminal acidity that be 4.8～5.2 with pH at the temperature of 50～70 degrees Celsius, be carried out completing for 1.5～2.5 hours.In this step, particularly, first, under the effect of oxygenant, make zinc, copper, cadmium etc. be oxidized into oxide compound, then under the effect of electrolytic solution, mainly carry out following chemical reaction:
ZnO+H
2SO
4=ZnSO
4+H
2O
CuO+H
2SO
4=CuSO
4+H
2O
CdO+H
2SO
4=CdSO
4+H
2O
The first dense device 200: according to embodiments of the invention, the first dense device 200 is connected with neutral leaching device 100, for the neutral leach liquor obtaining is carried out to the first dense processing, thereby can obtain respectively the first supernatant liquor and the first end liquid.According to embodiments of the invention, the first supernatant liquor main component: Zn
2+concentration can be 140～160g/L, Fe
alwaysthe concentration of ion can be lower than 30mg/L, Cu
2+concentration can be 200～1000mg/L, Cd
2+concentration can be 200～600mg/L, the first end liquid main component: the content of zinc element can be 18～22wt%, the content of ferro element can be 10～15wt%.In this step, particularly, neutral leach liquor is added in thickener, through natural subsidence process carry out liquid-solid separation after adding polyacrylamide flocculant simultaneously.
Neutralizing treatment device 300: according to embodiments of the invention, neutralizing treatment device 300 is connected with the first dense device 200, for the first end liquid obtaining is carried out to neutralizing treatment, thereby can obtain the solution through neutralizing treatment.According to embodiments of the invention, the condition of neutralizing treatment is also not particularly limited, and according to a particular embodiment of the invention, neutralizing treatment can carry out completing for 1.5～2.5 hours under the terminal acidity that be 1.5～2.5 with pH at the temperature of 60～75 degrees Celsius.In this step, concrete, in the first end liquid obtaining, contain a large amount of zinc by neutralizing treatment, can make most of zinc be dissolved in solution, thereby can improve the zinc concentration in solution, for follow-up spray deironing is prepared.
The second dense device 400: according to embodiments of the invention, the second dense device 400 is connected with neutralizing treatment device 300, carries out the second dense processing for the solution of the process neutralizing treatment to obtaining, thereby can obtain respectively the second supernatant liquor and the second end liquid.According to embodiments of the invention, the second supernatant liquor main component: Zn
2+concentration can be 100～140g/L, Fe
alwaysionic concn can be 5～35g/L, and the content of the second end liquid main component Zn element is 15～25wt%, and the content of Fe element is 15～25wt%.
Peracid leaching device 500: according to embodiments of the invention, peracid leaching device 500 is connected with the second dense device 400, for the second end liquid obtaining is carried out to high Ore Leaching processing, thereby can obtain the solution through high Ore Leaching processing.According to embodiments of the invention, the condition of high Ore Leaching processing is also not particularly limited, and according to a particular embodiment of the invention, high Ore Leaching processing can be to carry out at least 2 hours under 40～70g/L condition with terminal acidity at the temperature of 85～95 degrees Celsius.The main chemical reactions occurring is:
ZnFe
2O
4+4H
2SO
4=Fe
2（SO
4）
3+ZnSO
4+4H
2O
ZnO+H
2SO
4=ZnSO
4+H
2O
The 3rd dense device 600: according to embodiments of the invention, the 3rd dense device 600 is connected with peracid leaching device 500, for the solution of the high Ore Leaching processing of the process obtaining is carried out to the 3rd dense processing, thereby can obtain respectively the 3rd supernatant liquor and the 3rd end liquid.According to embodiments of the invention, the 3rd supernatant liquor main component: Zn
2+concentration can be 100～120g/L, Fe
alwaysthe concentration of ion can be 15～30g/L, H
2sO
4concentration can be 40～70g/L; The 3rd end liquid main component: the content of zinc element can be 5～12wt%, the content of ferro element can be 5～15wt%.
Super acid leaching device 700: according to embodiments of the invention, super acid leaching device 700 is connected with the 3rd dense device 600, leaches processing for described the 3rd end liquid obtaining being carried out to super acid, thereby can obtain leaching through super acid the solution of processing.According to embodiments of the invention, super acid-treated condition is also not particularly limited, and according to a particular embodiment of the invention, super acid leaches and processes can be to carry out at least 2 hours under 100～120g/L condition with terminal acidity at the temperature of 85～95 degrees Celsius.In this step, concrete, in the 3rd end liquid, add the vitriol oil and zinc electrolysis waste solution, adopt the strengthening of high temperature peracid to leach the zinc ferrite that is difficult to leaching, can further improve thus the leaching yield of zinc.The main chemical reactions occurring is: ZnFe
2o
4+ 4H
2sO
4=Fe
2(SO
4)
3+ ZnSO
4+ 4H
2o.
