CN112251614A - Method for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate - Google Patents
Method for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate Download PDFInfo
- Publication number
- CN112251614A CN112251614A CN202011292284.8A CN202011292284A CN112251614A CN 112251614 A CN112251614 A CN 112251614A CN 202011292284 A CN202011292284 A CN 202011292284A CN 112251614 A CN112251614 A CN 112251614A
- Authority
- CN
- China
- Prior art keywords
- leaching
- silver
- gold
- carbon
- tank
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 229910052737 gold Inorganic materials 0.000 title claims abstract description 162
- 239000010931 gold Substances 0.000 title claims abstract description 162
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 title claims abstract description 142
- 229910052709 silver Inorganic materials 0.000 title claims abstract description 131
- 239000004332 silver Substances 0.000 title claims abstract description 131
- 238000000034 method Methods 0.000 title claims abstract description 41
- 239000012141 concentrate Substances 0.000 title claims abstract description 40
- PGWMQVQLSMAHHO-UHFFFAOYSA-N sulfanylidenesilver Chemical compound [Ag]=S PGWMQVQLSMAHHO-UHFFFAOYSA-N 0.000 title claims abstract description 19
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 390
- 238000002386 leaching Methods 0.000 claims abstract description 205
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 126
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims abstract description 109
- 238000001179 sorption measurement Methods 0.000 claims abstract description 105
- 238000003756 stirring Methods 0.000 claims abstract description 55
- 239000003153 chemical reaction reagent Substances 0.000 claims abstract description 41
- 239000000203 mixture Substances 0.000 claims abstract description 32
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 31
- 239000011593 sulfur Substances 0.000 claims abstract description 31
- 238000002156 mixing Methods 0.000 claims abstract description 29
- 238000000926 separation method Methods 0.000 claims abstract description 29
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 claims abstract description 26
- 229910052683 pyrite Inorganic materials 0.000 claims abstract description 26
- 239000011028 pyrite Substances 0.000 claims abstract description 26
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 24
- KXZJHVJKXJLBKO-UHFFFAOYSA-N chembl1408157 Chemical compound N=1C2=CC=CC=C2C(C(=O)O)=CC=1C1=CC=C(O)C=C1 KXZJHVJKXJLBKO-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000002161 passivation Methods 0.000 claims abstract description 17
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims abstract description 16
- 235000011941 Tilia x europaea Nutrition 0.000 claims abstract description 16
- 238000003795 desorption Methods 0.000 claims abstract description 16
- 239000004571 lime Substances 0.000 claims abstract description 16
- 239000000126 substance Substances 0.000 claims abstract description 10
- 239000007800 oxidant agent Substances 0.000 claims abstract description 9
- 230000001590 oxidative effect Effects 0.000 claims abstract description 8
- 238000005273 aeration Methods 0.000 claims abstract description 7
- PQTCMBYFWMFIGM-UHFFFAOYSA-N gold silver Chemical compound [Ag].[Au] PQTCMBYFWMFIGM-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000002002 slurry Substances 0.000 claims description 41
- 238000005188 flotation Methods 0.000 claims description 32
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical group OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 26
- 238000000605 extraction Methods 0.000 claims description 22
- 230000008929 regeneration Effects 0.000 claims description 19
- 238000011069 regeneration method Methods 0.000 claims description 19
- 238000005086 pumping Methods 0.000 claims description 15
- 229920006395 saturated elastomer Polymers 0.000 claims description 15
- 239000007787 solid Substances 0.000 claims description 11
- 239000012286 potassium permanganate Substances 0.000 claims description 6
- 238000010301 surface-oxidation reaction Methods 0.000 claims description 5
- 239000000575 pesticide Substances 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims 1
- 230000000717 retained effect Effects 0.000 claims 1
- 229910052500 inorganic mineral Inorganic materials 0.000 abstract description 18
- 239000011707 mineral Substances 0.000 abstract description 18
- 239000007788 liquid Substances 0.000 abstract description 14
- 230000003647 oxidation Effects 0.000 abstract description 5
- 238000007254 oxidation reaction Methods 0.000 abstract description 5
- 230000005465 channeling Effects 0.000 abstract description 2
- 239000002245 particle Substances 0.000 description 25
- 239000003814 drug Substances 0.000 description 23
- 239000003795 chemical substances by application Substances 0.000 description 14
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 description 12
- -1 sulfide ions Chemical class 0.000 description 12
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 10
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 10
- 239000004088 foaming agent Substances 0.000 description 9
- 238000011084 recovery Methods 0.000 description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 239000000243 solution Substances 0.000 description 6
- 150000002500 ions Chemical class 0.000 description 5
- 229910052742 iron Inorganic materials 0.000 description 5
- 239000002699 waste material Substances 0.000 description 5
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 4
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 4
- 239000002250 absorbent Substances 0.000 description 4
- 230000002745 absorbent Effects 0.000 description 4
- 239000007864 aqueous solution Substances 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 4
- 229910052802 copper Inorganic materials 0.000 description 4
- 239000010949 copper Substances 0.000 description 4
- 229910001448 ferrous ion Inorganic materials 0.000 description 4
- 239000002244 precipitate Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- LFAGQMCIGQNPJG-UHFFFAOYSA-N silver cyanide Chemical compound [Ag+].N#[C-] LFAGQMCIGQNPJG-UHFFFAOYSA-N 0.000 description 4
- 229940098221 silver cyanide Drugs 0.000 description 4
- 238000005728 strengthening Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000012958 reprocessing Methods 0.000 description 3
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- 229910052785 arsenic Inorganic materials 0.000 description 2
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 229940079593 drug Drugs 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000008396 flotation agent Substances 0.000 description 2
- 238000000227 grinding Methods 0.000 description 2
- 230000002209 hydrophobic effect Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000000813 microbial effect Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 238000009279 wet oxidation reaction Methods 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
Images
Classifications
-
- 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
- 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
- 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
-
- 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
Landscapes
- 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 method for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate, belonging to the field of mineral separation and comprising two parts: (1) the pretreatment of the active carbon removal and the oxidation passivation of the surface of the pyrite comprises the following steps: (a) adding lime and an oxidant to the gold-silver-containing sulfur concentrate to be treated, and sequentially carrying out pretreatment of stirring, desorption and reagent removal twice and alkaline leaching and aeration once to strengthen surface passivation; (b) adding active carbon into a second section of the stirring tank for removing the chemicals and passivating, and sequentially channeling the mixture of the carbon and pulp forward, wherein the active carbon and the pulp mutually flow in a counter-current manner; (2) cyaniding leaching-active carbon is used for respectively adsorbing and extracting gold and silver step by step, and the steps are as follows: (a) adding sodium cyanide for size mixing, and performing single cyaniding leaching; (b) adding activated carbon to extract silver, and feeding the carbon pulp mixture forward in sequence, wherein the activated carbon and the ore pulp mutually flow in a counter-current manner. The invention can improve the adsorption speed and the adsorption rate of the activated carbon, improve the leaching speed and the leaching rate of the gold and silver and reduce the content of the gold and silver in tail liquid.
