CN115261635A - Comprehensive recycling method of high-grade multi-element gold concentrate - Google Patents
Comprehensive recycling method of high-grade multi-element gold concentrate Download PDFInfo
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- CN115261635A CN115261635A CN202210917275.6A CN202210917275A CN115261635A CN 115261635 A CN115261635 A CN 115261635A CN 202210917275 A CN202210917275 A CN 202210917275A CN 115261635 A CN115261635 A CN 115261635A
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- gold
- leaching
- tailings
- silver
- concentrate
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- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 title claims abstract description 206
- 229910052737 gold Inorganic materials 0.000 title claims abstract description 186
- 239000010931 gold Substances 0.000 title claims abstract description 186
- 238000000034 method Methods 0.000 title claims abstract description 97
- 239000012141 concentrate Substances 0.000 title claims abstract description 68
- 238000004064 recycling Methods 0.000 title claims abstract description 50
- 238000002386 leaching Methods 0.000 claims abstract description 137
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims abstract description 95
- 229910052709 silver Inorganic materials 0.000 claims abstract description 84
- 239000004332 silver Substances 0.000 claims abstract description 84
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 51
- 230000008569 process Effects 0.000 claims abstract description 43
- 238000005188 flotation Methods 0.000 claims abstract description 35
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 30
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 30
- 239000011593 sulfur Substances 0.000 claims abstract description 30
- 238000000926 separation method Methods 0.000 claims abstract description 22
- 239000002994 raw material Substances 0.000 claims abstract description 21
- 238000000227 grinding Methods 0.000 claims abstract description 12
- 238000007670 refining Methods 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims description 41
- 238000006243 chemical reaction Methods 0.000 claims description 31
- 238000000967 suction filtration Methods 0.000 claims description 21
- 239000012535 impurity Substances 0.000 claims description 20
- 238000006722 reduction reaction Methods 0.000 claims description 20
- 239000007787 solid Substances 0.000 claims description 20
- 238000005406 washing Methods 0.000 claims description 19
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 18
- 239000003112 inhibitor Substances 0.000 claims description 18
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims description 17
- 230000002000 scavenging effect Effects 0.000 claims description 16
- 239000002002 slurry Substances 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 14
- 229910017604 nitric acid Inorganic materials 0.000 claims description 14
- 238000001556 precipitation Methods 0.000 claims description 13
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 12
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 11
- 238000003723 Smelting Methods 0.000 claims description 11
- 239000004571 lime Substances 0.000 claims description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 10
- QZPSXPBJTPJTSZ-UHFFFAOYSA-N aqua regia Chemical compound Cl.O[N+]([O-])=O QZPSXPBJTPJTSZ-UHFFFAOYSA-N 0.000 claims description 10
- 238000001914 filtration Methods 0.000 claims description 10
- 230000001590 oxidative effect Effects 0.000 claims description 10
- 239000011780 sodium chloride Substances 0.000 claims description 9
- HRZFUMHJMZEROT-UHFFFAOYSA-L sodium disulfite Chemical compound [Na+].[Na+].[O-]S(=O)S([O-])(=O)=O HRZFUMHJMZEROT-UHFFFAOYSA-L 0.000 claims description 9
- 235000010262 sodium metabisulphite Nutrition 0.000 claims description 9
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 8
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 8
- 238000006864 oxidative decomposition reaction Methods 0.000 claims description 8
- 238000003756 stirring Methods 0.000 claims description 8
- 239000002562 thickening agent Substances 0.000 claims description 8
- 239000003599 detergent Substances 0.000 claims description 7
- 239000011449 brick Substances 0.000 claims description 6
- TUZCOAQWCRRVIP-UHFFFAOYSA-N butoxymethanedithioic acid Chemical compound CCCCOC(S)=S TUZCOAQWCRRVIP-UHFFFAOYSA-N 0.000 claims description 6
- 239000004568 cement Substances 0.000 claims description 6
- 239000004088 foaming agent Substances 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- 235000019353 potassium silicate Nutrition 0.000 claims description 6
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical group [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 claims description 6
- 229920003063 hydroxymethyl cellulose Polymers 0.000 claims description 5
- 229940031574 hydroxymethyl cellulose Drugs 0.000 claims description 5
- 239000007791 liquid phase Substances 0.000 claims description 5
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical group OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 4
- 239000007795 chemical reaction product Substances 0.000 claims description 4
- 239000003153 chemical reaction reagent Substances 0.000 claims description 4
- 230000018044 dehydration Effects 0.000 claims description 4
