CN101443466A - Process for recovery of antimony and metal values from antimony- and metal value-bearing materials - Google Patents
Process for recovery of antimony and metal values from antimony- and metal value-bearing materials Download PDFInfo
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- CN101443466A CN101443466A CNA2007800176651A CN200780017665A CN101443466A CN 101443466 A CN101443466 A CN 101443466A CN A2007800176651 A CNA2007800176651 A CN A2007800176651A CN 200780017665 A CN200780017665 A CN 200780017665A CN 101443466 A CN101443466 A CN 101443466A
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- antimony
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- valuable metal
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B30/00—Obtaining antimony, arsenic or bismuth
- C22B30/02—Obtaining antimony
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B11/00—Obtaining noble metals
- C22B11/08—Obtaining noble metals by cyaniding
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/12—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic alkaline solutions
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Abstract
A process for recovery of antimony and metal values from antimony- and metal value-bearing materials is provided. A coarse (typically >250-[mu]m) concentrate of the antimony- and metal value-bearing materials is provided. The coarse concentrate is then subjected to a process for selective recovery of antimony in the form of solid antimony or an antimony containing solution. A residue containing the remaining metal values is then subjected to suitable recovery processes to recover the remaining metal values.
Description
Technical field
The present invention relates to from the material that contains antimony and valuable metal (metal value) to reclaim the method for antimony and valuable metal, relate in particular to from the material that contains white antimony and contain that gold copper-base alloy is for example quartzy, reclaim the method for valuable antimony and gold pyrite and the arsenopyrite.
In addition, the invention still further relates to the method that from the mixture that contains valency metallic substance and gangue, reclaims valuable metal, wherein saidly contain the hardness that the valency hardness of metal materials is lower than described gangue, its difference of hardness makes the described valency metallic substance that contains have precedence over described gangue and grind.
Background technology
In traditional hydrometallurgical recovery valuable metal, before further reclaiming metal by leaching process, electrolytic deposition etc., usually the method by fragmentation, grinding and pneumatic flotation obtains high-grade concentrate.Usually, in production higher-grade concentrate, can cause the loss of valuable metal by grinding, cleaning and enrichment process, it depends on the mineralogy of concentrate.When a kind of valency metallic substance that contains contains valency metallic substance or gangue when soft than another kind, for example less than 2 mohrs units, such loss may be bigger because softer material may be ground undersized so that can not reclaim by conventional apparatus or equipment.
White antimony is a kind of stibium containing material, it is believed that it is a kind of soft mineral.But the white antimony association has the material that contains Jin Heyin, is considered to hard mineral with the material of its association, particularly quartz and pyrite.Many other valuable metals come from sulfide ore, for example pyrite and chalcopyrite.These sulfide ores also usually association precious metal is arranged, for example the gold and silver-colored.From the material of containing metal sulfide, particularly when this material also contains precious metal, reclaim any method of blended valuable metal, all need to consider first process of the interested underlying metal of selective recovery under the condition of second process of not damaging the selective recovery precious metal, vice versa.
The present invention attempts overcoming at least some shortcomings in the above-mentioned shortcoming.
Summary of the invention
According to an aspect of the present invention, provide a kind of method that from the material that contains antimony and valuable metal, reclaims antimony and valuable metal, said method comprising the steps of:
A) provide the described rough concentrate (coarse concentrate) that contains the material of antimony and valuable metal;
B) make described rough concentrate stand the process of selective recovery antimony, thereby obtain solid antimony or contain antimony solution and the residue that contains residual valuable metal; And
C) from described residue, reclaim described residual valuable metal.
In one embodiment of the invention, stibium containing material is white antimony, side's golden antimony ore (auro-stibnite), tetrahedrite or its combination.The suitable example of described stibium containing material includes but not limited to ore, concentrate or any other material that contains antimony-containing mineral.