Description
Technical Field
The invention relates to a method for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate, belonging to the field of mineral separation.
Background
Mineral separation is a process of separating useful minerals from useless minerals or harmful minerals in mineral raw materials by a physical or chemical method or separating a plurality of useful minerals, which is also called mineral processing, wherein useful components in products are enriched and called concentrate, and useless components are enriched and called tailings, and the useful components enriched products provided by mineral separation are mainly used as raw materials for extracting metals in the smelting industry. At present, the common methods for extracting gold and silver from gold-bearing silver-sulfur concentrate include direct cyanidation leaching and oxidation pretreatment (including roasting, wet oxidation, microbial oxidation) followed by recyaniation leaching. For the direct cyaniding leaching method, the collecting agent attached to the surface of mineral particles can sharply reduce the leaching speed and leaching rate of gold and silver; when the oxygen is supplemented in cyaniding leaching (generally, the consumed oxygen is supplemented in an air-filled mode), because a large amount of foaming agent exists in the ore pulp, a large amount of foam floats on the surface of the ore pulp, so that the ore pulp is easy to leak, the leakage is easy to form, great difficulty is brought to production operation, and gold and silver losses are easy to form; when the activated carbon is used for enriching gold and silver, because the solution contains flotation agents such as a collecting agent, a foaming agent and the like, organic substances are adsorbed by the activated carbon to block fine holes of the activated carbon, so that the adsorption speed and the adsorption rate of the gold and silver are reduced sharply, and the content of the gold and silver in tail liquid is higher; during cyaniding leaching, because of the dissolution of pyrite, sulfide ions and ferrous ions exist in ore pulp, the ore pulp reacts with cyanide chemically, a large amount of cyanide is consumed, and the sulfide ions and cyanide complex ions of the gold and silver are precipitated, so that the leaching rate of gold and silver is reduced, and particularly the leaching rate of silver is greatly influenced; the cyanide tail liquid contains a large amount of cyanide and a small amount of gold and silver, so the cyanide tail liquid must be recycled, and in the process, the collecting agent and the foaming agent are continuously enriched, so the production is seriously influenced. For a method of oxidation pretreatment (comprising roasting, wet oxidation and microbial oxidation) and then cyanidation leaching, the method has the disadvantages of long process flow, complex process, high production control difficulty, high production cost, low comprehensive economic benefit of mineral separation, difficult control of three-waste pollution and poor production safety and controllability; and is not suitable for extracting gold and silver from sulfur concentrate flotation products with low gold, silver, sulfur and iron contents. Therefore, the key to solve the existing problems is to seek a scientific and effective treatment method for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate.
Disclosure of Invention
The invention provides a method for efficiently extracting gold and silver from gold and silver-containing sulfur concentrate, which can improve the adsorption speed and adsorption rate of activated carbon, improve the leaching speed and leaching rate of the gold and silver and reduce the content of the gold and silver in tail liquor.
The technical scheme comprises the pretreatment of twice gradient countercurrent reagent removal of activated carbon and one-time enhanced passivation of the surface of pyrite, cyaniding leaching-step extraction of gold and silver by activated carbon, and specifically comprises the following steps:
(1) and performing gradient countercurrent active carbon removal and pyrite surface oxidation passivation pretreatment. The method is carried out by three-stage stirring, and comprises the following steps:
(a) adding 16-20 kg/t of lime and 1-1.5 kg/t of oxidants such as hydrogen peroxide or potassium permanganate into gold-containing silver-sulfur concentrate to be treated, carrying out size mixing according to the liquid-solid ratio of 1:1, sequentially carrying out two-stage stirring desorption and reagent removal and one-stage alkaline leaching enhanced surface passivation pretreatment, wherein the pretreatment time of each stage is 2-4 hours, the third stage is an inflation enhanced alkaline leaching tank, and the inflation amount of the inflation enhanced alkaline leaching tank is 0.3m3/（m2H). In the process, lime plays a role in desorbing a flotation reagent (a collecting agent) on the surface of mineral particles into an aqueous solution, and simultaneously ensuring a proper end point pH value (pH = 11-12) of ore pulp; the hydrogen peroxide is used for oxidizing the surface of the pyrite particles to generate a layer of passive film, so that the pyrite and sodium cyanide are prevented from chemically reacting, and sulfur ions precipitate dissolved submicron silver cyanide complex ions;
(b) adding absorbent granular activated carbon from the second section of the mixing tank for removing the medicine and passivating, stirring and adsorbing for a period of time, and then sequentially pumping the mixture of the carbon and the pulp forward (namely the second section to the first section), wherein the activated carbon and the ore pulp are mutually countercurrent, a carbon separating sieve for separating the carbon pulp is arranged between the two sections of mixing tanks for removing the medicine, the ore pulp returns to the original mixing tank for removing the medicine, and the granular activated carbon is reserved in the mixing tank for removing the medicine in front. After the activated carbon in the first-stage adsorption stirring tank is saturated, the carbon pulp mixture is conveyed to a No. 1 vibrating screen for carbon pulp separation, ore pulp returns to the first-stage medicine removal tank, and the activated carbon loaded with a flotation reagent is recycled after regeneration. The carbon extraction amount and the regeneration frequency of the activated carbon are determined according to the saturation degree of the activated carbon adsorption flotation reagent. The concentration of the active carbon in the reagent removing stirring tank is kept between 45 and 65g/L, and the active carbon has the function of adsorbing and removing flotation reagents (collecting agents and foaming agents) in the ore pulp, so that the cyaniding leached ore pulp is ensured not to contain the flotation reagents.
(2) Cyaniding leaching-active carbon is used for respectively adsorbing and extracting gold and silver step by step, and the steps are as follows:
(a) conveying the ore pulp subjected to the steps of removing the chemicals and passivating to a No. 2 stirring barrel, adding 4-6 kg/t of sodium cyanide for size mixing, performing cyanide leaching by using No. 1 and No. 2 leaching tanks separately, performing leaching while adsorbing by using other leaching adsorption tanks, wherein the air inflation of each leaching tank is 0.3m3/（m2H), and the total leaching time is 24-36 hours. Adding gold extraction activated carbon from the 7# leaching adsorption tank, pumping the carbon pulp mixture forward in sequence after leaching and adsorbing for a period of time, allowing the activated carbon and the ore pulp to flow counter-currently, installing a carbon separation sieve for separating the carbon pulp between the two sections of leaching adsorption tanks, returning the ore pulp to the original leaching adsorption tank, and retaining the activated carbon in the front leaching adsorption tank. And after gold is adsorbed and saturated in the 3# groove, conveying the carbon slurry mixture to a 2# vibrating screen for carbon slurry separation, returning ore pulp to the 3# leaching adsorption groove, and allowing the high-gold low-silver activated carbon to enter a desorption workshop. The carbon extraction amount and the regeneration frequency of the activated carbon are determined according to the saturation degree of the activated carbon for adsorbing gold, and the concentration of the activated carbon in the leaching adsorption tank is kept between 15 and 30 g/L.