- 238000006297 dehydration reaction Methods 0.000 claims description 4
- 239000012065 filter cake Substances 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 239000002245 particle Substances 0.000 claims description 4
- 239000000575 pesticide Substances 0.000 claims description 4
- 238000003825 pressing Methods 0.000 claims description 4
- 241000254137 Cicadidae Species 0.000 claims description 3
- 229920002907 Guar gum Polymers 0.000 claims description 3
- 239000000665 guar gum Substances 0.000 claims description 3
- 229960002154 guar gum Drugs 0.000 claims description 3
- 235000010417 guar gum Nutrition 0.000 claims description 3
- 238000005202 decontamination Methods 0.000 claims 1
- 238000000605 extraction Methods 0.000 abstract description 18
- 229910052500 inorganic mineral Inorganic materials 0.000 abstract description 15
- 239000011707 mineral Substances 0.000 abstract description 15
- 239000002184 metal Substances 0.000 abstract description 5
- 229910052751 metal Inorganic materials 0.000 abstract description 5
- 150000002739 metals Chemical class 0.000 abstract description 5
- 238000011084 recovery Methods 0.000 description 25
- 239000012752 auxiliary agent Substances 0.000 description 13
- 230000000052 comparative effect Effects 0.000 description 13
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- 230000008901 benefit Effects 0.000 description 7
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- 230000000694 effects Effects 0.000 description 7
- 238000011161 development Methods 0.000 description 6
- 238000012546 transfer Methods 0.000 description 6
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 230000009286 beneficial effect Effects 0.000 description 4
- 238000003912 environmental pollution Methods 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- NJRXVEJTAYWCQJ-UHFFFAOYSA-N thiomalic acid Chemical compound OC(=O)CC(S)C(O)=O NJRXVEJTAYWCQJ-UHFFFAOYSA-N 0.000 description 4
- UMGDCJDMYOKAJW-UHFFFAOYSA-N thiourea Chemical compound NC(N)=S UMGDCJDMYOKAJW-UHFFFAOYSA-N 0.000 description 4
- 241000931705 Cicada Species 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical group [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Natural products NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000002440 industrial waste Substances 0.000 description 2
- 239000011268 mixed slurry Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000010008 shearing Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 231100000331 toxic Toxicity 0.000 description 2
- 230000002588 toxic effect Effects 0.000 description 2
- 238000005303 weighing Methods 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- VGGLHLAESQEWCR-UHFFFAOYSA-N N-(hydroxymethyl)urea Chemical compound NC(=O)NCO VGGLHLAESQEWCR-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000010953 base metal Substances 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 159000000007 calcium salts Chemical class 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- -1 gold and silver Chemical class 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 150000002366 halogen compounds Chemical class 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- ZFSLODLOARCGLH-UHFFFAOYSA-N isocyanuric acid Chemical compound OC1=NC(O)=NC(O)=N1 ZFSLODLOARCGLH-UHFFFAOYSA-N 0.000 description 1
- 239000011133 lead Substances 0.000 description 1
- 231100000053 low toxicity Toxicity 0.000 description 1
- 239000002366 mineral element Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- QUBQYFYWUJJAAK-UHFFFAOYSA-N oxymethurea Chemical compound OCNC(=O)NCO QUBQYFYWUJJAAK-UHFFFAOYSA-N 0.000 description 1
- 229950005308 oxymethurea Drugs 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 239000010970 precious metal Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 229940001584 sodium metabisulfite Drugs 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- DHCDFWKWKRSZHF-UHFFFAOYSA-N sulfurothioic S-acid Chemical compound OS(O)(=O)=S DHCDFWKWKRSZHF-UHFFFAOYSA-N 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
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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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/02—Froth-flotation processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/14—Flotation machines
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/027—Recovery of sulfur from material containing elemental sulfur, e.g. luxmasses or sulfur containing ores; Purification of the recovered sulfur
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B33/00—Clay-wares
- C04B33/02—Preparing or treating the raw materials individually or as batches
- C04B33/13—Compounding ingredients
- C04B33/132—Waste materials; Refuse; Residues
- C04B33/138—Waste materials; Refuse; Residues from metallurgical processes, e.g. slag, furnace dust, galvanic waste
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/14—Cements containing slag
- C04B7/147—Metallurgical slag
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
- C22B3/065—Nitric acids or salts thereof
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
- C22B3/10—Hydrochloric acid, other halogenated acids or salts thereof
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
- C22B3/46—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes by substitution, e.g. by cementation