Contain the valency metallic substance and be ore, concentrate or any can be from wherein reclaiming other material of valuable metal.In one embodiment, the described valency metallic substance that contains is to contain the metallic sulfide that one or more plant valuable metal.Preferably, the described valency metallic substance that contains is that association has and contains for example metallic sulfide of gold and/or silver-colored material of valency precious metal.It is pyrite, chalcopyrite and arsenopyrite that this class association has the exemplary of the metallic sulfide of gold and/or silver.
In general, rough concentrate is the coarse grain flotation concentrate.Available following steps prepare the rough concentrate incoming flow: will contain the material fragmentation and the grinding of antimony and valuable metal, and make the material that obtains stand floatation process.In one embodiment, described floatation process may further comprise the steps: coarse grained first floatation process that contains the material of antimony and valuable metal in order to collecting is set, and optional be provided with in order to scan the material that contains antimony and valuable metal than small grain size particulate second floatation process.
In one embodiment of the invention, the granularity of rough concentrate is greater than 125 μ m.Preferably, the granularity of rough concentrate is greater than 250 μ m.
In one embodiment of the invention, the process of selective recovery antimony comprises: with alkaline sulphide solution lixiviate rough concentrate, thereby obtain containing antimony solution and the residue that contains residual valuable metal, and the described antimony solution that contains is separated with described residue.Described method also comprises the step that contains the antimony electrolysis of solutions with isolated, to reclaim metallic antimony.
Usually, described alkaline sulphide solution contains 5-50g/L OH
-(g/L) and 50-400g/L S
2-Usually, described lixiviate is reflected under the room temperature to 105 ℃ and carries out 2-24h.
In one embodiment, before carrying out electrolysis, will contain the clarification of antimony solution and pass through the adsorption medium elution, to reclaim the dissolved valuable metal.Usually, pass through the adsorption medium elution, to reclaim dissolved precious metal, particularly gold through the clarifying antimony solution that contains.
In one embodiment, before carrying out electrolysis, the pH value that will contain antimony solution is adjusted to alkalescence.By being metered into caustic solution, the pH value of solution is raise.The exemplary of caustic solution comprises sodium hydroxide, potassium hydroxide or calcium hydroxide.
In one embodiment, electrolysis is that 3-4.5V and anodic current density are 600-800A/m at voltage
2With cathode current density be 250-600A/m
2Under carry out.Electrolysis continues 4-8h down at 40-60 ℃.
Advantageously, in one embodiment of the invention, the by product of electrolytic reaction is a sodium sulfate.
In one embodiment, the residue that contains residual valuable metal contains gold.The exemplary that remains in the form of the gold in the residue is the gold that discharges from the gold in the concentrate incoming flow, by step b) and the gold of arsenopyrite association from stibium containing material.Can from residue, reclaim gold by following steps: residue cyaniding and formation are contained golden lixiviate mother liquor (pregnant leach solution), carry out leaching process subsequently.The exemplary of leaching process comprises electrolysis, be adsorbed onto on carbon or the resin or by zinc being added to leach and make the gold precipitation in the mother liquor, for example carried out in Merrill Crowe method.Before cyaniding, can make residue through oxidated leaching process, so that gold discharges from arsenopyrite and other refractory mineral.
The present invention is also based on following beat all reality: can be by the low-grade rough concentrate incoming flow that contains the material that mixes valuable metal is provided, improve from than pulsus durus stone and contain the valency metal than the metal recovery the soft material, the granularity of the size ratio of wherein said low-grade rough concentrate incoming flow tradition concentrate incoming flow is big.This deviates from mutually with regular practice, because compare with the incoming flow of fine grinding higher-grade concentrate, handles the low-grade concentrate incoming flow of corase grind and will pay economic cost usually.
According to another aspect of the present invention, a kind of method that reclaims valuable metal from the mixture that contains valency metal soft material and gangue is provided, the hardness of the wherein said described gangue of hardness ratio that contains valency metal soft material is low, its difference of hardness makes the described valency metal soft material that contains have precedence over gangue and grind, and said method comprising the steps of:
A) provide and contain the described rough concentrate that contains valency metal soft material;
B) make described rough concentrate stand the process of selective recovery valuable metal, thus the containing metal solution and the residue of metal that obtains reclaiming or recovery.