(b) Adding silver-extracting activated carbon from the No. 11 leaching adsorption tank, pumping the carbon slurry mixture forward in sequence after leaching and adsorbing for a period of time, allowing the activated carbon and the ore slurry to flow in a mutually countercurrent manner, installing a carbon separation sieve for separating the carbon slurry between the two sections of leaching adsorption tanks, returning the ore slurry to the original leaching adsorption tank, and retaining the activated carbon in the front leaching adsorption tank. And after the silver is adsorbed and saturated in the 8# groove, conveying the carbon slurry mixture to a 3# vibrating screen for carbon slurry separation, returning ore pulp to the 8# leaching adsorption groove, and allowing the low-gold high-silver activated carbon to enter a desorption workshop. The carbon extraction amount and the regeneration frequency of the activated carbon are determined according to the saturation degree of the activated carbon for adsorbing silver, and the concentration of the activated carbon in the leaching adsorption tank is kept between 15 and 30 g/L.
The invention provides a novel method for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate, which can improve the adsorption speed and adsorption rate of activated carbon, improve the leaching speed and leaching rate of gold and silver, reduce the content of gold and silver in tail liquid, simultaneously avoid the phenomena of leakage, overflow and drip, and has simple flow, easy control, small three-waste pollution, safety, controllability and strong adaptability of the cyanogen-containing tail liquid reprocessing.
Has the advantages that:
(1) carrying out pretreatment for 6-12 hours by adopting 16-20 kg/t lime and 1-1.5 kg/t of oxidants such as hydrogen peroxide or potassium permanganate to destroy the collecting agent adsorbed on the surface of the mineral particles;
(2) lime and hydrogen peroxide are matched with each other for pretreatment for 6-12 hours, the surfaces of pyrite mineral particles are passivated in advance, and during cyaniding leaching, the effects of preventing or reducing the reaction of pyrite and sodium cyanide and precipitating dissolved submicron silver complex ions by sulfur ions are achieved, and meanwhile, the appropriate end point pH value (pH = 11-12) of ore pulp is ensured.
(3) A three-stage gradient countercurrent activated carbon adsorption process is adopted to remove the flotation reagent in the solution, and the concentration of the depurative activated carbon is 45-65 g/L. The influence of a flotation reagent on the leaching of sodium cyanide, the gold and silver adsorption effect of activated carbon and the production control is avoided;
(4) the independent aeration quantity is 0.3m3/（m2H) in the pyrite surface strengthening passivation alkaline leaching pretreatment section, the leaching time is 2-4 hours.
(5) Adding 4-6 kg/t of sodium cyanide into a No. 2 stirring barrel for size mixing, performing single cyaniding leaching by using No. 1 and No. 2 leaching tanks, and then performing leaching and adsorption on gold and silver respectively in stages, wherein the concentration of activated carbon in the leaching tanks is 15-30 g/L, the total leaching time is 24-36 hours, the gold and silver extraction efficiency is enhanced, and two products of high-gold low-silver activated carbon and low-gold high-silver activated carbon are obtained.
By the above mode, the following steps are realized:
(1) the speed and the adsorption rate of the activated carbon for adsorbing the gold and silver are improved. In the pretreatment and drug removal stage, the active carbon is adopted to completely remove the flotation reagent in advance, so that the subsequent gold and silver leaching and adsorption stage is avoided, and the flotation reagent is adsorbed on the surface of the activated carbon for extracting gold and silver to block holes of the activated carbon and block the adsorption of gold and silver;
(2) the leaching speed and leaching rate of the gold and silver are improved, and the content of the gold and silver in tail liquor is reduced. In the pretreatment stage, lime desorbs the hydrophobic collecting agent adsorbed on the surfaces of the gold and silver particles into solution; meanwhile, hydrogen peroxide and oxygen passivate the surface of the pyrite, so that the influence of ferrous ions and sulfur ions is reduced, and the adsorption stage of gold and silver leaching is promoted, and the adsorption of gold and silver particles on cyanogen and oxygen and the chemical reaction of the gold and silver particles with each other are promoted;
(3) can avoid the phenomena of leakage and the reprocessing of the cyanogen-containing tail liquid. In the pretreatment pesticide removing stage, active carbon is adopted to completely remove the foaming agent in the ore pulp in advance, so that the subsequent gold and silver leaching and adsorbing stage is avoided, and in the aeration process, a large amount of bubbles are formed on the surface of the ore pulp to form leakage and leakage, so that part of gold and silver particles are lost;
(4) simple process flow, easy control, little pollution of three wastes, safety and controllability. The process adopts a stirring tank and a leaching tank which have simple structures and are easy to operate; meanwhile, the generated wastewater is completely recycled, and the safety guarantee is easy;
(5) the method has strong adaptability, is particularly suitable for treating the gold-silver-containing sulfur concentrate with high silver content and large fluctuation, and can completely adsorb the leachate with higher silver content in pregnant solution. In the leaching and adsorption stage of gold and silver, gold and silver are respectively extracted step by step, so that the problem that gold adsorbs silver by activated carbon is overcome, and the recovery rate of gold and silver is improved.
In conclusion, the invention provides a way for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate, which influences leaching and adsorption extraction of gold and silver by flotation agents existing in flotation concentrate; the sulfur and ferrous ions on the surface of the sulfur concentrate particles react with sodium cyanide to consume the sodium cyanide, and the sulfur ions dissolved in the solution precipitate with gold and silver ions, thereby reducing the recovery rate of gold and silver. (1) Mainly solves the external reasons (influence on the common) influencing the recovery rate of the gold and the silver, and (2) mainly solves the problem that the gold and the silver are mixed together and influence each other to cause the respective recovery rate to be reduced, and the gold and the silver are separately treated to eliminate or reduce the influence degree between each other, thereby achieving the purpose of improving the respective recovery rate. The invention can improve the adsorption speed and the adsorption rate of the active carbon, improve the leaching speed and the leaching rate of the gold and silver, reduce the content of the gold and silver in the tail liquid, simultaneously avoid the phenomena of leakage and leakage, and has simple flow, easy control, little pollution of three wastes, safety, controllability and strong adaptability of the cyanogen-containing tail liquid.
Drawings
FIG. 1 is a process flow for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate;
FIG. 2 is a connection diagram of an apparatus for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate;
wherein, 1: 1# stirring barrel, 2: 2# medicine-removing and carbon-channeling device, 3: 1# vibrating screen, 4: a medicine removing barrel; 5: slurry pump, 6: 2# stirring barrel, 7 leaching tank, 8: 2# vibrating screen, 9: 2# leaching and carbon channeling device, 10: and 3# vibrating screen.
