CN114622101B - Mineral separation method for comprehensively leaching and recovering gold and silver from gold and silver ore with higher sulfur content - Google Patents
Mineral separation method for comprehensively leaching and recovering gold and silver from gold and silver ore with higher sulfur content Download PDFInfo
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- CN114622101B CN114622101B CN202210221510.6A CN202210221510A CN114622101B CN 114622101 B CN114622101 B CN 114622101B CN 202210221510 A CN202210221510 A CN 202210221510A CN 114622101 B CN114622101 B CN 114622101B
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- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 title claims abstract description 106
- 238000002386 leaching Methods 0.000 title claims abstract description 106
- 229910052737 gold Inorganic materials 0.000 title claims abstract description 104
- 239000010931 gold Substances 0.000 title claims abstract description 104
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 229910052709 silver Inorganic materials 0.000 title claims abstract description 66
- 239000004332 silver Substances 0.000 title claims abstract description 66
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 35
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 35
- 239000011593 sulfur Substances 0.000 title claims abstract description 35
- 229910052500 inorganic mineral Inorganic materials 0.000 title claims abstract description 11
- 239000011707 mineral Substances 0.000 title claims abstract description 11
- 238000000926 separation method Methods 0.000 title claims abstract description 8
- 239000002002 slurry Substances 0.000 claims abstract description 75
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 58
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 49
- 238000000034 method Methods 0.000 claims abstract description 40
- 238000001179 sorption measurement Methods 0.000 claims abstract description 36
- 238000005273 aeration Methods 0.000 claims abstract description 25
- 238000003795 desorption Methods 0.000 claims abstract description 21
- 239000012535 impurity Substances 0.000 claims abstract description 13
- 238000003756 stirring Methods 0.000 claims abstract description 10
- 238000000227 grinding Methods 0.000 claims abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims description 97
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 14
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 14
- 239000004571 lime Substances 0.000 claims description 14
- 238000010907 mechanical stirring Methods 0.000 claims description 7
- 239000012141 concentrate Substances 0.000 claims description 6
- MNWBNISUBARLIT-UHFFFAOYSA-N sodium cyanide Chemical compound [Na+].N#[C-] MNWBNISUBARLIT-UHFFFAOYSA-N 0.000 claims description 6
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 claims description 5
- 238000010494 dissociation reaction Methods 0.000 claims description 5
- 230000005593 dissociations Effects 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 5
- 230000008569 process Effects 0.000 abstract description 28
- 238000011084 recovery Methods 0.000 abstract description 26
- 238000005868 electrolysis reaction Methods 0.000 abstract description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 6
- 229910052760 oxygen Inorganic materials 0.000 abstract description 6
- 239000001301 oxygen Substances 0.000 abstract description 6
- 238000004062 sedimentation Methods 0.000 abstract description 4
- 238000004064 recycling Methods 0.000 abstract description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 12
- 230000009466 transformation Effects 0.000 description 7
- 230000000694 effects Effects 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- PQTCMBYFWMFIGM-UHFFFAOYSA-N gold silver Chemical compound [Ag].[Au] PQTCMBYFWMFIGM-UHFFFAOYSA-N 0.000 description 3
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- 159000000007 calcium salts Chemical class 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- XKGUKYPCHPHAJL-UHFFFAOYSA-N methanetetracarbonitrile Chemical compound N#CC(C#N)(C#N)C#N XKGUKYPCHPHAJL-UHFFFAOYSA-N 0.000 description 1
- 238000002715 modification method Methods 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- 238000005215 recombination Methods 0.000 description 1
- 230000006798 recombination Effects 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
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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
- C22B11/00—Obtaining noble metals
- C22B11/08—Obtaining noble metals by cyaniding
-
- 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
- C22B11/04—Obtaining noble metals by wet processes
-
- 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
- C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
- C22B3/24—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition by adsorption on solid substances, e.g. by extraction with solid resins
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Manufacturing & Machinery (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention relates to a mineral separation method for comprehensively leaching and recovering gold and silver from gold and silver ores with higher sulfur content, which comprises the following steps: grinding and classifying raw ore, wherein the obtained classified overflow ore pulp enters an aerated slurry returning device and a multi-stage series process mode two-stage alkaline leaching operation, the ore pulp after alkaline leaching enters an aerated slurry returning device and a multi-stage series process mode nine-stage leaching adsorption operation, the obtained gold-loaded carbon enters a impurity removing operation, the gold-loaded carbon enters a desorption electrolysis operation after impurity removal to obtain final electrolytic gold mud, and the leached tailings are final tailings. The method changes the original process flow on site into an aeration slurry returning device and a multistage series connection enhanced stirring leaching adsorption process mode, thereby solving the problems of insufficient dissolved oxygen rate of ore pulp, such as an ore pulp sedimentation tank, a carbon sedimentation tank and the like, and finally greatly improving the gold and silver recovery rate of gold and silver ores with higher sulfur content, reducing the gold and silver content in tailings and realizing comprehensive recycling of mine resources.