In one embodiment of the invention, describedly contain difference of hardness between valency metal soft material and the gangue more than or equal to 2 mohrs units.
In another embodiment, the described hardness that contains valency metal soft material is more than 2 mohrs units.
In one embodiment, described residue contains one or more plants other valuable metal, and described method also comprise from residue reclaim described one or more plant the step of other valuable metal.
Description of drawings
Now only with reference to the accompanying drawings by the preferred embodiment of case description, wherein in conjunction with all aspects of the invention:
The schema of an embodiment of schema 1 expression the inventive method;
Fig. 1 is the X-ray diffraction analysis figure of the rough concentrate described in the embodiment 1; And
Fig. 2 carries out the X-ray diffraction analysis figure of residue residual after the lixiviate with alkaline sulphide solution described in the embodiment 1 to rough concentrate.
The schema of this embodiment of the present invention is based on Hillgrove Mine, the auriferous arsenopyrite ore deposit of New SouthWales, the pilot-plant test of white antimony ore.Should be understood that in this example white antimony is a stibium containing material, and the auriferous arsenopyrite ore deposit is for containing the valency metallic substance.In addition, it should be understood that white antimony is the soft material that contains the valency metal for the example of second aspect present invention is provided, and the auriferous arsenopyrite ore deposit is the material that contains second valuable metal.Gangue is a rock mass.
The detailed description of the preferred embodiment for the present invention
Before describing the preferred embodiments of the invention, should be understood that to the invention is not restricted to described particular device that these equipment can change.Should also be understood that term used herein only is for describing the purpose of particular, is not to be intended to limit the scope of the invention by any way.Must be noted that, as used in this article, do not have when numeral-classifier compound is modified and also comprise plural form, unless spell out in addition in the literary composition.Unless otherwise defined, all the implication with those skilled in the art's common sense is identical for the implication of all scientific and technical terminologies used herein.
Reference flowchart Fig. 1, all respects according to an embodiment of the invention, the material that contains antimony and valuable metal that is provided for processing.The material that contains antimony and valuable metal can be ore, concentrate or any can be from wherein reclaiming for example other material of gold and silver and tungsten of antimony and other valuable metal, particularly precious metal.
Stibium containing material can be white antimony, the golden antimony ore in side, tetrahedrite or its combination.Scheme as an alternative, stibium containing material can be contain antimony contain the valency metallic substance.
Native state usually is dispersed in the quartz particles, and normal and metallic sulfide ores is pyrite (FeS for example
2), chalcopyrite, lead glance, white antimony and arsenopyrite occur together.Therefore, the preferred embodiments of the invention are particularly advantageous aspect recovery antimony and precious metal from blended gold/antimony/arsenic minerals stone or concentrate are for example golden.
Therefore, the material that contains antimony and valuable metal is preferably antimony/gold/metallic sulfide mixed ore.Usually, antimony/gold/metallic sulfide mixed ore is auriferous white antimony-arsenopyrite-pyrite ore.Usually, the relative hardness difference of each is very big in these mineral.The hardness of white antimony is 2 mohrs units, and the hardness of arsenopyrite is 3 1/2-6 mohrs units, and pyritous hardness is 6 mohrs units, and quartzy hardness is 7 mohrs units.
The material that contains antimony and valuable metal stands pulverizing, flotation, mixing and/or pulp and chemistry and/or physics conditioning, to obtain rough concentrate.Different with the technology of traditional preparation concentrate, the granularity of rough concentrate of the present invention is greater than 125 μ m.Preferably, the stibium containing material and the granularity of rough concentrate that contains the valency metallic substance are greater than 250 μ m.Favourable characteristics of the present invention are, can adopt traditional sulphide flotation means, and need be by other grinding and cleaning course.