Detailed Description
The system for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate as shown in fig. 2 comprises a pretreatment system and a leaching system; the pretreatment system comprises a No. 1 stirring barrel 1, a No. 1 pretreatment tank, a No. 2 pretreatment tank and an aeration leaching pretreatment tank, the 1# stirring barrel 1 is arranged at a high position (the position is higher than that of the pretreatment tank, so that ore pulp in the stirring barrel can conveniently enter the pretreatment tank), the 1# stirring barrel 1 is added with gold and silver-containing sulfur concentrate and lime to be treated, the upper ends of the side walls of the 1# stirring barrel 1, the 1# pretreatment tank, the 2# pretreatment tank and the air-inflation leaching pretreatment tank are respectively provided with an overflow port, the 1# stirring barrel 1 overflow port outlet is connected with the middle part of the 1# pretreatment tank, the 1# pretreatment tank overflow port outlet is connected with the middle part of the 2# pretreatment tank, activated carbon is added into the 2# pretreatment tank, the 2# pretreatment tank overflow port outlet is connected with the middle part of the air-inflation leaching pretreatment tank, and the air-inflation leaching pretreatment tank overflow port outlet is connected with the inlet at the upper; the middle parts of the No. 1 pretreatment tank and the No. 2 pretreatment tank extend into the adsorption tube 10, a pump is arranged on the adsorption tube 10, negative pressure is provided by the adsorption pump 4 for adsorption, the other end of the adsorption tube 10 in the No. 2 pretreatment tank extends into the No. 1 pretreatment tank, the other end of the adsorption tube in the No. 1 pretreatment tank extends into the No. 1 vibrating screen, solid particles collected at the lower end of the screen of the No. 1 vibrating screen are medicine-carrying activated carbon, and the solid particles return to the regeneration device for regeneration;
liquid collected at the lower end of the No. 1 vibrating screen and ore pulp at an overflow port outlet of the No. 1 stirring barrel enter a No. 1 pretreatment tank together; an inflator pump 6 is arranged in the air-inflation leaching pretreatment tank through a pipeline; the leaching system comprises: the device comprises a No. 2 stirring barrel 7, No. 1-11 leaching tanks, a No. 2 vibrating screen and a No. 3 vibrating screen, wherein the No. 2 stirring barrel is arranged at a high position, overflow ports are respectively arranged at the upper ends of the side walls of the No. 2 stirring barrel 7 and the No. 1-11 leaching tanks, the outlet of the overflow port of the No. 2 stirring barrel 7 is connected with the middle part of the No. 1 leaching tank, the outlet of the overflow port of the No. 1 leaching tank is connected with the middle part of the No. 2 leaching tank, the outlet of the overflow port of the No. 2 leaching tank is connected with the middle part of the No. 3; outlets of overflow ports of the 3# to 7# leaching tanks are sequentially connected with the middle part of the next-stage leaching tank, the middle parts of the 4# to 7# leaching tanks extend into the adsorption pipe 10, the adsorption pipe is provided with an adsorption pump 2, and the other ends of the adsorption pipes 10 in the 4# to 7# leaching tanks extend into the previous-stage leaching tank; the middle part of the 3# leaching tank extends into an adsorption pipe, a pump is arranged on the adsorption pipe, the other end of the adsorption pipe in the 3# leaching tank extends into a 2# vibrating screen 9, solid particles collected at the lower end of a screen of the 2# vibrating screen 9 are high-gold low-silver activated carbon, liquid collected at the lower end of the 2# vibrating screen 9 and ore pulp at an overflow port outlet of the 2# leaching tank enter the 3# leaching tank together, sodium cyanide is added into the 3# leaching tank, and activated carbon is added into the 7# leaching tank; the outlet of the overflow port of the 8# -11 # leaching tank is sequentially connected with the middle part of the next-stage leaching tank, the middle part of the 9# -11 # leaching tank extends into an adsorption pipe, the adsorption pipe is provided with a pump, and the other end of the adsorption pipe in the 9# -11 # leaching tank extends into the previous-stage leaching tank;
the middle part of the 8# leaching tank extends into an adsorption pipe, a pump is arranged on the adsorption pipe, the other end of the adsorption pipe in the 8# leaching tank extends into a 3# vibrating screen 11, solid particles collected at the lower end of a screen of the 3# vibrating screen 11 are low-gold high-silver activated carbon, liquid collected at the lower end of the 3# vibrating screen 11 and ore pulp at an overflow port outlet of a 7# leaching tank enter the 8# leaching tank together, activated carbon is added into the 11# leaching tank, and sulfur concentrate flows out from the overflow port outlet of the 11# leaching tank; stirring devices are arranged in the No. 1 stirring barrel, the No. 2 stirring barrel, the No. 1 pretreatment tank, the No. 2 pretreatment tank, the aeration leaching pretreatment tank and the No. 1-11 leaching tank; screens are arranged at the overflow ports of the No. 1 pretreatment tank, the No. 2 pretreatment tank and the No. 3-11 leaching tanks, so that the activated carbon is prevented from flowing into the next-stage tank through the overflow ports; the No. 1 vibrating screen 3, the No. 2 vibrating screen 9 and the No. 3 vibrating screen 11 are all inclined vibrating screens, and funnel-shaped collecting devices are arranged at the lower ends of the vibrating screens and used for collecting liquid; the lower end of the screen of the vibrating screen is provided with a solid particle discharge hole.
The extraction method comprises the steps of active carbon twice gradient countercurrent reagent removal and one pyrite surface strengthening passivation pretreatment, cyaniding leaching-active carbon step by step extraction of gold and silver, and specifically comprises the following steps:
(1) and performing gradient countercurrent active carbon removal and pyrite surface oxidation passivation pretreatment. The method is carried out by three-stage stirring, and comprises the following steps:
(a) adding 16-20 kg/t of lime and 1-1.5 kg/t of oxidants such as hydrogen peroxide or potassium permanganate into gold-containing silver-sulfur concentrate to be treated, carrying out size mixing according to the liquid-solid ratio of 1:1, sequentially carrying out two-stage stirring desorption and reagent removal and one-stage alkaline leaching enhanced surface passivation pretreatment, wherein the pretreatment time of each stage is 2-4 hours, the third stage is an inflation enhanced alkaline leaching tank, and the inflation amount of the inflation enhanced alkaline leaching tank is 0.3m3/（m2H). In the process, lime plays a role in desorbing a flotation reagent (a collecting agent) on the surface of mineral particles into an aqueous solution, and simultaneously ensuring a proper end point pH value (pH = 11-12) of ore pulp; the hydrogen peroxide is used for oxidizing the surface of the pyrite particles to generate a layer of passive film, so that the pyrite and sodium cyanide are prevented from chemically reacting, and sulfur ions precipitate dissolved submicron silver cyanide complex ions;
(b) adding absorbent granular activated carbon from the second section of the mixing tank for removing the medicine and passivating, stirring and adsorbing for a period of time, and then sequentially pumping the mixture of the carbon and the pulp forward (namely the second section to the first section), wherein the activated carbon and the ore pulp are mutually countercurrent, a carbon separating sieve for separating the carbon pulp is arranged between the two sections of mixing tanks for removing the medicine, the ore pulp returns to the original mixing tank for removing the medicine, and the granular activated carbon is reserved in the mixing tank for removing the medicine in front. After the activated carbon in the first-stage adsorption stirring tank is saturated, the carbon pulp mixture is conveyed to a No. 1 vibrating screen for carbon pulp separation, ore pulp returns to the first-stage medicine removal tank, and the activated carbon loaded with a flotation reagent is recycled after regeneration. The carbon extraction amount and the regeneration frequency of the activated carbon are determined according to the saturation degree of the activated carbon adsorption flotation reagent. The concentration of the active carbon in the reagent removing stirring tank is kept between 45 and 65g/L, and the active carbon has the function of adsorbing and removing flotation reagents (collecting agents and foaming agents) in the ore pulp, so that the cyaniding leached ore pulp is ensured not to contain the flotation reagents.