The 4th dense device 800: according to embodiments of the invention, the 4th dense device 800 is connected with super acid leaching device 700, be used for the obtained solution that leaching is processed through super acid and carry out the 4th dense processing, thereby can obtain respectively the 4th supernatant liquor and the 4th end liquid.According to embodiments of the invention, the 4th supernatant liquor main component: Zn
2+concentration can be 100～120g/L, Fe
alwaysthe concentration of ion can be 10～35g/L, H
2sO
4concentration can be 100～120g/L, the 4th end liquid main component: the content of zinc element can be 4～10wt%, and the content of ferro element can be 5～15wt%, and the content of lead element can be 10～20wt%.
The first washing and filtering device 900: according to embodiments of the invention, the first washing and filtering device 900 is connected with the 4th dense device 800, for described the 4th end liquid obtaining is carried out to the first washing and filtering, thereby can obtain respectively plumbous silver-colored slag and the first filtrate.
Spray deironing apparatus 1000: according to embodiments of the invention, spray Chen Tie device 1000 is connected with the second dense device 400, be suitable for utilizing zinc roasted ore and/or zinc oxide fumes to described the second supernatant liquor is sprayed to deironing processing, thereby can obtain iron ore slurry.According to embodiments of the invention, the condition of spray deironing processing is also not particularly limited, and according to a particular embodiment of the invention, spray deironing processing can be carried out under the terminal acidity that be 3.0～4.5 with pH at the temperature of 80～90 degrees Celsius.The main chemical reactions occurring is:
Fe
2（SO
4）
3+H
2O+3ZnO=2FeO.OH↓+3ZnSO
4
Sorting equipment 1100: according to embodiments of the invention, sorting equipment 1100 is connected with spray deironing apparatus 1000, for iron ore slurry is carried out to stage treatment, thereby can obtain respectively coarse sand and mixing solutions.In this step, concrete, obtained iron ore slurry is carried out to cyclone classification or screw classifying, fine particle (scum) is separated with coarse particles (unreacted is calcining completely), the fine particle of separating carries out dense processing, and coarse particles returns to neutralizing treatment.
The 5th dense device 1200: according to embodiments of the invention, the 5th dense device 1200 is connected with sorting equipment 1100, for mixing solutions being carried out to the 5th dense processing, thereby can obtain respectively the 5th supernatant liquor and the 5th end liquid.According to embodiments of the invention, the 5th supernatant liquor main component: Zn
2+concentration can be 100～140g/L, Fe
alwaysthe concentration of ion can be 1～4g/L, the 5th end liquid main component: the content of zinc element can be 5.0～12.0wt%, and the content of ferro element can be 25～35wt%.
The second washing and filtering device 1300: according to embodiments of the invention, the second washing and filtering device 1300 is connected with the 5th dense device 1200, for the 5th end liquid is carried out to the second washing and filtering, thereby can obtain scum and the second filtrate.
Can effectively implement the method for above-mentioned processing zinc roasted ore according to the system of the processing zinc roasted ore of the embodiment of the present invention.
With reference to figure 2, according to embodiments of the invention, the system of processing zinc roasted ore further comprises:
Refining plant 1400: according to embodiments of the invention, refining plant 1400 is connected with the first dense device 200, for the first supernatant liquor is carried out to purifying treatment.In this step, particularly, purifying treatment is in fact by adding zinc dust precipitation copper removal, cadmium, or adds Zinc dust Cementation for Cobalt Removal, nickel in the time that other additive (as antimonic salt) exists.Thus, can make the Cu in the first supernatant liquor by purifying treatment
2+, Cd
2+, Co
2+, Ni
2+deng impurity except within the permission content range of zinc electrolytic deposition process, guarantee the zinc metal sheet that normally carries out and produce better quality of electrolytic deposition process, simultaneously, by the inrichment of scavenging process, making has a valency associated element in raw material, as Cu, Cd, Co etc. obtain enrichment, and can obtain byproduct copper ore concentrates, Spongy Cadmium and cobalt concentrate through processing.Its main main chemical reactions equation is as follows:
CuSO
4+Zn=Cu↓+ZnSO
4
CdSO
4+Zn=Cd↓+ZnSO
4
CoSO
4+Zn=Co↓+ZnSO
4
NiSO
4+Zn=Ni↓+ZnSO
4
With reference to figure 3, according to embodiments of the invention, according to the embodiment of the present invention, the 3rd dense device 600 is connected with neutralizing treatment device 300 respectively with sorting equipment 100, for the 3rd supernatant liquor and coarse sand are returned and carry out neutralizing treatment.Thus, thus, can utilize the acid in zinc oxide neutralization the 3rd supernatant liquor in the first end liquid, thereby the qualified front liquid of deironing can be provided.
According to embodiments of the invention, the 4th dense device 800 is connected with peracid leaching device 500 respectively with the first washing device 900, for the 4th supernatant liquor and the first filtrate returning are carried out to high Ore Leaching processing.Thus, can significantly improve the leaching yield of zinc.
According to embodiments of the invention, the 5th dense device 1200 is connected with neutral leaching device 100 respectively with the second washing and filtering device 1300, for the 5th supernatant liquor and the second filtrate returning are carried out to neutrality leaching processing.Thus, can further improve the recovery utilization rate of valuable metal.