Description
Technical Field
The invention belongs to the technical field of mineral processing, relates to a mineral separation method for comprehensively leaching and recovering gold and silver from oxidized ores, and in particular relates to a mineral separation method for comprehensively leaching and recovering gold and silver from gold and silver ores with higher sulfur content.
Background
For gold resources, particularly large and extra large gold deposits, gold distribution is often represented by an upper gold-bearing oxidation zone, a lower gold-bearing sulphide zone, and a middle oxygen-sulphide contact transition zone. The part of ore belt ore has higher sulfur content, but the recovery index of gold and silver is not ideal by using the traditional cyanide carbon slurry process to recover or strengthen the leaching aid agent because of higher oxidation degree, and the recovery rate of gold and silver is only about 65 percent and 10 percent respectively.
Under the condition, in order to further remove sulfur and improve the recovery rate of gold and silver, a large amount of lime (conventionally, 6-8 kg/t of lime is generally added, and 25-30 kg/t of lime is added at present) is needed to remove sulfur and finally form calcium sulfate, but the viscosity of ore pulp is increased due to the formation of a large amount of calcium sulfate, and a colloid-like mud flow state is formed. The ore pulp is difficult to combine with various reaction factors well in the modes of simple mechanical stirring paddles, external aeration and the like, firstly, the content of dissolved oxygen used for reaction in the ore pulp is sharply reduced (from 6-8 mg/L to 3-5 mg/L), secondly, the added NaCN is difficult to diffuse on the surfaces of reaction minerals such as gold and silver quickly and uniformly, thirdly, the activated carbon can be calcified due to the fact that a large amount of calcium salt is adsorbed, and then the specific gravity is increased, and is deposited at the bottom of a leaching tank, the activated carbon cannot be well contacted with valuable metal gold and silver complex ions and the like in the ore pulp, so that the adsorption rate is reduced, the leaching liquid is passivated, and further leaching reaction is inhibited, so that the reaction enters into a dead space, namely, the colloid-like mud flow state formed by the ore pulp cannot normally carry out the reaction.
Particularly, the surface of the carbon-carrying carbon is adhered by a large amount of calcium salt in the subsequent process of the carbon slurry process, and the desorption and electrolysis operation of gold and silver cannot be normally carried out.
Therefore, how to comprehensively leach and recycle gold and silver from gold and silver ores with higher sulfur content is a difficult problem facing mine enterprises on the premise of ensuring technical indexes and economic indexes.