(2) Cyaniding leaching-active carbon is used for respectively adsorbing and extracting gold and silver step by step, and the steps are as follows:
(a) conveying the ore pulp subjected to the steps of removing the chemicals and passivating to a No. 2 stirring barrel, adding 4-6 kg/t of sodium cyanide for size mixing, performing cyanide leaching by using No. 1 and No. 2 leaching tanks separately, performing leaching while adsorbing by using other leaching tanks, wherein the air inflation of each leaching tank is 0.3m3/（m2H), and the total leaching time is 24-36 hours. Adding gold-extracting active carbon from No. 7 leaching tank, leaching and adsorbing for a period of time, sequentially pumping the carbon pulp mixture forward, allowing the active carbon and the ore pulp to flow in a mutually countercurrent manner, installing a carbon separating sieve for separating the carbon pulp between two sections of leaching tanks, returning the ore pulp to the original leaching tank, and retaining the active carbon in the front leaching tank. And after gold is adsorbed and saturated in the 3# groove, conveying the carbon slurry mixture to a 2# vibrating screen for carbon slurry separation, returning ore slurry to the 3# leaching groove, and allowing the high-gold low-silver activated carbon to enter a desorption workshop. The carbon extraction amount and the regeneration frequency of the activated carbon are determined according to the saturation degree of the activated carbon for adsorbing gold, and the concentration of the activated carbon in the leaching tank is kept between 15 and 30 g/L.
(b) Adding silver-extracting activated carbon from a No. 11 leaching tank, pumping the carbon pulp mixture forward in sequence after leaching and adsorbing for a period of time, allowing the activated carbon and the ore pulp to flow in a mutually reverse manner, installing a carbon separation sieve for separating the carbon pulp between two sections of leaching tanks, returning the ore pulp to the original leaching tank, and retaining the activated carbon in the front leaching tank. And after the silver is adsorbed and saturated in the 8# groove, conveying the carbon slurry mixture to a 3# vibrating screen for carbon slurry separation, returning ore slurry to the 8# leaching groove, and allowing the low-gold high-silver activated carbon to enter a desorption workshop. The carbon extraction amount and the regeneration frequency of the activated carbon are determined according to the saturation degree of the activated carbon for adsorbing silver, and the concentration of the activated carbon in the leaching tank is kept between 15 and 30 g/L.
The first embodiment is as follows:
the flotation sulfur concentrate containing gold and silver has the grinding fineness of 86% in-0.043 mm, and the chemical analysis results of main elements are as follows: gold Au5.68g/t, silver Ag46.45g/t, copper Cu0.15%, sulfur S47.34%, arsenic As0.026%, iron Fe42.16%; the results of the phase analysis are shown in Table 1.
As can be seen from element analysis, the gold contained in the sulfur concentrate is 5.68g/t, and is a low-grade gold-containing material, and in addition, the concentrate has high contents of copper, iron and sulfur, and is not beneficial to leaching of gold and silver in the cyaniding leaching process. As can be seen from Table 1, gold exists mainly in the form of bare gold, and is secondarily wrapped by sulfide (i.e., pyrite), and a small amount of gold is wrapped by other gangue, and the wrapped part is not beneficial to leaching of gold.
The invention is used for implementing the gold-silver-containing sulfur concentrate, and the technical scheme comprises the pretreatment of activated carbon sub-stage gradient countercurrent reagent removal and primary pyrite surface strengthening and passivation and cyaniding leaching-the activated carbon step by step extracts gold and silver:
(1) and performing gradient countercurrent active carbon removal and pyrite surface oxidation passivation pretreatment. The method is carried out by three-stage stirring, and comprises the following steps:
(a) adding 16-20 kg/t of lime and 1-1.5 kg/t of oxidants such as hydrogen peroxide or potassium permanganate into gold-containing silver-sulfur concentrate to be treated, carrying out size mixing according to the liquid-solid ratio of 1:1, sequentially carrying out two-stage stirring desorption and reagent removal and one-stage alkaline leaching enhanced surface passivation pretreatment, wherein the pretreatment time of each stage is 2-4 hours, the third stage is an inflation enhanced alkaline leaching tank, and the inflation amount of the inflation enhanced alkaline leaching tank is 0.3m3/（m2H). In the process, lime plays a role in desorbing a flotation reagent (a collecting agent) on the surface of mineral particles into an aqueous solution, and simultaneously ensuring a proper end point pH value (pH = 11-12) of ore pulp; the hydrogen peroxide is used for oxidizing the surface of the pyrite particle to generate a layer of passive film to prevent the pyrite from chemically reacting with sodium cyanide and prevent the dissolved submicron silver cyanide from being complexed by sulfur ionsSub-precipitation;
(b) adding absorbent granular activated carbon from the second section of the mixing tank for removing the medicine and passivating, stirring and adsorbing for a period of time, and then sequentially pumping the mixture of the carbon and the pulp forward (namely the second section to the first section), wherein the activated carbon and the ore pulp are mutually countercurrent, a carbon separating sieve for separating the carbon pulp is arranged between the two sections of mixing tanks for removing the medicine, the ore pulp returns to the original mixing tank for removing the medicine, and the granular activated carbon is reserved in the mixing tank for removing the medicine in front. After the activated carbon in the first-stage adsorption stirring tank is saturated, the carbon pulp mixture is conveyed to a No. 1 vibrating screen for carbon pulp separation, ore pulp returns to the first-stage medicine removal tank, and the activated carbon loaded with a flotation reagent is recycled after regeneration. The carbon extraction amount and the regeneration frequency of the activated carbon are determined according to the saturation degree of the activated carbon adsorption flotation reagent. The concentration of the active carbon in the reagent removing stirring tank is kept between 45 and 65g/L, and the active carbon has the function of adsorbing and removing flotation reagents (collecting agents and foaming agents) in the ore pulp, so that the cyaniding leached ore pulp is ensured not to contain the flotation reagents.