Understand for convenient, utilize the method for the system processing zinc roasted ore of the processing zinc roasted ore of the embodiment of the present invention to be described in detail below with reference to Fig. 4-6 pair.According to embodiments of the invention, the method comprises:
S100: neutral leaching processed
According to embodiments of the invention, roasted ore mixed with oxygenant and electrolytic solution and carry out neutrality and leach processing, thereby can obtain neutral leach liquor.According to embodiments of the invention, the composition of zinc roasted ore is also not particularly limited, according to a particular embodiment of the invention, zinc roasted ore can be zinc, the cadmium of 0.1～0.5wt%, the lead of 1～3wt%, the copper of 0.2～1.0wt%, the iron of 8～20wt%, the sulphur of 0.1～2.5wt%, the calcium oxide of 0.5～1.0wt%, the magnesium oxide of 0.5～1.0wt%, the silicon-dioxide of 1.0～5.0wt% and a small amount of arsenic, silver, fluorine, chlorine, indium, germanium, cobalt and the nickel etc. that contain 45～55wt%.
According to embodiments of the invention, the particular type of oxygenant is also not particularly limited, and according to a particular embodiment of the invention, oxygenant can be for being selected from least one in manganese ore powder, potassium permanganate, air and oxygen.According to embodiments of the invention, the particular type of electrolytic solution is also not particularly limited, and according to a particular embodiment of the invention, electrolytic solution can be zinc electrolysis waste solution.According to a particular embodiment of the invention, Zn in zinc electrolysis waste solution
2+concentration can be 45-55g/L, H
2sO
4concentration can be 160-180g/L.According to embodiments of the invention, the condition that neutral leaching is processed is also not particularly limited, according to a particular embodiment of the invention, neutral leaching processed and can under the terminal acidity that be 4.8～5.2 with pH at the temperature of 50～70 degrees Celsius, be carried out completing for 1.5～2.5 hours.In this step, particularly, first, under the effect of oxygenant, make zinc, copper, cadmium etc. be oxidized into oxide compound, then under the effect of electrolytic solution, mainly carry out following chemical reaction:
ZnO+H
2SO
4=ZnSO
4+H
2O
CuO+H
2SO
4=CuSO
4+H
2O
CdO+H
2SO
4=CdSO
4+H
2O
S200: the first dense processing
According to embodiments of the invention, obtained neutral leach liquor is carried out to the first dense processing, thereby can obtain respectively the first supernatant liquor and the first end liquid.According to embodiments of the invention, the first supernatant liquor main component: Zn
2+concentration can be 140～160g/L, Fe
alwaysthe concentration of ion can be lower than 30mg/L, Cu
2+concentration can be 200～1000mg/L, Cd
2+concentration can be 200～600mg/L, the first end liquid main component: the content of zinc element can be 18～22wt%, the content of ferro element can be 10～15wt%.In this step, particularly, neutral leach liquor is added in thickener, through natural subsidence process carry out liquid-solid separation after adding polyacrylamide flocculant simultaneously.
S300: neutralizing treatment
According to embodiments of the invention, the first obtained end liquid is carried out to neutralizing treatment, thereby can obtain the solution through neutralizing treatment.According to embodiments of the invention, the condition of neutralizing treatment is also not particularly limited, and according to a particular embodiment of the invention, neutralizing treatment can carry out completing for 1.5～2.5 hours under the terminal acidity that be 1.5～2.5 with pH at the temperature of 60～75 degrees Celsius.In this step, concrete, in the first end liquid obtaining, contain a large amount of zinc by neutralizing treatment, can make most of zinc be dissolved in solution, thereby can improve the zinc concentration in solution, for follow-up spray deironing is prepared.
S400: the second dense processing
According to embodiments of the invention, the solution of obtained process neutralizing treatment is carried out to the second dense processing, thereby can obtain respectively the second supernatant liquor and the second end liquid.According to embodiments of the invention, the second supernatant liquor main component: Zn
2+concentration can be 100～140g/L, Fe
alwaysionic concn can be 5～35g/L, and the content of the second end liquid main component Zn element is 15～25wt%, and the content of Fe element is 15～25wt%.
S500: high Ore Leaching processing
According to embodiments of the invention, the second obtained end liquid is carried out to high Ore Leaching processing, thereby can obtain the solution through high Ore Leaching processing.According to embodiments of the invention, the condition of high Ore Leaching processing is also not particularly limited, and according to a particular embodiment of the invention, high Ore Leaching processing can be to carry out at least 2 hours under 40～70g/L condition with terminal acidity at the temperature of 85～95 degrees Celsius.The main chemical reactions occurring is:
ZnFe
2O
4+4H
2SO
4=Fe
2（SO
4）
3+ZnSO
4+4H
2O
ZnO+H
2SO
4=ZnSO
4+H
2O
S600: the 3rd dense processing
According to embodiments of the invention, the solution of high process obtaining Ore Leaching processing is carried out to the 3rd dense processing, to obtain respectively the 3rd supernatant liquor and the 3rd end liquid.According to embodiments of the invention, the 3rd supernatant liquor main component: Zn
2+concentration can be 100～120g/L, Fe
alwaysthe concentration of ion can be 15～30g/L, H
2sO
4concentration can be 40～70g/L; The 3rd end liquid main component: the content of zinc element can be 5～12wt%, the content of ferro element can be 5～15wt%.With reference to figure 5, according to embodiments of the invention, the 3rd supernatant liquor can be returned and carries out neutralizing treatment.Thus, can utilize the acid in zinc oxide neutralization the 3rd supernatant liquor in the first end liquid, thereby the qualified front liquid of deironing can be provided.