In preferred embodiments, antimony/gold/metallic sulfide mixed ore is handled by fragmentation/grinding/flotation circuit usually, with obtain containing charging level antimony greater than 15%, greater than the charging level gold of 35g/t and optional concentrate greater than 4% charging level arsenic.
Before being transported to shredder, make the material that contains antimony and valuable metal carry out primary fragmentation.With regard to the treatment capacity of primary fragmentation, any suitable crusher all can be used for the material that fragmentation contains antimony and valuable metal, comprises jaw crusher, high pressure mixing roll, roller crusher or gyratory crusher.
The material that contains antimony and valuable metal with fragmentation is delivered to shredder from crusher then.The representative instance of shredder is that runner milling, rod mill, ball mill, autogenous mill or half are from (SAG) grinding machine.The material that contains antimony and valuable metal through grinding is sieved under 3-4mm, and minus mesh enters the gravity concentrate loop, and oversize enters shredder.Scheme as an alternative, the material that contains antimony and valuable metal through grinding can enter and carry out grain-by-grain seed selection in the cyclonic separator.
Then with granularity less than the materials conveyance that contains antimony and valuable metal of 3-4mm through grinding to the gravity treatment loop that comprises synergy gravity concentrator and scalping cyclonic separator.The concentrate that forms in synergy gravity concentrator loop enters the concentrate incoming flow of combination, further to handle in alkaline sulfides lixiviate groove.Usually, granularity of concentrate p80 is 150-600 μ m.
The gravity tailings of synergy gravity concentrator is sent into the scalping cyclonic separator, herein cyclone underflow (greater than the coarse particles of 250 μ m) is sent into the rough floatation groove, and cyclonic separator top stream (less than the fine particle of 250 μ m) is sent into scavenger flotation cell.
Before carrying out flotation, for the concentrate incoming flow is provided, according to the imagination requirement of the material that contains antimony and valuable metal, randomly nurse one's health the material that contains antimony and valuable metal, to improve the whole validity and the efficient of process operation through grinding with known suitable amendment.For example, be that the lead nitrate of 250-2500g/t or copper sulfate, dosage are xanthate collector and pore forming material conditioning blended side gold antimony ore-arsenopyrite-pyrite of 30-250g/t with dosage.Usually, will nurse one's health 1-5 minute through the material that contains antimony and valuable metal that grinds.
In preferred embodiments, with lead nitrate (500-1000g/t), PAX collecting agent (80-120g/t) blended side's gold antimony ore-arsenopyrite-pyrite was nursed one's health 2-4 minute.
The crude mineral (greater than 250 μ m) that the rough floatation groove discharges in order to collecting is set, be mainly contain antimony and valuable metal than soft material, for example white antimony is used for the mineral grain less than 250 μ m that collecting discharges and scavenger flotation cell is set.In preferred embodiments, the resistates of the gold of residual white antimony of the main collecting of scavenger flotation cell and arsenopyrite concentrate form.
The rough floatation groove is operated as the coarse grain flotation cell, and flotation time is about 2-20 minute, depends on the mineralogy of concentrate.Rough floatation groove mine tailing enters shredder with regrinding.Through the blended side of conditioning gold antimony ore-arsenopyrite-pyrite, flotation time is generally 10-15 minute for as mentioned above.
Then, send into be used to carry out the lixiviate reactor of alkaline sulfides leaching process before, will in antimony lixiviate feed hopper, merge from the concentrate and the gravity concentrate of each flotation cell, obtain the concentrate incoming flow of about 5-15% feed material.
Make rough concentrate carry out lixiviate conditioning then, with the antimony of the form of selective recovery lixiviate mother liquor with contain the solid residue of residual valuable metal.Can from described lixiviate mother liquor, reclaim metallic antimony by electrolysis, and the available appropriate technology residual valuable metal of selective recovery from described solid residue that is suitable for valuable metal.For example, contain at solid residue under the situation of gold, can solid residue be carried out cyaniding according to the technology of knowing.