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- General Chemical & Material Sciences (AREA)
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Abstract
The invention provides a comprehensive recycling method of high-grade multi-element gold concentrate, belonging to the technical field of comprehensive recycling of mineral resources, comprising the following steps: grinding the raw materials by grinding and grading to obtain ground pulp; leaching the ground pulp to obtain gold mud and leached tailings; carrying out flotation treatment on the leached tailings to obtain a sulfur concentrate and flotation tailings; refining the gold mud to obtain gold ingots and silver ingots; and a harmless treatment process for performing harmless treatment on the flotation tailings. The comprehensive recycling method of the high-grade multi-element gold concentrate is used for solving the problems that the gold and silver extraction rate is low due to the fact that a mineral separation agent is not suitable in the existing high-grade multi-element gold concentrate recycling, the unit element mineral enrichment is difficult due to the complex ore properties, the extraction rate of high-value metals such as gold and silver is low, the recycling process is too long and is not easy to operate, and high-value elements such as gold, silver and sulfur are carried in tailings.
Description
Technical Field
The invention relates to the technical field of comprehensive recovery and utilization of mineral resources, in particular to a comprehensive recovery and utilization method of high-grade multi-element gold concentrate.
Background
Gold and silver are precious rare metals, are also indispensable important resources in economic development and daily life, and play a vital role in international finance, so that all countries in the world pay great attention to the production and processing of gold and silver. Along with the rapid development of economy in China, the living standard of people is continuously improved, the production and consumption of gold and silver are increased day by day, the yield value of gold and silver needs to be increased urgently, and the requirements of the current society can be met only by continuously searching, developing and utilizing new mineral resources. The comprehensive recycling of high-grade multi-element gold concentrate is the current direction.
The purposes of fully and efficiently utilizing effective mineral resources and reducing environmental pollution can be achieved by comprehensively recycling high-grade multi-element gold concentrate. However, although China takes the energy chemical industry as a support in a long period of time, a large-scale and centralized comprehensive resource recycling system is not completely established, and the contradiction between economic development and ecological environment protection is increasingly prominent. Therefore, when gold and silver are produced by using high-grade multi-element gold concentrate, comprehensive utilization of co-associated mineral resources and tailings of the gold and silver is required to be enhanced so as to continuously promote concepts of energy conservation, emission reduction and cyclic development.
The existing beneficiation methods of gold concentrate mainly comprise flotation, gravity separation, cyanidation and the like. More than 85% of gold in the world is extracted by a cyanidation method, and the technology is mature. The cyanidation method has the advantages of high gold extraction recovery rate, strong adaptability to ores, low cost and the like. The drawbacks of the cyanidation process are also quite evident: cyanide is extremely toxic, has great potential safety hazard and environmental pollution risk in the transportation, storage and use processes, and in addition, the discharge of industrial cyanide-containing waste water and solid waste can seriously pollute water sources and soil environment, destroy ecological balance and influence the body health of surrounding residents.
In order to solve the problem of severe toxic pollution of cyanide, in recent years, a great deal of research work is carried out on gold ore dressing agents at home and abroad, and cyanide-free and non-toxic dressing agents such as a thiourea method, a thiosulfate method, a hypochlorite method, halogen compounds and the like are searched in an effort. However, these beneficiation agents have the problems of high production cost, poor stability, large consumption, poor adaptability to ores and the like, and these factors restrict the difficulty in industrial popularization and application of these beneficiation agents. In addition, the ore of the raw materials such as high-grade multi-element gold concentrate has complex properties and contains various useful mineral elements, and single element is difficult to extract or remove completely, so that the single element mineral is difficult to enrich, the extraction rate of high-value metals such as gold and silver is low, the recovery process is overlong and difficult to operate, and a considerable part of elements such as gold, silver, sulfur and the like are carried in tailings, so that the comprehensive and efficient recovery of the elements such as gold, silver, sulfur and the like is difficult.