For recovering gold and silver from gold and silver ores with higher sulfur content, the most widely adopted process is to pretreat the ores to remove sulfur, and usually, an acidification oxidation-alkaline leaching pulp-carbon pulp recovery process or an oxidation roasting-alkaline leaching pulp-carbon pulp recovery process can be adopted. Although the pretreatment-carbon slurry process can improve the recovery rate of gold and silver operation, the method aims at the problems that the current factory selection and transformation workload is large, a strong acid or fire roasting process is introduced, the environmental impact is large, and the transformation work is not easy to develop. And the investment cost of the roasting process is high, the waste gas generated by roasting is required to be treated later, and the whole treatment process is complicated and complicated, so that the method is an urgent problem for mine enterprises. Therefore, the research has important significance on how to realize gold and silver recovery through an environment-friendly, efficient and simplest process modification method for the gold and silver ores with higher sulfur content.
Disclosure of Invention
The invention aims to provide an environment-friendly, efficient, simple and comprehensive beneficiation method for recovering gold and silver from gold and silver ores with high sulfur content in mines, wherein the recovery effect of gold and silver is poor, and a large amount of gold and silver is lost in tailings, so that the resources are lost and the benefits of the mines are damaged.
The invention mainly aims at the beneficiation method of high sulfur oxide ores, wherein the sulfur content is more than 4 percent, and the method is mainly distributed on the partial high sulfur ores of an oxygen sulfide contact ore zone or an oxidation ore zone of a gold and silver ore body, and comprises the following specific steps: 1) Ore is subjected to grinding and classifying operation, and ore pulp with dissociation degree of-200 meshes accounting for more than 90% is obtained.
2) The ore pulp obtained in the step 1) enters an alkaline leaching reaction tank according to the liquid-solid ratio of 3-4:1, alkaline leaching pretreatment operation is carried out under the condition of adding 25-30 kg/t lime, pretreated ore pulp is obtained, and more than 2 air-filled pulp returning devices are arranged on the alkaline leaching reaction tank; the inflatable slurry returning device is added in the alkaline leaching operation, so that the effect of a micro-channel reactor can be achieved, the stirring flow strength of ore pulp under the condition of high-dosage lime addition is ensured, the dissolved oxygen amount required by the reaction in the ore pulp is improved, and meanwhile, the smoothness of the subsequent leaching adsorption operation is ensured.
3) The pretreated ore pulp obtained in the step 2) enters a leaching adsorption reaction tank, leaching adsorption operation is carried out under the condition of adding 4-6 kg/t of NaCN and 18-24 g/L of activated carbon, and gold-loaded carbon and cyanide tailings are obtained; more than 2 aeration slurry returning devices are arranged on the leaching adsorption reaction tank; the aeration slurry returning device is added in the leaching adsorption operation, so that the effect of a micro-channel reactor can be formed, the stirring flow intensity of ore pulp is ensured, the dissolved oxygen amount required by the reaction in the ore pulp is improved, the problem of active carbon precipitation is solved, the flow and distribution of active carbon in the tank body are optimized, and the leaching rate of gold and silver and the adsorption rate of the active carbon to leaching liquid are ensured. The high-intensity stirring and high-dissolved oxygen reaction environment obtained by adding the aeration slurry returning device in the leaching operation is further improved in gold and silver leaching rate.
4) Adding 8-10 kg/t of NaCO into the impurity removal reaction tank of the gold-loaded carbon obtained in the step 3) 3 Performing carbon pretreatment and impurity removal operation to obtain clean gold-carrying carbon; the gold-loaded carbon increases impurity removal operation, and effectively removes CaSO adhered to the surface of the carbon 4 The desorption working surface is opened by the impurities, so that the blockage of a desorption column tank body and a pipeline is solved, and the desorption rate of the gold-loaded carbon is ensured.