S700: super acid leaches to be processed
According to embodiments of the invention, the 3rd obtained end liquid is carried out to super acid and leach processing, thereby can obtain leaching through super acid the solution of processing.According to embodiments of the invention, super acid-treated condition is also not particularly limited, and according to a particular embodiment of the invention, super acid leaches and processes can be to carry out at least 2 hours under 100～120g/L condition with terminal acidity at the temperature of 85～95 degrees Celsius.In this step, concrete, in the 3rd end liquid, add the vitriol oil and zinc electrolysis waste solution, adopt the strengthening of high temperature peracid to leach the zinc ferrite that is difficult to leaching, can further improve thus the leaching yield of zinc.The main chemical reactions occurring is: ZnFe
2o
4+ 4H
2sO
4=Fe
2(SO
4)
3+ ZnSO
4+ 4H
2o.
S800: the 4th dense processing
According to embodiments of the invention, the obtained solution that leaching is processed through super acid is carried out to the 4th dense processing, to obtain respectively the 4th supernatant liquor and the 4th end liquid.According to embodiments of the invention, the 4th supernatant liquor main component: Zn
2+concentration can be 100～120g/L, Fe
alwaysthe concentration of ion can be 10～35g/L, H
2sO
4concentration can be 100～120g/L, the 4th end liquid main component: the content of zinc element can be 4～10wt%, and the content of ferro element can be 5～15wt%, and the content of lead element can be 10～20wt%.
S900: the first washing and filtering
According to embodiments of the invention, the 4th obtained end liquid is carried out to the first washing and filtering, thereby can obtain respectively plumbous silver-colored slag and the first filtrate.With reference to figure 5, according to embodiments of the invention, can return and carry out high Ore Leaching processing by the first obtained filtrate with the 4th supernatant liquor, can improve thus the leaching yield of zinc.
S1000: spray deironing processing
According to embodiments of the invention, utilize the second supernatant liquor that zinc roasted ore and/or zinc oxide fumes obtain S400 to spray deironing processing, thereby can obtain iron ore slurry.According to embodiments of the invention, the condition of spray deironing processing is also not particularly limited, and according to a particular embodiment of the invention, spray deironing processing can be carried out under the terminal acidity that be 3.0～4.5 with pH at the temperature of 80～90 degrees Celsius.The main chemical reactions occurring is:
Fe
2（SO
4）
3+H
2O+3ZnO=2FeO.OH↓+3ZnSO
4
S1100: stage treatment
According to embodiments of the invention, obtained iron ore slurry is carried out to stage treatment, thereby can obtain respectively coarse sand and mixing solutions.With reference to figure 5, according to embodiments of the invention, obtained coarse sand can be returned and carries out neutralizing treatment, so that liquid before qualified deironing to be provided.In this step, concrete, obtained iron ore slurry is carried out to cyclone classification or screw classifying, fine particle (scum) is separated with coarse particles (unreacted is calcining completely), the fine particle of separating carries out dense processing, and coarse particles returns to neutralizing treatment.
S1200: the 5th dense processing
According to embodiments of the invention, above obtained mixing solutions is carried out to the 5th dense processing, thereby can obtain respectively the 5th supernatant liquor and the 5th end liquid.According to embodiments of the invention, the 5th supernatant liquor main component: Zn
2+concentration can be 100～140g/L, Fe
alwaysthe concentration of ion can be 1～4g/L, the 5th end liquid main component: the content of zinc element can be 5.0～12.0wt%, and the content of ferro element can be 25～35wt%.
S1300: the second washing and filtering
According to embodiments of the invention, above the 5th obtained end liquid is carried out to the second washing and filtering, thereby can obtain scum and the second filtrate.With reference to figure 5, according to embodiments of the invention, the 5th obtained supernatant liquor and the second filtrate returning can be carried out to neutrality leaching processing.
Utilize the method for the system processing zinc roasted ore of the processing zinc roasted ore of the embodiment of the present invention to leach treatment process and can significantly improve scum slag rate using zinc roasted ore or oxygenant flue dust as the neutralizing agent of spray deironing treating processes by employing super acid, and significantly reduce plumbous silver-colored slag slag rate, in the plumbous silver-colored slag of gained, plumbous silver is of high grade, simultaneously, the method has adopted zinc hydrometallurgy hot acid leaching-Spraying Precipitator in Iron Removal, adhere to that liquid walks short circuit, material walk long distances, 2 reinforced, the feature of 3 acid addings, the comprehensive lead that reclaims, silver, copper, cadmium, cobalt, indium, the valuable metals such as bismuth, effectively improve the recovery utilization rate of valuable metal, in addition, the method is simple compared with other procedure, only by regulating the speed that adds of neutralizing agent (roasted ore) and iron-containing liquor, need not reduction process and add other additive, can realize scum and the effective of plumbous silver-colored slag separates, the scum obtaining can be delivered to the plumbous plumbous warm sludge of smelting of fuming furnace collocation of smelting and process together, the plumbous silver-colored slag of higher-grade obtaining send plumbous reduction furnace for smelting direct production lead bullion, realize plumbous zinc complementation, wet fire is compatible, the technique object of energy-saving and emission-reduction, open up new way for reducing zinc hydrometallurgy production cost, realize smelting waste slag innoxious, the object of resource utilization, promote the lifting of Business Economic Benefit.