(2) Cyaniding leaching-active carbon is used for respectively adsorbing and extracting gold and silver step by step, and the steps are as follows:
(a) conveying the ore pulp subjected to the steps of removing the chemicals and passivating to a No. 2 stirring barrel, adding 4-6 kg/t of sodium cyanide for size mixing, performing cyanide leaching by using No. 1 and No. 2 leaching tanks separately, performing leaching while adsorbing by using other leaching adsorption tanks, wherein the air inflation of each leaching tank is 0.3m3/（m2H), and the total leaching time is 24-36 hours. Adding gold extraction activated carbon from the 7# leaching adsorption tank, pumping the carbon pulp mixture forward in sequence after leaching and adsorbing for a period of time, allowing the activated carbon and the ore pulp to flow counter-currently, installing a carbon separation sieve for separating the carbon pulp between the two sections of leaching adsorption tanks, returning the ore pulp to the original leaching adsorption tank, and retaining the activated carbon in the front leaching adsorption tank. And after gold is adsorbed and saturated in the 3# groove, conveying the carbon slurry mixture to a 2# vibrating screen for carbon slurry separation, returning ore pulp to the 3# leaching adsorption groove, and allowing the high-gold low-silver activated carbon to enter a desorption workshop. The carbon extraction amount and the regeneration frequency of the activated carbon are determined according to the saturation degree of the activated carbon for adsorbing gold, and the concentration of the activated carbon in the leaching adsorption tank is kept between 15 and 30 g/L.
(b) Adding silver-extracting activated carbon from the No. 11 leaching adsorption tank, pumping the carbon slurry mixture forward in sequence after leaching and adsorbing for a period of time, allowing the activated carbon and the ore slurry to flow in a mutually countercurrent manner, installing a carbon separation sieve for separating the carbon slurry between the two sections of leaching adsorption tanks, returning the ore slurry to the original leaching adsorption tank, and retaining the activated carbon in the front leaching adsorption tank. And after the silver is adsorbed and saturated in the 8# groove, conveying the carbon slurry mixture to a 3# vibrating screen for carbon slurry separation, returning ore pulp to the 8# leaching adsorption groove, and allowing the low-gold high-silver activated carbon to enter a desorption workshop. The carbon extraction amount and the regeneration frequency of the activated carbon are determined according to the saturation degree of the activated carbon for adsorbing silver, and the concentration of the activated carbon in the leaching adsorption tank is kept between 15 and 30 g/L. The gold content of the finally obtained high-gold and low-silver activated carbon is 1265.52g/t, the silver content is 1854.78g/t, the gold content of the low-gold and high-silver activated carbon is 217.66g/t, the silver content of the low-gold and high-silver activated carbon is 5375.66g/t, the total gold recovery rate is 86.83 percent, and the total silver recovery rate is 64.87 percent.
(5) The adsorption speed and the adsorption rate of the activated carbon are improved. In the pretreatment and drug removal stage, the active carbon is adopted to completely remove the flotation reagent in advance, so that the subsequent gold and silver leaching and adsorption stage is avoided, and the flotation reagent is adsorbed on the surface of the activated carbon for extracting gold and silver to block holes of the activated carbon and block the adsorption of gold and silver;
(6) the leaching speed and leaching rate of the gold and silver are improved, and the content of the gold and silver in tail liquor is reduced. In the pretreatment stage, lime desorbs the hydrophobic collecting agent adsorbed on the surfaces of the gold and silver particles into solution; meanwhile, hydrogen peroxide and oxygen passivate the surface of the pyrite, so that the influence of ferrous ions and sulfur ions is reduced, and the adsorption stage of gold and silver leaching is promoted, and the adsorption of gold and silver particles on cyanogen and oxygen and the chemical reaction of the gold and silver particles with each other are promoted;
(7) can avoid the phenomena of leakage and the reprocessing of the cyanogen-containing tail liquid. In the pretreatment pesticide removing stage, active carbon is adopted to completely remove the foaming agent in the ore pulp in advance, so that the subsequent gold and silver leaching and adsorbing stage is avoided, and in the aeration process, a large amount of bubbles are formed on the surface of the ore pulp to form leakage and leakage, so that part of gold and silver particles are lost;
(8) simple process flow, easy control, little pollution of three wastes, safety and controllability. The process adopts a stirring tank and a leaching tank which have simple structures and are easy to operate; meanwhile, the generated wastewater is completely recycled, and the safety guarantee is easy.
Example two:
the flotation sulfur concentrate containing gold and silver has the grinding fineness of 85 percent (minus 0.043 mm), and the chemical analysis result of main elements is as follows: gold Au6.31g/t, silver Ag78.18g/t, copper Cu0.10%, sulfur S46.85%, arsenic As0.11%, iron Fe42.49%; the results of the phase analysis are shown in Table 2.
As can be known from element analysis, the gold content in the sulfur concentrate is 6.31g/t, and the sulfur concentrate is a low-grade gold-containing material, and in addition, the concentrate has high contents of copper, iron and sulfur, and is not beneficial to leaching gold in the cyaniding leaching process. As can be seen from Table 1, gold exists mainly in the form of bare gold, and is secondarily wrapped by sulfide (i.e., pyrite), and a small amount of gold is wrapped by other gangue, and the wrapped part is not beneficial to leaching of gold.
The invention is used for implementing the gold-silver-containing sulfur concentrate, and the technical scheme comprises two times of gradient countercurrent reagent removal of activated carbon, pretreatment of one time of pyrite surface strengthening and passivation, cyaniding leaching and step-by-step extraction of gold and silver by activated carbon:
(1) and performing gradient countercurrent active carbon removal and pyrite surface oxidation passivation pretreatment. The method is carried out by three-stage stirring, and comprises the following steps:
(a) adding 16-20 kg/t of lime and 1-1.5 kg/t of oxidants such as hydrogen peroxide or potassium permanganate into gold-containing silver-sulfur concentrate to be treated, carrying out size mixing according to the liquid-solid ratio of 1:1, sequentially carrying out two-stage stirring desorption and reagent removal and one-stage alkaline leaching enhanced surface passivation pretreatment, wherein the pretreatment time of each stage is 2-4 hours, the third stage is an inflation enhanced alkaline leaching tank, and the inflation amount of the inflation enhanced alkaline leaching tank is 0.3m3/（m2H). In the process, lime plays a role in desorbing a flotation reagent (a collecting agent) on the surface of mineral particles into an aqueous solution, and simultaneously ensuring a proper end point pH value (pH = 11-12) of ore pulp; the hydrogen peroxide is used for oxidizing the surface of the pyrite particles to generate a layer of passive film, so that the pyrite and sodium cyanide are prevented from chemically reacting, and sulfur ions precipitate dissolved submicron silver cyanide complex ions;
(b) adding absorbent granular activated carbon from the second section of the mixing tank for removing the medicine and passivating, stirring and adsorbing for a period of time, and then sequentially pumping the mixture of the carbon and the pulp forward (namely the second section to the first section), wherein the activated carbon and the ore pulp are mutually countercurrent, a carbon separating sieve for separating the carbon pulp is arranged between the two sections of mixing tanks for removing the medicine, the ore pulp returns to the original mixing tank for removing the medicine, and the granular activated carbon is reserved in the mixing tank for removing the medicine in front. After the activated carbon in the first-stage adsorption stirring tank is saturated, the carbon pulp mixture is conveyed to a No. 1 vibrating screen for carbon pulp separation, ore pulp returns to the first-stage medicine removal tank, and the activated carbon loaded with a flotation reagent is recycled after regeneration. The carbon extraction amount and the regeneration frequency of the activated carbon are determined according to the saturation degree of the activated carbon adsorption flotation reagent. The concentration of the active carbon in the reagent removing stirring tank is kept between 45 and 65g/L, and the active carbon has the function of adsorbing and removing flotation reagents (collecting agents and foaming agents) in the ore pulp, so that the cyaniding leached ore pulp is ensured not to contain the flotation reagents.