5) The clean gold-loaded carbon obtained in the step 4) enters a desorption electrolytic tank for desorption to obtain electrolytic gold mud, and the lean carbon after desorption returns to a leaching adsorption operation tail tank to obtain the electrolytic gold mud as final concentrate;
the inflatable slurry returning device comprises a cavity, the lower end of the cavity is connected with the lower end of the reaction tank through a pipeline, the upper end of the cavity is provided with two pipelines, one pipeline is connected with the upper end of the reaction tank, and the other pipeline is connected with an external air pump; the external air pump provides compressed air with the air pressure above 0.2 Mpa. Mechanical stirring devices are arranged in the alkaline leaching reaction tank and the leaching adsorption reaction tank, namely motors are arranged on upper end covers of the alkaline leaching reaction tank and the leaching adsorption reaction tank, and stirring paddles are arranged on motor shafts extending into the reaction tank.
Further, 3-4 aeration slurry returning devices are respectively arranged on the alkaline leaching reaction tank and the leaching adsorption reaction tank, and the aeration slurry returning devices are uniformly distributed around the alkaline leaching reaction tank and the leaching adsorption reaction tank.
Further, more than 2 alkaline leaching reaction tanks and an inflatable slurry returning device in the step (2) are combined and then connected in series for alkaline leaching operation; in the step (3), more than 2 leaching adsorption reaction tanks and an aeration slurry returning device are combined and then connected in series for alkaline leaching operation; namely, the slurry outlet of the reaction tank of the upper stage is connected with the slurry inlet of the lower stage.
Further, in the step 1), the sulfur content in the gold-silver ore is more than 4%.
Further, preferably, in the step (2), the 2 alkaline leaching reaction tanks and the aeration slurry returning device are combined and then connected in series to perform alkaline leaching operation, that is, the slurry outlet of the reaction tank of the previous stage is connected with the slurry inlet of the next stage.
Further, preferably, in the step (3), the combination of the 9 leaching adsorption reaction tanks and the aerated slurry returning device is followed by alkaline leaching operation in a serial connection manner, that is, the slurry outlet of the reaction tank of the previous stage is connected with the slurry inlet of the next stage.
The beneficial effects are that: according to the invention, after grinding and grading are carried out on the gold and silver ore with higher sulfur content, the ore pulp is subjected to alkaline leaching pretreatment and cyanide leaching adsorption by adopting a process mode of an inflatable pulp returning device and multistage serial connection, and the gold and silver recovery rate is greatly improved on the premise of high efficiency and environmental protection by a mineral separation method of further recovering gold and silver through desorption electrolysis after carbon enrichment of gold and silver.
The aeration back slurry combination mode is that slurry (comprising ore pulp, lime, naCN and active carbon) is circularly conveyed to a reaction tank together through compressed air, so that the active carbon deposited at the bottom can be effectively contacted with air and ore pulp in a flowing way, recombination and further reaction of various materials in a circulating conveying pipe are realized, a micro-channel reaction system is formed, the problems that the viscosity of ore pulp is increased and the contact probability of reactants is low under the condition of excessive calcium sulfate can be effectively solved, and thus, good cyanide leaching operation of noble metals such as gold and silver can be realized. The compressed air is more than 0.2Mpa (greater than atmospheric pressure), the volume in the chamber is rapidly expanded, the pulp at the upper part of the chamber is pushed out, the pulp at the pulp inlet at the bottom of the chamber is continuously gushed out, and the pulp is continuously output from bottom to top after being mixed in the chamber under the condition of continuous input of the compressed air, so that a continuous process is formed.
In addition, the applicant also finds that after the operation of the air-filling back slurry combination mode, the viscosity of the ore slurry can be promoted to be reduced, the situation that the ore slurry in the reaction tank is reacted and rigidified due to excessive calcium sulfate is broken, the whole reaction starts to be active, and the point-to-surface driving effect is realized. Probably because the partial area reaction is carried out by the combination mode of the aeration back slurry, the viscosity of the ore slurry is promoted to be reduced, and reactants contact with the final whole materials to participate in the reaction, thereby realizing the point-to-surface diffusion effect.