With reference to figure 6, according to embodiments of the invention, the method for processing zinc roasted ore further comprises:
S1400: purifying treatment
According to embodiments of the invention, the first obtained supernatant liquor is carried out to purifying treatment.In this step, particularly, purifying treatment is in fact by adding zinc dust precipitation copper removal, cadmium, or adds Zinc dust Cementation for Cobalt Removal, nickel in the time that other additive (as antimonic salt) exists.Thus, can make the Cu in the first supernatant liquor by purifying treatment
2+, Cd
2+, Co
2+, Ni
2+deng impurity except within the permission content range of zinc electrolytic deposition process, guarantee the zinc metal sheet that normally carries out and produce better quality of electrolytic deposition process, simultaneously, by the inrichment of scavenging process, making has a valency associated element in raw material, as Cu, Cd, Co etc. obtain enrichment, and can obtain byproduct copper ore concentrates, Spongy Cadmium and cobalt concentrate through processing.Its main main chemical reactions equation is as follows:
CuSO
4+Zn=Cu↓+ZnSO
4
CdSO
4+Zn=Cd↓+ZnSO
4
CoSO
4+Zn=Co↓+ZnSO
4
NiSO
4+Zn=Ni↓+ZnSO
4
As mentioned above, the method for utilizing the system of the processing zinc roasted ore of the embodiment of the present invention to process zinc roasted ore can have and is selected from following advantage one of at least:
The method of utilizing the system of the processing zinc roasted ore of the embodiment of the present invention to process zinc roasted ore adheres to that liquid walks short circuit, material walk long distances, the feature of 2 reinforced, 3 acid addings, comprehensively reclaim the valuable metals such as lead, silver, copper, cadmium, cobalt, indium, bismuth, effectively improved the recovery utilization rate of valuable metal;
The method operation that utilizes the system of the processing zinc roasted ore of the embodiment of the present invention to process zinc roasted ore is controlled simple, and what only need to control neutralizing agent (roasted ore or zinc oxide fumes) and iron-containing liquor adds speed, temperature, pH value;
Utilize method that the system of the processing zinc roasted ore of the embodiment of the present invention processes zinc roasted ore without adding Na
+, NH
4 +the additives such as salt;
The method of utilizing the system of the processing zinc roasted ore of the embodiment of the present invention to process zinc roasted ore adopts low iron to sink iron, makes Fe
3+enter solution with injection mode;
Utilize method that the system of the processing zinc roasted ore of the embodiment of the present invention processes zinc roasted ore without reduction operation, lower concentration ferric iron directly generates goethite precipitation;
Utilize the system of the processing zinc roasted ore of the embodiment of the present invention to process the dust rate of method scum pyrogenic attack output of zinc roasted ore low, flue dust quality is good;
Utilize the system of the processing zinc roasted ore of the embodiment of the present invention to process method removing impurities (F, Cl, As, Sb, the Si etc.) ability of zinc roasted ore strong;
Utilize the system of the processing zinc roasted ore of the embodiment of the present invention to process the method equipment configuration of zinc roasted ore simple, without high pressure or specific installation;
Utilize the system of the processing zinc roasted ore of the embodiment of the present invention to process the plumbous silver of super acid leached mud (plumbous silver-colored slag) in the method for zinc roasted ore of high grade, plumbous as the refining of the direct Song Qian of byproduct smeltery.
Below with reference to specific embodiment, present invention is described, it should be noted that, these embodiment are only descriptive, and do not limit the present invention in any way.