The alkaline sulfides leaching process carries out 2-24h at about 25 ℃ under normal pressure to about 105 ℃ temperature in the lixiviate container.Extracting solution contains 5-50g/L OH
-With 50-400g/L S
2-In preferred embodiments, extracting solution contains 10-20g/L OH
-With 50-150g/L S
2-, the alkaline sulfides leaching process carries out 6-8h under 95-105 ℃.
According to following reaction with alkaline sulfides lixiviate antimony sulfide:
3Na
2S+Sb
2S
3(white antimony) → 2Na
3SbS
3(1)
3Na
2S+4Cu
2SSb
2S
3(tetrahedrite) → 4Cu
2S+2Na
3SbS
3(2)
In the alkaline sulfides leaching process, antimony is dissolving fully basically, forms stibiated lixiviate mother liquor.Usually, the antimony greater than 99% in the rough concentrate incoming flow is dipped in the lixiviate mother liquor.
Before from the lixiviate mother liquor, reclaiming antimony, the lixiviate mother liquor is filtered and clarification.Usually from the lixiviate mother liquor, reclaim antimony according to following reaction by electrolysis:
4Na
3SbS
3+12NaOH→4Sb↓+12Na
2S+6H
2O+3O
2 (3)
Electrolysis is that 3-4.5V and anodic current density are 600-800A/m at voltage under 40-60 ℃
2With cathode current density be 250-600A/m
2Under carry out 4-8h.
In some cases, according to the mineral composition of concentrate incoming flow, other valuable metal for example the gold and arsenic may be partially dissolved in the lixiviate mother liquor.Imagination can reclaim other valuable metal by method and the technology of knowing from the lixiviate mother liquor.For example, be under the situation of gold at the dissolved valuable metal, from the lixiviate mother liquor, reclaim the dissolved gold by the adsorption medium elution usually.
Be included in valuable metal in the concentrate incoming flow, particularly have the valency precious metal for example gold stay usually in the solid residue that forms in the alkaline sulfides lixiviate step.Imagination can reclaim valuable metal by method and the technology of knowing from solid residue.For example by pulp again and with cyanide process, carbon slurry method (carbon-in-pulp, CIP), elution, electrolysis and smelting process handle slurry and reclaim any valency gold that has from solid residue.
If other valuable metal is present in the residue with economically feasible amount, the also available subsequently technology of knowing reclaims.For example, in schema 1, tungsten reclaims from golden lixiviate flotation tailings as tungsten concentrate.
Refer now to following examples and further describe embodiment preferred of the present invention.Processing condition and parameter are intended to illustrate all respects of the present invention as mentioned herein, but not are intended to limit the present invention's scope required for protection.
Embodiment
The material that contains antimony and valuable metal of embodiment is on average containing white antimony-arsenopyrite-pyrite ore of 1%Sb, 0.8%As and 4g/tAu.
Primary fragmentation is carried out in antimony/golden sulfide mixing ore deposit, obtain the particle of granularity less than 10cm, the turnout of 24h is about 1000t.By loading machine the ore of fragmentation is delivered to the shredder (initial flow is 30t/h) that is used to grind then, and sends into the rough segmentation cyclonic separator.Cyclone overflow (about 250 μ m) enters the rough floatation groove, and the dirty flash flotation groove that enters of cyclonic separator, to reclaim the mineral of very thick (250 μ m to 6-7mm).
Clean in the cleaner flotation groove than rough concentrate, concentrate and the flash flotation concentrate with cleaning merges then, and sends into centrifugal separator or gravity concentrator, to reclaim free gold.
Usually contain 17.25% Sb, 2.75% As and 1.01o/t Au or higher concentrate incoming flow by the preparation of above-mentioned loop.
The rough floatation groove is set in order to the thick free mineral acidity of collecting (greater than 250 μ m), is mainly the white antimony block.Rough floatation groove PbNO
3(500g/t), PAX collecting agent (50g/t) and pore forming material (IF50) move about 3 minutes conditioning time under pH neutral, flotation time is about 1 minute.Roughly select/flash tails report turns back in the shredder and grinds.