The method changes the original process flow on site into an aeration slurry returning device and a multistage series connection enhanced stirring leaching adsorption process mode, thereby solving the problems of insufficient dissolved oxygen rate of ore pulp, such as an ore pulp sedimentation tank, a carbon sedimentation tank and the like, and finally greatly improving the gold and silver recovery rate of gold and silver ores with higher sulfur content, reducing the gold and silver content in tailings and realizing comprehensive recycling of mine resources.
The difference with the prior art is that:
(1) The obtained ore grinding graded product enters an inflatable pulping device and multistage series connection process mode for pretreatment, leaching and active carbon enrichment recovery; (2) The obtained activated carbon is further subjected to impurity removal operation to obtain clean gold-loaded carbon, and the clean gold-loaded carbon enters desorption electrolysis operation to obtain electrolytic gold-silver mud as final concentrate; (3) On the premise of not changing the grinding fineness and not increasing the ductility pretreatment process, the comprehensive improvement of the gold and silver recovery rate is realized by the means of process equipment transformation and process optimization, and huge profit is created for mines, so that the method is an environment-friendly beneficiation method for realizing comprehensive utilization of resources.
Drawings
FIG. 1 is a process flow diagram of the present invention;
FIG. 2 is a schematic structural diagram of the inflatable slurry returning device of the invention;
FIG. 3 is a schematic diagram showing the connection of the aerated slurry-back device and the reaction tank;
FIG. 4 is a schematic diagram of the multistage series connection of the aerated slurry-back device and the reaction tank of the present invention;
wherein, 1 a reaction tank; 2, a motor; 3, feeding a ore pipe; 4, a mineral discharging pipe; a 5 chamber; 6, a slurry outlet pipe; 7, a slurry returning pipe; 8, an air inlet pipe; 9 stirring paddles; a 10-ring; 11 struts.
Detailed Description
The following is a further detailed description of the present invention, taken in conjunction with the accompanying drawings and examples, which are given by way of illustration only and not as limitations on the practice of the invention.
The inflatable slurry returning device shown in fig. 2 comprises a chamber 5, wherein a slurry outlet pipe 6 is arranged at the lower end of the chamber 5 and is used for being connected with a slurry outlet at the lower end of the reaction tank 1; the upper end of the chamber 5 is provided with two pipelines, one pipeline is a slurry return pipe 7 and is used for being connected with the upper end of the reaction tank 1, and the other pipeline is an air inlet pipe 8 and is used for being connected with an external air pump.
Further, as shown in fig. 3, the reactor further comprises a reaction tank 1, wherein one side of the upper part of the reaction tank 1 is provided with a feeding pipe 3, the feeding pipe 3 stretches into the reaction tank 1, and the other side of the reaction tank 1 is provided with an overflow ore discharging pipe 4; the middle part of the reaction tank 1 is supported by a supporting rod 11 and provided with a ring 10, and a slurry return pipe 7 extends into the ring 10; the lower end of the chamber 5 is connected with a slurry outlet at the lower end of the reaction tank 1 through a slurry outlet pipe 6; the cavity 5 is connected with the upper end of the reaction tank 1 through a slurry return pipe 7, and the cavity 5 is connected with an external air pump through an air inlet pipe 8.
Further, a mechanical stirring device is arranged on the reaction tank 1.
Further, more than 1 aeration slurry returning devices are arranged around the reaction tank 1; according to the size of the reaction tank, 2, 3, 4 and more than one aeration slurry returning devices can be uniformly arranged. .
Further, the mechanical stirring device comprises a motor 2 and a stirring paddle 9, the motor 2 is arranged at the upper end of the reaction tank 1 through a frame, and the stirring paddle 9 is arranged on the output shaft of the motor extending into the reaction tank.