Embodiment 1
Zinc roasting mineral phase composite table 1:
Table 1
| Composition | Zn | Cd | Pb | Cu | Fe | S | S SO4 | CaO | MgO | SiO 2 |
| Amount to/% | 52.38 | 0.22 | 1.71 | 0.57 | 15.6 | 0.4 | 1.31 | 0.91 | 0.68 | 3.42 |
| Composition | As | Ag | F | Cl | In | Ge | Co | Ni | ? | ? |
| Amount to/g/t | 7970 | 194 | 23.9 | 51.2 | 228 | 4.55 | 433 | 399 | ? | ? |
Get the 100kg zinc roasted ore of said components, it is processed, specifically comprise the following steps:
Under the terminal acidity that is 5.2 with pH after roasted ore is mixed with oxygenant and electrolytic solution, carry out neutrality and leach processing 2 hours at the temperature of 65 degrees Celsius, thereby can obtain neutral leach liquor; Obtained neutral leach liquor is carried out to the first dense processing, thereby can obtain respectively the first supernatant liquor and the first end liquid; Under the terminal acidity that is 2.0 with pH, the first obtained end liquid is carried out to neutralizing treatment 2 hours at the temperature of 70 degrees Celsius, thereby can obtain the solution through neutralizing treatment; The solution of obtained process neutralizing treatment is carried out to the second dense processing, thereby can obtain respectively the second supernatant liquor and the second end liquid; At the temperature of 95 degrees Celsius, process 2 hours for the second obtained end liquid being carried out under 60g/L condition to high Ore Leaching with terminal acidity, thereby can obtain the solution through high Ore Leaching processing; The solution of high process obtaining Ore Leaching processing is carried out to the 3rd dense processing, to obtain respectively the 3rd supernatant liquor and the 3rd end liquid; At the temperature of 95 degrees Celsius, be under 100g/L condition with terminal acidity, the 3rd obtained end liquid carried out to super acid and leach processing 2 hours, thereby can obtain leaching through super acid the solution of processing; The obtained solution that leaching is processed through super acid is carried out to the 4th dense processing, to obtain respectively the 4th supernatant liquor and the 4th end liquid; The 4th obtained end liquid is carried out to the first washing and filtering, thereby can obtain respectively plumbous silver-colored slag and the first filtrate, and return and carry out high Ore Leaching processing by the first obtained filtrate with the 4th supernatant liquor; Under the terminal acidity that is 4.0 with pH at the temperature of 90 degrees Celsius, utilize zinc roasted ore to spray deironing processing to the second supernatant liquor obtaining, thereby can obtain iron ore slurry; Obtained iron ore slurry is carried out to stage treatment, thereby can obtain respectively coarse sand and mixing solutions.And obtained coarse sand and the 3rd supernatant liquor are returned and carry out neutralizing treatment; Above obtained mixing solutions is carried out to the 5th dense processing, thereby can obtain respectively the 5th supernatant liquor and the 5th end liquid; Above the 5th obtained end liquid is carried out to the second washing and filtering, thereby can obtain scum and the second filtrate, and the 5th obtained supernatant liquor and the second filtrate returning are carried out to neutrality leaching processing.
The composition of the first supernatant liquor, scum and the plumbous silver-colored slag obtaining after processing by aforesaid method is in Table 2-4:
The first supernatant liquor composition is as following table 2:
Table 2
| Element | Zn | Cu | Cd | Co | Ni |
| Composition g/L | 130～140 | 0.47 | 0.28 | 0.04 | 0.037 |
Scum slag rate 46%, main component is as following table 3:
Table 3
| Composition | Zn | Pb | Cu | Fe | S is total | CaO | MgO | SiO 2 | Ag | In |
| Amount to/% | 10 | 1.34 | 0.29 | 30 | 2.57 | 0.72 | 0.16 | 3.35 | 0.0152 | 0.044 |
Plumbous silver-colored slag slag rate 12%, main component is as following table 4:
Table 4
| Composition | Zn | Pb | Cu | Fe | S is total | CaO | MgO | SiO 2 | Ag | In |
| Amount to/% | 5.0 | 11.4 | 0.76 | 12 | 15.0 | 5.77 | 0.68 | 19.47 | 0.1265 | 0.015 |
Embodiment 2
Get the 100kg zinc roasted ore of said components, it is processed, specifically comprise the following steps:
Under the terminal acidity that is 5.0 with pH after roasted ore is mixed with oxygenant and electrolytic solution, carry out neutrality and leach processing 2.5 hours at the temperature of 70 degrees Celsius, thereby can obtain neutral leach liquor; Obtained neutral leach liquor is carried out to the first dense processing, thereby can obtain respectively the first supernatant liquor and the first end liquid; Under the terminal acidity that is 1.5 with pH, the first obtained end liquid is carried out to neutralizing treatment 2 hours at the temperature of 65 degrees Celsius, thereby can obtain the solution through neutralizing treatment; The solution of obtained process neutralizing treatment is carried out to the second dense processing, thereby can obtain respectively the second supernatant liquor and the second end liquid; At the temperature of 95 degrees Celsius, process 4 hours for the second obtained end liquid being carried out under 55g/L condition to high Ore Leaching with terminal acidity, thereby can obtain the solution through high Ore Leaching processing; The solution of high process obtaining Ore Leaching processing is carried out to the 3rd dense processing, to obtain respectively the 3rd supernatant liquor and the 3rd end liquid; At the temperature of 95 degrees Celsius, be under 120g/L condition with terminal acidity, the 3rd obtained end liquid carried out to super acid and leach processing 4 hours, thereby can obtain leaching through super acid the solution of processing; The obtained solution that leaching is processed through super acid is carried out to the 4th dense processing, to obtain respectively the 4th supernatant liquor and the 4th end liquid; The 4th obtained end liquid is carried out to the first washing and filtering, thereby can obtain respectively plumbous silver-colored slag and the first filtrate, and return and carry out high Ore Leaching processing by the first obtained filtrate with the 4th supernatant liquor; Under the terminal acidity that is 3.8 with pH at the temperature of 90 degrees Celsius, utilize zinc oxide fumes to spray deironing processing to the second supernatant liquor obtaining, thereby can obtain iron ore slurry; Obtained iron ore slurry is carried out to stage treatment, thereby can obtain respectively coarse sand and mixing solutions.And obtained coarse sand and the 3rd supernatant liquor are returned and carry out neutralizing treatment; Above obtained mixing solutions is carried out to the 5th dense processing, thereby can obtain respectively the 5th supernatant liquor and the 5th end liquid; Above the 5th obtained end liquid is carried out to the second washing and filtering, thereby can obtain scum and the second filtrate, and the 5th obtained supernatant liquor and the second filtrate returning are carried out to neutrality leaching processing.