(2) Cyaniding leaching-active carbon is used for respectively adsorbing and extracting gold and silver step by step, and the steps are as follows:
(a) conveying the ore pulp subjected to the steps of removing the chemicals and passivating to a No. 2 stirring barrel, adding 4-6 kg/t of sodium cyanide for size mixing, performing cyanide leaching by using No. 1 and No. 2 leaching tanks separately, performing leaching while adsorbing by using other leaching adsorption tanks, wherein the air inflation of each leaching tank is 0.3m3/（m2H), and the total leaching time is 24-36 hours. Adding gold extraction activated carbon from the 7# leaching adsorption tank, pumping the carbon pulp mixture forward in sequence after leaching and adsorbing for a period of time, allowing the activated carbon and the ore pulp to flow counter-currently, installing a carbon separation sieve for separating the carbon pulp between the two sections of leaching adsorption tanks, returning the ore pulp to the original leaching adsorption tank, and retaining the activated carbon in the front leaching adsorption tank. And after gold is adsorbed and saturated in the 3# groove, conveying the carbon slurry mixture to a 2# vibrating screen for carbon slurry separation, returning ore pulp to the 3# leaching adsorption groove, and allowing the high-gold low-silver activated carbon to enter a desorption workshop. The carbon extraction amount and the regeneration frequency of the activated carbon are determined according to the saturation degree of the activated carbon for adsorbing gold, and the concentration of the activated carbon in the leaching adsorption tank is kept between 15 and 30 g/L.
(b) Adding silver-extracting activated carbon from the No. 11 leaching adsorption tank, pumping the carbon slurry mixture forward in sequence after leaching and adsorbing for a period of time, allowing the activated carbon and the ore slurry to flow in a mutually countercurrent manner, installing a carbon separation sieve for separating the carbon slurry between the two sections of leaching adsorption tanks, returning the ore slurry to the original leaching adsorption tank, and retaining the activated carbon in the front leaching adsorption tank. And after the silver is adsorbed and saturated in the 8# groove, conveying the carbon slurry mixture to a 3# vibrating screen for carbon slurry separation, returning ore pulp to the 8# leaching adsorption groove, and allowing the low-gold high-silver activated carbon to enter a desorption workshop. The carbon extraction amount and the regeneration frequency of the activated carbon are determined according to the saturation degree of the activated carbon for adsorbing silver, and the concentration of the activated carbon in the leaching adsorption tank is kept between 15 and 30 g/L. The gold content of the finally obtained high-gold and low-silver activated carbon is 1357.38g/t, the silver content is 1728.85g/t, the gold content of the low-gold and high-silver activated carbon is 215.66g/t, the silver content of the low-gold and high-silver activated carbon is 6165g/t, the total recovery rate of gold is 88.15%, and the total recovery rate of silver is 67.41%.
The above examples show that the method for obtaining gold and silver by the invention has stable and reliable indexes, has better adaptability to different flotation concentrates containing gold, silver and sulfur, and is particularly suitable for treating the concentrates containing gold, silver and sulfur with higher proportion of gold, silver content.
Claims (4)
1. A method for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate is characterized by comprising two parts:
(1) the method comprises the following steps of performing gradient countercurrent active carbon removal and pyrite surface oxidation passivation pretreatment by stirring in three sections:
(a) adding lime and an oxidant into gold-silver-containing sulfur concentrate to be treated, carrying out size mixing according to the liquid-solid ratio of 1:1, sequentially carrying out pretreatment of stirring, desorption and reagent removal twice and one-time alkaline leaching enhanced surface passivation, and using an inflatable enhanced alkaline leaching tank in the third section;
(b) adding active carbon into the second-stage pesticide-removing and passivating stirring tank, stirring and adsorbing for a period of time, then sequentially pumping the mixture of carbon and pulp forward, wherein the active carbon and the pulp flow in a mutually countercurrent manner, a carbon separating sieve for separating the carbon pulp is arranged between the two sections of pesticide-removing stirring tanks, the pulp returns to the original pesticide-removing stirring tank, and the granular active carbon is retained in the front pesticide-removing stirring tank; when the activated carbon in the first-stage adsorption stirring tank is saturated, conveying the carbon slurry mixture to a No. 1 vibrating screen for carbon slurry separation, returning ore pulp to the first-stage pesticide removing tank, and recycling the activated carbon loaded with a flotation reagent after regeneration;
(2) cyaniding leaching-active carbon is used for respectively adsorbing and extracting gold and silver step by step, and the steps are as follows:
(a) conveying the ore pulp subjected to the steps of removing the chemicals and passivating to a No. 2 stirring barrel, adding sodium cyanide for size mixing, and then performing single cyaniding leaching by using No. 1 and No. 2 leaching tanks, wherein other leaching adsorption tanks perform leaching while adsorbing, and each leaching tank is inflated; adding gold extraction activated carbon from the 7# leaching adsorption tank, pumping the carbon pulp mixture forward in sequence after leaching and adsorbing for a period of time, allowing the activated carbon and the ore pulp to flow in a mutually countercurrent manner, installing a carbon separation sieve for separating the carbon pulp between the two sections of leaching adsorption tanks, returning the ore pulp to the original leaching adsorption tank, and retaining the activated carbon in the front leaching adsorption tank; after gold is adsorbed and saturated in the No. 3 groove, conveying the carbon slurry mixture to a No. 2 vibrating screen for carbon slurry separation, returning ore pulp to the No. 3 leaching adsorption groove, and allowing high-gold low-silver activated carbon to enter a desorption workshop;
(b) adding silver-extracting activated carbon from the No. 11 leaching adsorption tank, pumping the carbon slurry mixture forward in sequence after leaching and adsorbing for a period of time, wherein the activated carbon and the ore slurry are in mutual countercurrent, a carbon separation sieve for separating the carbon slurry is arranged between the two sections of leaching adsorption tanks, the ore slurry returns to the original leaching adsorption tank, and the activated carbon is reserved in the front leaching adsorption tank; and after the silver is adsorbed and saturated in the 8# groove, conveying the carbon slurry mixture to a 3# vibrating screen for carbon slurry separation, returning ore pulp to the 8# leaching adsorption groove, and allowing the low-gold high-silver activated carbon to enter a desorption workshop.