Then the gravity concentrate mine tailing is sent into antimony lixiviate feed hopper, there they are merged and sedimentation, before sending into antimony lixiviate reactor, to form the concentrate incoming flow.
With alkaline sulphide solution (10g/L OH
-, 50g/L S
2-) (slurry solid content=100g/L) is handled 8h, makes total amount reduce 23.7%, and the residue analysis result is 0.05%Sb, 2.63%As, 0.76o/t Au and 7.93% S altogether with the concentrate incoming flow under 100 ℃.
Carry out X-ray diffraction analysis to the concentrate incoming flow with by the residue that the alkaline sulfides leaching process obtains, the results are shown in Fig. 1 and 2, confirm that white antimony and silicon-dioxide are the principal phase of concentrate incoming flow, and residue contains silicon-dioxide and aluminum oxide as principal phase.
The pulp separation of leaving antimony lixiviate reactor is become solid ingredient and liquid ingredient, to be used for downstream processing.Solid residue (or filter cake) contains the most valency gold that has, and it is sent into cyanidation circuit, be used for pulp again and reclaim gold, and the liquid portion of slurry (or filtrate flow) contains valency antimony is arranged, and it is sent into the undivided cell with mild steel anode and negative electrode as the lixiviate mother liquor.The lixiviate mother liquor contains 17g/L Sb, 25g/L OH
-With 55g/L S
Solvable
By applying 600A/m
2Cathode current density, 800A/m
2Anodic current density and the bath voltage of 3.4V, metallic antimony is deposited on the negative electrode of undivided cell.Electrolytic process carries out 2h under 50 ℃, faraday current efficiency is 64%.
With isolating solid residue or filter cake pulp and pulp more again after the alkaline sulfides leaching process.Before sending into lixiviate and adsorption stage, the pH value of the cyanidation circuit feed stream of pulp again is adjusted to about 10.5.Sodium cyanide solution is metered into, to help that gold is extracted the solution phase mutually from solid.
Then, according to of the gold-containing solution electrolysis of known technology, to reclaim the valuable metal gold with lixiviate.
In this embodiment, selective leaching proposes to surpass 99.5% antimony and 29% As, 42% Au and 47% S from the concentrate charging.
May not constitute the part that any data of admitting wherein forms general knowledge known in this field in Australia or any other such reference of country with reference to the application and the publication of prior art though should be understood that this paper.
For the purpose of this specification sheets and claims, should be expressly understood that word " comprises " and refers to that " including but not limited to ", word " comprise " and have corresponding implication.
Do not deviating under the situation that the present invention conceives substantially, except those schemes of having described, various equivalent modifications can be expected many variations and change.Think all these variations and change all within the scope of the invention, essence of the present invention is determined by foregoing description.
Claims (28)
1. method that reclaims antimony and valuable metal from the material that contains antimony and valuable metal said method comprising the steps of:
(a) provide the described rough concentrate that contains the material of antimony and valuable metal;
(b) make described rough concentrate stand the process of selective recovery antimony, thereby obtain solid antimony or contain antimony solution and the residue that contains residual valuable metal; And
(c) from described residue, reclaim described residual valuable metal.
2. according to the process of claim 1 wherein that described stibium containing material is white antimony, the golden antimony ore in side, tetrahedrite or its combination.
3. according to the method for claim 1 or 2, wherein said contain the valency metallic substance be ore, concentrate or any can be from wherein reclaiming other material of valuable metal.
4. according to each method in the aforementioned claim, the wherein said valency metallic substance that contains is to contain the metallic sulfide that one or more plant valuable metals.
5. according to the method for claim 4, the wherein said valency metallic substance that contains is that association has the metallic sulfide that contains the valency precious metal material.
6. according to the method for claim 5, wherein the described metallic sulfide of gold and/or silver is arranged is pyrite, chalcopyrite and arsenopyrite in association.