The composition of the first supernatant liquor, scum and the plumbous silver-colored slag obtaining after processing by aforesaid method is in Table 5-7:
The first supernatant liquor composition is as following table 5:
Table 5
| Element | Zn | Cu | Cd | Co | Ni |
| Composition g/L | 130～140 | 0.5 | 0.3 | 0.05 | 0.04 |
Scum slag rate 44%, main component is as following table 6:
Table 6
| Composition | Zn | Pb | Cu | Fe | S is total | CaO | MgO | SiO 2 | Ag | In |
| Amount to/% | 8 | 1.5 | 0.2 | 32 | 2.6 | 0.76 | 0.17 | 3.58 | 0.018 | 0.05 |
Plumbous silver-colored slag slag rate 10%, main component is as following table 7:
Table 7
| Composition | Zn | Pb | Cu | Fe | S is total | CaO | MgO | SiO 2 | Ag | In |
| Amount to/% | 4.5 | 15 | 0.76 | 10 | 15.2 | 5.77 | 0.68 | 19.48 | 0.15 | 0.015 |
Comparative example
Get the 100kg zinc roasted ore of said components, it is processed, specifically comprise the following steps:
Under the terminal acidity that is 5.2 with pH after roasted ore is mixed with oxygenant and electrolytic solution, carry out neutrality and leach processing 2 hours at the temperature of 65 degrees Celsius, thereby can obtain neutral leach liquor; Obtained neutral leach liquor is carried out to the first dense processing, thereby can obtain respectively the first supernatant liquor and the first end liquid; Under the terminal acidity that is 2.0 with pH, the first obtained end liquid is carried out to neutralizing treatment 2 hours at the temperature of 70 degrees Celsius, thereby can obtain the solution through neutralizing treatment; The solution of obtained process neutralizing treatment is carried out to the second dense processing, thereby can obtain respectively the second supernatant liquor and the second end liquid; At the temperature of 90 degrees Celsius, process 2 hours for the second obtained end liquid being carried out under 50g/L condition to high Ore Leaching with terminal acidity, thereby can obtain the solution through high Ore Leaching processing; The solution of high process obtaining Ore Leaching processing is carried out to the 3rd dense processing, to obtain respectively the 3rd supernatant liquor and the 3rd end liquid; The 3rd end liquid is carried out to the first washing and filtering, thereby can obtain respectively plumbous silver-colored slag and the first filtrate, and return and carry out high Ore Leaching processing by the first obtained filtrate with the 3rd supernatant liquor; Under the condition that is 3.5 with terminal acidity at the temperature of 90 degrees Celsius, utilize bicarbonate of ammonia and sodium bicarbonate to spray deironing processing to the second supernatant liquor obtaining, thereby can obtain iron ore slurry; Obtained iron ore slurry is carried out to stage treatment, thereby can obtain respectively coarse sand and mixing solutions; And obtained coarse sand and the second supernatant liquor are returned and carry out neutralizing treatment; Above obtained mixing solutions is carried out to the 4th dense processing, thereby can obtain respectively the 4th supernatant liquor and the 4th end liquid; Above the 4th obtained end liquid is carried out to the second washing and filtering, thereby can obtain scum and the second filtrate, and the 4th obtained supernatant liquor and the second filtrate returning are carried out to neutrality leaching processing.
The composition of the first supernatant liquor, scum and the plumbous silver-colored slag obtaining after processing by aforesaid method is in Table 8-10:
The first supernatant liquor composition is as following table 8:
Table 8
| Element | Zn | Cu | Cd | Co | Ni |
| Composition g/L | 130～140 | 0.4 | 0.2 | 0.02 | 0.02 |
Scum slag rate: 28%, main component is as following table 9:
Table 9
| Composition | Zn | Pb | Cu | Fe | S is total | CaO | MgO | SiO 2 | Ag | In |
| Amount to/% | 4.2 | 0.15 | 0.16 | 26 | 11.85 | 0.6 | 0.2 | 3.2 | 0.004 | 0.015 |
Plumbous silver-colored slag slag rate: 26%, main component is as following table 10:
Table 10
| Composition | Zn | Pb | Cu | Fe | S is total | CaO | MgO | SiO 2 | Ag | In |
| Amount to/% | 5.8 | 3.4 | 0.2 | 20 | 10.6 | 1.35 | 0.8 | 7.9 | 0.02 | 0.014 |
As can be seen here, the scum rate in embodiment 1-2 is high compared with comparative example, and plumbous silver-colored slag rate is low compared with comparative example, simultaneously without adding Na
+, NH
4 +the heavy chalybeate such as salt, and in plumbous silver-colored slag, plumbous silver is of high grade, can comprehensively reclaim the valuable metals such as lead, silver, copper, cadmium, cobalt, indium, bismuth, effectively improve valuable metal recovery utilization ratio, the plumbous silver-colored slag of higher-grade obtaining send plumbous reduction furnace for smelting direct production lead bullion, has realized the technique object of plumbous zinc complementation, wet fire compatibility, energy-saving and emission-reduction, has opened up new way for reducing zinc hydrometallurgy production cost, realize that smelting waste slag is innoxious, the object of resource utilization, promoted the lifting of Business Economic Benefit.