2. The method for efficiently extracting gold and silver from gold-bearing silver-sulfur concentrate according to claim 1,
the oxidant is hydrogen peroxide or potassium permanganate.
3. The method for efficiently extracting gold and silver from gold-bearing silver-sulfur concentrate according to claim 2,
in the step (1), adding 16-20 kg/t of lime and 1-1.5 kg/t of oxidant, and carrying out size mixing according to the liquid-solid ratio of 1: 1; the leaching tank is 0.3m at best3/（m2H); the concentration of the active carbon in the pesticide removing stirring tank is kept at 45-65 g/L.
4. The method for efficiently extracting gold and silver from gold-bearing silver-sulfur concentrate according to claim 3,
in the step (2), adding 4-6 kg/t of sodium cyanide; the aeration quantity of each leaching tank is 0.3m3/（m2H), the total leaching time is 24-36 hours; the concentration of the activated carbon in the leaching adsorption tank is kept at 15-30 g/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011292284.8A CN112251614A (en) | 2020-11-18 | 2020-11-18 | Method for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011292284.8A CN112251614A (en) | 2020-11-18 | 2020-11-18 | Method for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112251614A true CN112251614A (en) | 2021-01-22 |
Family
ID=74266882
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011292284.8A Pending CN112251614A (en) | 2020-11-18 | 2020-11-18 | Method for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112251614A (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101451192A (en) * | 2007-11-28 | 2009-06-10 | 灵宝市金源矿业有限责任公司 | Comprehensive recovery method for directly cyanating and intensified leaching multi-metal gold ore concentrate |
| CN101856635A (en) * | 2010-04-26 | 2010-10-13 | 青岛黄金铅锌开发有限公司 | Method using mineral dressing backwater to float and to recover gold, silver, lead and zinc in cyanidation tailings of gold mine |
| CN103409643A (en) * | 2013-07-19 | 2013-11-27 | 广州有色金属研究院 | Method for gold leaching of skarn gold ore |
| CN107297270A (en) * | 2017-08-10 | 2017-10-27 | 鹤庆北衙矿业有限公司 | A kind of oxysulphied ore deposit handling process |
| CN109351465A (en) * | 2018-10-19 | 2019-02-19 | 山东国大黄金股份有限公司 | A kind of method that step separates Determination of multiple metal elements in synthetical recovery Gold Concentrate under Normal Pressure |
-
2020
- 2020-11-18 CN CN202011292284.8A patent/CN112251614A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101451192A (en) * | 2007-11-28 | 2009-06-10 | 灵宝市金源矿业有限责任公司 | Comprehensive recovery method for directly cyanating and intensified leaching multi-metal gold ore concentrate |
| CN101856635A (en) * | 2010-04-26 | 2010-10-13 | 青岛黄金铅锌开发有限公司 | Method using mineral dressing backwater to float and to recover gold, silver, lead and zinc in cyanidation tailings of gold mine |
| CN103409643A (en) * | 2013-07-19 | 2013-11-27 | 广州有色金属研究院 | Method for gold leaching of skarn gold ore |
| CN107297270A (en) * | 2017-08-10 | 2017-10-27 | 鹤庆北衙矿业有限公司 | A kind of oxysulphied ore deposit handling process |
| CN109351465A (en) * | 2018-10-19 | 2019-02-19 | 山东国大黄金股份有限公司 | A kind of method that step separates Determination of multiple metal elements in synthetical recovery Gold Concentrate under Normal Pressure |
Non-Patent Citations (2)
| Title |
|---|
| 张亦飞等编著: "《现代黄金冶炼技术》", 北京：冶金工业出版社, pages: 316 * |
| 徐恩聚: "铁帽型金银矿石提金银的工艺研究", vol. 9, no. 6, pages 193 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US6355175B1 (en) | Method for separating and isolating precious metals from non precious metals dissolved in solutions | |
| US7559973B2 (en) | Precious metal recovery using thiocyanate lixiviant | |
| CN102134641B (en) | Gold extraction process of gold concentrate with high carbon, arsenic and sulfur | |
| AU2011200703B2 (en) | Method for Leaching of a Copper-containing Ore | |
| ES2940464T3 (en) | Process to recover copper and/or precious metals | |
| US5147618A (en) | Process for recovery of gold from refractory gold ores using sulfurous acid as the leaching agent | |
| MX2010002914A (en) | Controlled copper leach recovery circuit. | |
| Hedjazi et al. | Industrial application of ammonia-assisted cyanide leaching for copper-gold ores | |
| Oraby et al. | Gold dissolution and copper suppression during leaching of copper–gold gravity concentrates in caustic soda-low free cyanide solutions | |
| CN213680830U (en) | System for high-efficient gold and silver of drawing in follow auriferous silver sulphur concentrate | |
| CA1333107C (en) | Process for the detoxification of effluents from ore processing operations with hydrogen peroxide, using a magnetic pre-separation stage | |
| Sceresini et al. | Gold-copper ores | |
| CN112251614A (en) | Method for efficiently extracting gold and silver from gold-containing silver-sulfur concentrate | |
| CN106636636A (en) | Microbubble strengthened biological oxidation pretreatment method for gold concentrate difficult to deal with | |
| RU2268316C1 (en) | Method of sorption leaching of metals at reduced reagent treatment | |
| CN115927852A (en) | Method for recovering gold, silver and copper from sulfur concentrate calcine washing waste liquid | |
| US5308380A (en) | MIC oxygenation: "extraction of metals values from metals bearing ores" | |
| US5310413A (en) | Process and apparatus for extraction of metal values from metal bearing ores | |
| RU2234544C1 (en) | Method of reworking of auriferous arsenical ores and concentrates | |
| CA2008063C (en) | Hydrometallurgical leaching process and apparatus | |
| CN217796651U (en) | System for efficiently recycling valuable components in copper-and sulfur-containing complex oxidized gold and silver ores | |
| WO2020165845A1 (en) | Pre-treatment process for the recovery of precious metals | |
| US5288302A (en) | Method and apparatus for extraction of metal values from metal bearing ores | |
| CN217324228U (en) | Aerify and return thick liquid device | |
| CN114622101B (en) | Mineral separation method for comprehensively leaching and recovering gold and silver from gold and silver ore with higher sulfur content |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20210122 |
|
| RJ01 | Rejection of invention patent application after publication |