7. according to each method in the aforementioned claim, wherein said rough concentrate prepares by following steps: with described material fragmentation and the grinding that contains antimony and valuable metal, and make the gained material stand floatation process.
8. according to the method for claim 7, wherein said floatation process comprises: be provided with in order to collecting and contain coarse grained first floatation process that the material of antimony and valuable metal discharges, and optional setting is in order to scan second floatation process of the material that contains antimony and valuable metal.
9. according to each method in the aforementioned claim, wherein said rough concentrate contains the charging level antimony greater than 15%.
10. according to each method in the aforementioned claim, the granularity of wherein said rough concentrate is greater than 125 μ m.
11. according to each method in the aforementioned claim, the process of wherein said selective recovery antimony comprises: with the described rough concentrate of alkaline sulphide solution lixiviate, thereby the residue that obtains containing antimony solution and contain residual valuable metal, and the described antimony solution that contains separated with described residue.
12. according to the method for claim 11, wherein said alkaline sulphide solution contains 5-50g/LOH-(g/L) and 50-400g/L S
2-
13. according to the method for claim 11 or 12, wherein said lixiviate is reflected under the room temperature to 105 ℃ carries out 2-24h.
14. according to each method among the claim 11-13, it also comprises and contains the antimony electrolysis of solutions to reclaim the step of metallic antimony with isolated.
15., wherein before carrying out electrolysis, contain the clarification of antimony solution and pass through the adsorption medium elution described, to reclaim the dissolved valuable metal according to the method for claim 14.
16. according to the method for claim 15, the wherein said clarifying antimony solution that contains is by described adsorption medium elution, to reclaim the dissolved precious metal.
17., wherein before carrying out electrolysis, the described pH value that contains antimony solution is adjusted to the alkaline pH value according to the method for claim 14.
18., wherein the described pH value that contains antimony solution is raise by adding caustic solution according to the method for claim 17.
19. according to each method among the claim 14-18, described electrolysis is carried out under the anodic current density condition higher than negative electrode.
20. according to each method among the claim 14-19, wherein said electrolysis is that 3-4.5V and anodic current density are 600-800A/m at voltage
2With cathode current density be 250-600A/m
2Under carry out.
21. according to each method in the aforementioned claim, the wherein said residue that contains residual valuable metal contains gold.
22., wherein from described residue, reclaim gold: make described residue stand cyaniding and form to contain golden lixiviate mother liquor, carry out leaching process subsequently by following steps according to the method for claim 21.
23. according to the method for claim 22, wherein said leaching process is selected from electrolysis, be adsorbed onto on carbon or the resin or by zinc is added to and make gold precipitation, MerrillCrowe method in the described lixiviate mother liquor.
24. according to the method for claim 22, wherein before cyaniding, can make described residue, from arsenopyrite and other refractory mineral, to discharge gold through oxidated leaching process.
25. method that from the mixture that contains valency metal soft material and gangue, reclaims valuable metal, the wherein said hardness that contains valency metal soft material is lower than the hardness of described gangue, difference of hardness makes the described valency metal soft material that contains have precedence over gangue and grind, and said method comprising the steps of:
A) provide and comprise the described rough concentrate that contains valency metal soft material;
B) make described rough concentrate stand the process of selective recovery valuable metal, thus the containing metal solution and the residue of metal that obtains reclaiming or recovery.
26., wherein saidly contain difference of hardness between valency metal soft material and the described gangue more than or equal to 2 mohrs units according to the method for claim 25.
27. according to the method for claim 25, the wherein said hardness that contains valency metal soft material is below 2 mohrs units.