The mineral separation method for comprehensively leaching and recovering gold and silver from gold and silver ores with higher sulfur content as shown in fig. 1 comprises the following steps: 1) Grinding and classifying the ore to obtain ore pulp with dissociation degree of-200 meshes accounting for more than 90%; 2) The ore pulp obtained in the step 1) enters an alkaline leaching reaction tank according to the liquid-solid ratio of 3-4:1, alkaline leaching pretreatment operation is carried out under the condition of adding 25-30 kg/t lime, pretreated ore pulp is obtained, and more than 2 air-filled pulp returning devices are arranged on the alkaline leaching reaction tank; 3) The pretreated ore pulp obtained in the step 2) enters leaching adsorptionLeaching and adsorbing operation is carried out in a reaction tank under the condition of adding 4-6 kg/t of NaCN and 18-24 g/L of activated carbon to obtain gold-loaded carbon and cyanide tailings; more than 2 aeration slurry returning devices are arranged on the leaching adsorption reaction tank; 4) Adding 8-10 kg/t of NaCO into the impurity removal reaction tank of the gold-loaded carbon obtained in the step 3) 3 Performing carbon pretreatment and impurity removal operation to obtain clean gold-carrying carbon; 5) And (3) the clean gold-loaded carbon obtained in the step (4) enters a desorption electrolytic tank for desorption to obtain electrolytic gold mud, and the desorbed lean carbon returns to a leaching adsorption operation tail tank to obtain the electrolytic gold mud as final concentrate.
Further, 3-4 aeration slurry returning devices are respectively arranged on the alkaline leaching reaction tank and the leaching adsorption reaction tank.
Further, as shown in fig. 4, more than 2 alkaline leaching reaction tanks and an aeration slurry returning device in the step (2) are combined and then connected in series to perform alkaline leaching operation; in the step (3), more than 2 leaching adsorption reaction tanks and an aeration slurry returning device are combined and then connected in series for alkaline leaching operation; namely, the slurry outlet of the reaction tank of the upper stage is connected with the slurry inlet of the lower stage.
Further, in the step 1), the sulfur content in the gold-silver ore is more than 4%.
And (2) performing alkaline leaching operation in a mode of combining the 2 alkaline leaching reaction tanks and the inflatable slurry returning device and then connecting the two devices in series, namely connecting the slurry outlet of the reaction tank of the upper stage with the slurry inlet of the lower stage.
And (3) performing alkaline leaching operation in a mode of combining the 9 leaching adsorption reaction tanks and the gas-filled slurry returning device and then connecting the leaching adsorption reaction tanks and the gas-filled slurry returning device in series, namely connecting a slurry outlet of a reaction tank of the upper stage with a slurry inlet of the lower stage.
Further, an external air pump provides compressed air with the air pressure above 0.2 Mpa.
Example 1
The ore feeding is gold and silver ore with higher sulfur content in a certain region of Yunnan gold group, wherein the gold grade in the raw ore is 1.71g/t, the silver grade is 18.60g/t, the iron grade is 28.07%, the copper grade is 0.37% and the sulfur grade is 4.0%.
The ore is subjected to two-section one-circuit grinding classification operation to obtain the dissociation degree of-200 meshes accounting for 90 percent% or more pulp; the obtained liquid-solid ratio is 3:1, feeding ore pulp into an inflatable back-slurry device with lime addition amount of 26kg/t and carrying out two-stage alkaline leaching pretreatment operation in a multistage series process mode; the obtained pretreated ore pulp enters an aeration slurry returning device with the NaCN addition amount of 4kg/t and the carbon density of 18g/L and nine sections of leaching and adsorbing operation in a multi-stage series process mode; the obtained gold-loaded carbon enters NaCO 3 Impurity removal operation with the addition amount of 8 kg/t; the obtained clean gold-loaded carbon enters a desorption electrolysis operation to obtain electrolytic gold mud, and the lean carbon after desorption returns to a leaching adsorption operation tail tank; the obtained desorption electrolysis operation obtains electrolytic gold mud as final concentrate; finally, the electrolytic gold mud with the gold operation recovery rate of 85.59 percent and the silver operation recovery rate of 21.28 percent can be obtained.