In the description of this specification sheets, the description of reference term " embodiment ", " some embodiment ", " example ", " concrete example " or " some examples " etc. means to be contained at least one embodiment of the present invention or example in conjunction with specific features, structure, material or the feature of this embodiment or example description.In this manual, the schematic statement of above-mentioned term is not necessarily referred to identical embodiment or example.And specific features, structure, material or the feature of description can be with suitable mode combination in any one or more embodiment or example.
Although illustrated and described embodiments of the invention above, be understandable that, above-described embodiment is exemplary, can not be interpreted as limitation of the present invention, those of ordinary skill in the art can change above-described embodiment within the scope of the invention in the situation that not departing from principle of the present invention and aim, modification, replacement and modification.
Claims (5)
1. a system of processing zinc roasted ore, is characterized in that, comprising:
Neutral leaching device, described neutral leaching device is for mixing zinc roasted ore and carrying out neutrality and leach processing with oxygenant and electrolytic solution;
The first dense device, described the first dense device is connected with described neutral leaching device, for the neutral leach liquor obtaining is carried out to the first dense processing, to obtain respectively the first supernatant liquor and the first end liquid;
Neutralizing treatment device, described neutralizing treatment device is connected with described the first dense device, for described the first end liquid obtaining is carried out to neutralizing treatment;
The second dense device, described the second dense device is connected with described neutralizing treatment device, carries out the second dense processing for the solution of the process neutralizing treatment to obtaining, to obtain respectively the second supernatant liquor and the second end liquid;
Peracid leaching device, described peracid leaching device is connected with described the second dense device, for described the second end liquid obtaining is carried out to high Ore Leaching processing;
The 3rd dense device, described the 3rd dense device is connected with described peracid leaching device, for the solution of the high Ore Leaching processing of the process obtaining is carried out to the 3rd dense processing, to obtain respectively the 3rd supernatant liquor and the 3rd end liquid;
Super acid leaching device, described super acid leaching device is connected with described the 3rd dense device, leaches processing for described the 3rd end liquid obtaining being carried out to super acid;
The 4th dense device, described the 4th dense device is connected with described super acid leaching device, carries out the 4th dense processing, to obtain respectively the 4th supernatant liquor and the 4th end liquid for the obtained solution that leaching is processed through super acid;
The first washing and filtering device, described the first washing and filtering device is connected with described the 4th dense device, for described the 4th end liquid obtaining is carried out to the first washing and filtering, to obtain respectively plumbous silver-colored slag and the first filtrate;
Spray deironing apparatus, described spray Chen Tie device is connected with described the second dense device, is suitable for utilizing zinc roasted ore and/or zinc oxide fumes to described the second supernatant liquor is sprayed to deironing processing, to obtain iron ore slurry;
Sorting equipment, described sorting equipment is connected with described spray deironing apparatus, for described iron ore slurry is carried out to stage treatment, to obtain respectively coarse sand and mixing solutions;
The 5th dense device, described the 5th dense device is connected with described sorting equipment, for described mixing solutions being carried out to the 5th dense processing, to obtain respectively the 5th supernatant liquor and the 5th end liquid; And
The second washing and filtering device, described the second washing and filtering device is connected with described the 5th dense device, carries out the second washing and filtering for described the 5th end liquid, to obtain scum and the second filtrate.
2. the system of processing zinc roasted ore according to claim 1, is characterized in that, further comprises:
Refining plant, described refining plant is connected with described the first dense device, for described the first supernatant liquor is carried out to purifying treatment.
3. the system of processing zinc roasted ore according to claim 1, it is characterized in that, described the 3rd dense device is connected with described neutralizing treatment device respectively with described sorting equipment, for described the 3rd supernatant liquor and described coarse sand are returned and carry out described neutralizing treatment.
4. the system of processing zinc roasted ore according to claim 1, it is characterized in that, described the 4th dense device is connected with described peracid leaching device respectively with described the first washing device, for described the 4th supernatant liquor and described the first filtrate returning are carried out to described high Ore Leaching processing.
5. the system of processing zinc roasted ore according to claim 1, it is characterized in that, described the 5th dense device is connected with described neutral leaching device respectively with described the second washing and filtering device, for described the 5th supernatant liquor and described the second filtrate returning are carried out to the described neutral processing of leaching.
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Application publication date: 20140702 |