28. according to each method among the claim 25-27, wherein said residue also contains one or more plants other valuable metal, described method also comprise from described residue, reclaim described one or more plant the step of other valuable metal.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AU2006901878A AU2006901878A0 (en) | 2006-04-11 | Process for recovery of antimony and metal values from antimony - and metal value-bearing materials | |
| AU2006901878 | 2006-04-11 |
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| Publication Number | Publication Date |
|---|---|
| CN101443466A true CN101443466A (en) | 2009-05-27 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2007800176651A Pending CN101443466A (en) | 2006-04-11 | 2007-04-11 | Process for recovery of antimony and metal values from antimony- and metal value-bearing materials |
Country Status (7)
| Country | Link |
|---|---|
| CN (1) | CN101443466A (en) |
| AU (1) | AU2007236559A1 (en) |
| CA (1) | CA2648951A1 (en) |
| EA (1) | EA200870420A1 (en) |
| MX (1) | MX2008013141A (en) |
| WO (1) | WO2007115377A1 (en) |
| ZA (1) | ZA200808628B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU2009101298B4 (en) * | 2009-12-16 | 2010-02-11 | Rohan Bose | Process for recovering gold otherwise lost to the antimony bearing PLS from alkaline leaching of aurostibnite ores |
| CN101851705B (en) * | 2010-06-11 | 2011-07-20 | 湖南省桃江县板溪锑品矿冶厂 | Antimony impurity smelting method and reverberatory furnace for smelting |
| AR100110A1 (en) | 2014-01-31 | 2016-09-14 | Goldcorp Inc | PROCESS FOR THE SEPARATION AND RECOVERY OF METAL SULFURES OF A LESS OR CONCENTRATE OF MIXED SULFURS |
| RU2682365C1 (en) * | 2018-04-10 | 2019-03-19 | Федеральное государственное автономное образовательное учреждение высшего образования "Уральский федеральный университет имени первого Президента России Б.Н. Ельцина" | Antimony-containing raw materials processing method |
| CN114015897B (en) * | 2021-11-10 | 2022-09-27 | 中南大学 | Method for extracting antimony and gold from antimony-gold concentrate |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SE390545B (en) * | 1975-05-07 | 1976-12-27 | Boliden Ab | PROCEDURE FOR ELECTROLYTICAL EXTRACTION OF ONE OR MORE OF THE SUBSTANCES ANTIMON, MERCURY, ARSENIC AND TINN |
| US4051220A (en) * | 1976-03-01 | 1977-09-27 | Equity Mining Corporation | Sodium sulfide leach process |
| GB2004302B (en) * | 1977-09-13 | 1982-05-26 | Smith J | Electrowinning of metals from sulphide ores and products obtained therefrom |
| EP1078107B1 (en) * | 1998-04-22 | 2003-03-19 | Anglo American Research Laboratories (Proprietary) Limited | Ore comminution process using bed-compression method at low pressures and installation therefor |
| US6319389B1 (en) * | 1999-11-24 | 2001-11-20 | Hydromet Systems, L.L.C. | Recovery of copper values from copper ores |
| AUPR437601A0 (en) * | 2001-04-12 | 2001-05-17 | Wmc Resources Limited | Process for sulphide concentration |
| WO2006024886A1 (en) * | 2004-08-31 | 2006-03-09 | Anglo Operations Limited | Method for processing a value bearing feed material |
-
2007
- 2007-04-11 CN CNA2007800176651A patent/CN101443466A/en active Pending
- 2007-04-11 MX MX2008013141A patent/MX2008013141A/en unknown
- 2007-04-11 EA EA200870420A patent/EA200870420A1/en unknown
- 2007-04-11 WO PCT/AU2007/000478 patent/WO2007115377A1/en active Application Filing
- 2007-04-11 CA CA 2648951 patent/CA2648951A1/en not_active Abandoned
- 2007-04-11 AU AU2007236559A patent/AU2007236559A1/en not_active Abandoned
-
2008
- 2008-10-09 ZA ZA200808628A patent/ZA200808628B/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| AU2007236559A1 (en) | 2007-10-18 |
| ZA200808628B (en) | 2010-01-27 |
| EA200870420A1 (en) | 2009-08-28 |
| CA2648951A1 (en) | 2007-10-18 |
| WO2007115377A1 (en) | 2007-10-18 |
| MX2008013141A (en) | 2009-03-02 |
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Open date: 20090527 |