The technology before transformation comprises the following steps: the two-stage alkaline leaching pretreatment operation is to add lime of 6-8 kg/t into an alkaline leaching tank, the bottom of the alkaline leaching tank is inflated, mechanical stirring is matched for sulfur removal, finally, gold and silver are recovered by a cyanidation carbon slurry process, and gold and silver recovery indexes are not ideal due to incomplete sulfur removal, and gold and silver recovery rates are only 75.56% and 10.15% respectively; more lime is required to be added for further complete sulfur removal, so that the viscosity of ore pulp is increased due to the formation of a large amount of calcium sulfate, the reaction is rigidified, and the reaction cannot be performed.
Compared with the prior process flow without transformation, the gold recovery rate is improved from the original 75.56 percent to 85.59 percent by 10.03 percent; the recovery rate of silver is improved from 10.15% to 21.28%, and 11.13%.
Example 2
The ore feeding is gold and silver ore with higher sulfur content in a certain region of Yunnan gold group, wherein the gold grade in the raw ore is 1.68g/t, the silver grade is 17.94g/t, the iron grade is 32.48%, the copper grade is 0.38%, and the sulfur grade is 5.16%.
Carrying out two-section one-circuit grinding classification operation on the ore to obtain ore pulp with dissociation degree of-200 meshes accounting for more than 90%; the obtained liquid-solid ratio is 4:1, feeding ore pulp into an aeration pulp returning device with lime addition of 28kg/t and a multistage series process mode two-stage alkaline leaching pretreatment operation; the obtained pretreated ore pulp enters an aeration slurry returning device with the NaCN addition amount of 6kg/t and the carbon density of 24g/L and nine sections of leaching adsorption in a multi-stage series process modePerforming operation; the obtained gold-loaded carbon enters NaCO 3 Impurity removal operation with the addition amount of 10 kg/t; the obtained clean gold-loaded carbon enters a desorption electrolysis operation to obtain electrolytic gold mud, and the lean carbon after desorption returns to a leaching adsorption operation tail tank; the obtained desorption electrolysis operation obtains electrolytic gold mud as final concentrate; finally, the electrolytic gold mud with the gold operation recovery rate of 82.63 percent and the silver operation recovery rate of 18.07 percent can be obtained.
The technology before transformation comprises the following steps: the two-stage alkaline leaching pretreatment operation is to add lime of 6-8 kg/t into an alkaline leaching tank, the bottom of the alkaline leaching tank is inflated, mechanical stirring is matched for sulfur removal, finally, gold and silver are recovered by a cyanidation carbon slurry process, and gold and silver recovery indexes are not ideal due to incomplete sulfur removal, and gold and silver recovery rates are only 73.31% and 11.56% respectively; more lime is required to be added for further complete sulfur removal, so that the viscosity of ore pulp is increased due to the formation of a large amount of calcium sulfate, the reaction is rigidified, and the reaction cannot be performed.
Compared with the prior process flow without transformation, the gold recovery rate is improved from the original 73.31 percent to 82.63 percent, and the gold recovery rate is improved by 9.32 percent; the recovery rate of silver is improved from 11.56% to 18.07%, and is improved by 6.51%.
Claims (4)
1. A mineral separation method for comprehensively leaching and recovering gold and silver from gold and silver ores with higher sulfur content is characterized by comprising the following steps:
1) Grinding and classifying the ore to obtain ore pulp with dissociation degree of-200 meshes accounting for more than 90%;
2) The ore pulp obtained in the step 1) enters an alkaline leaching reaction tank according to the liquid-solid ratio of 3-4:1, alkaline leaching pretreatment operation is carried out under the condition of adding 25-30 kg/t lime, pretreated ore pulp is obtained, and more than 2 air-filled pulp returning devices are arranged on the alkaline leaching reaction tank;
3) The pretreated ore pulp obtained in the step 2) enters a leaching adsorption reaction tank, leaching adsorption operation is carried out under the condition of adding 4-6 kg/t of NaCN and 18-24 g/L of activated carbon, and gold-loaded carbon and cyanide tailings are obtained; more than 2 aeration slurry returning devices are arranged on the leaching adsorption reaction tank;
4) Adding 8 of the gold-loaded carbon obtained in the step 3) into a impurity removal reaction tank10kg/t NaCO 3 Performing carbon pretreatment and impurity removal operation to obtain clean gold-carrying carbon;
5) The clean gold-loaded carbon obtained in the step 4) enters a desorption electrolytic tank for desorption to obtain electrolytic gold mud, and the lean carbon after desorption returns to a leaching adsorption operation tail tank to obtain the electrolytic gold mud as final concentrate;
the inflatable slurry returning device comprises a cavity, the lower end of the cavity is connected with the lower end of the reaction tank through a pipeline, the upper end of the cavity is provided with two pipelines, one pipeline is connected with the upper end of the reaction tank, and the other pipeline is connected with an external air pump; mechanical stirring devices are arranged in the alkaline leaching reaction tank and the leaching adsorption reaction tank, namely motors are arranged on upper end covers of the alkaline leaching reaction tank and the leaching adsorption reaction tank, and stirring paddles are arranged on motor shafts extending into the reaction tank;
3-4 aeration slurry returning devices are respectively arranged on the alkaline leaching reaction tank and the leaching adsorption reaction tank;
in the step (2), more than 2 alkaline leaching reaction tanks and an aeration slurry returning device are combined and then connected in series for alkaline leaching operation; in the step (3), more than 2 leaching adsorption reaction tanks and an aeration slurry returning device are combined and then connected in series for alkaline leaching operation; namely, the slurry outlet of the reaction tank of the upper stage is connected with the slurry inlet of the lower stage;
the external air pump provides compressed air with the air pressure above 0.2 MPa.
2. The beneficiation method for comprehensively leaching and recovering gold and silver from gold and silver ores with high sulfur content according to claim 1, wherein the sulfur content of the gold and silver ores in the step 1) is more than 4%.
3. The beneficiation method for comprehensively leaching and recovering gold and silver from gold and silver ores with higher sulfur content according to claim 1, wherein in the step (2), the alkaline leaching operation is performed in a mode of combining 2 alkaline leaching reaction tanks and an inflatable slurry returning device and then connecting the alkaline leaching reaction tanks in series, namely, the slurry outlet of the reaction tank of the upper stage is connected with the slurry inlet of the lower stage.
4. The beneficiation method for comprehensively leaching and recovering gold and silver from gold and silver ores with higher sulfur content according to claim 1, wherein 9 leaching adsorption reaction tanks and an inflatable slurry returning device in the step (3) are combined and then are connected in series for alkaline leaching operation, namely a slurry outlet of a reaction tank of the upper stage is connected with a slurry inlet of the lower stage.
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| AU3299002A (en) * | 2001-04-10 | 2002-10-17 | Grd Minproc Limited | Improved processing of precious metal-containing materials |
| JP2015214731A (en) * | 2014-05-12 | 2015-12-03 | 住友金属鉱山株式会社 | Gold recovery method |
| CN108728640A (en) * | 2018-06-12 | 2018-11-02 | 灵宝金源矿业股份有限公司 | A kind of recovery process of arsenic-containing sulphur-containing type Gold |
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|---|---|---|---|---|
| AU3299002A (en) * | 2001-04-10 | 2002-10-17 | Grd Minproc Limited | Improved processing of precious metal-containing materials |
| JP2015214731A (en) * | 2014-05-12 | 2015-12-03 | 住友金属鉱山株式会社 | Gold recovery method |
| CN108728640A (en) * | 2018-06-12 | 2018-11-02 | 灵宝金源矿业股份有限公司 | A kind of recovery process of arsenic-containing sulphur-containing type Gold |
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