Disclosure of Invention
The invention provides a comprehensive recycling method of high-grade multi-element gold concentrate, which is used for solving the problems of low gold and silver extraction rate caused by inappropriate beneficiation agents, difficult unit element mineral enrichment caused by complex ore properties, low extraction rate of high-value metals such as gold and silver, overlong recovery flow and difficult operation, and high-value elements such as gold, silver and sulfur carried in tailings in the conventional high-grade multi-element gold concentrate recycling.
The invention provides a comprehensive recycling method of high-grade multi-element gold concentrate, which comprises the following steps: grinding and grading the raw materials to obtain ground pulp; leaching the ground pulp to obtain gold mud and leached tailings; carrying out flotation treatment on the leached tailings to obtain a sulfur concentrate and flotation tailings; refining the gold mud to obtain gold ingots and silver ingots; and a harmless treatment process for performing harmless treatment on the flotation tailings.
Further setting the grain diameter of the ground pulp to be more than or equal to 80 percent with minus 200 meshes; the leaching agent used in the leaching treatment is an environment-friendly gold extracting agent for cicadas; the replacement treatment adopts zinc powder for replacement; in the raw materials, the content of gold is more than 200.00g/t, the content of silver is more than 10.00g/t, and the content of sulfur is more than 3%.
In the invention, the raw material is high-grade multi-element gold concentrate mainly containing gold, silver, sulfur and other elements, gold and silver are leached by adopting an environment-friendly gold extracting agent in the process of comprehensive recycling, zinc powder is adopted for replacement refining, sulfur concentrate in tailings is recovered by adopting flotation, the harmless treatment of tailings is completed, the gold, the silver and the sulfur in the gold concentrate are comprehensively and integrally recovered by a multistage separation technology, and the comprehensive recovery rates of the gold, the silver and the sulfur respectively reach more than 99%, 80% and 80%.
The method achieves the purposes of fully and efficiently utilizing effective mineral resources and reducing environmental pollution, comprehensively recycles the co-associated mineral resources and tailings when the gold and silver are produced, prolongs a chain for comprehensively recycling gold concentrate resources, maximizes the utilization of the mineral resources, saves energy, protects environment, has high product quality, improves the resource recycling level, improves the resource utilization rate, does not use gold extracting agents such as cyanide and the like which are easy to cause pollution, and realizes green and environment-friendly production.
It is further provided that the leaching process comprises the steps of: feeding the ground pulp into a pre-leaching thickener for solid-liquid separation, adding a leaching agent and a pH value regulator into bottom flow pulp with the solid content of 65% obtained by solid-liquid separation, then performing leaching treatment, after the leaching is finished, performing washing separation on leached pulp obtained by leaching for 4-5 times, feeding leaching tailings obtained by washing separation into a flotation process, combining the pregnant solution obtained by washing separation with the pregnant solution obtained by solid-liquid separation in the pre-leaching thickener, then adding zinc powder into the pregnant solution for replacement treatment, replacing gold and silver from the pregnant solution, and filtering by a plate frame to obtain gold mud.
Further setting the addition amount of the leaching agent to be 300-1000g/t; the pH value regulator is lime, and the addition amount of the pH value regulator is that the pH value reaches 10-12; the leaching time is 36h; the addition amount of the zinc powder is 50-250g/t, and the particle size of the zinc powder is-325 meshes which is more than or equal to 95 percent.
The environment-friendly cicada gold extraction agent is an alkaline leaching agent, the main components of the environment-friendly cicada gold extraction agent comprise sodium carbide cyanurate, alkaline thiourea, alkaline polyferric oxide, alkali, carbonate and the like, all the components can be matched with each other in a synergistic manner to complex and dissolve gold in ores, and the gold is transferred to a liquid phase, so that the leaching effect is achieved, and the environment-friendly cicada gold extraction agent has the advantages of safety, low toxicity, high gold recovery rate, stable property and simplicity and convenience in operation.
The method is further provided with the following steps: adding 300-500g/t of activated carbon into the leaching tailings for removing the pesticide, then adding sulfuric acid to adjust the pH value of the leaching tailings to be 4.5-5.5, then adding 400-500g/t of inhibitor, 200-300g/t of collecting agent and 20-50g/t of foaming agent into the leaching tailings, and performing primary roughing to obtain rough concentrate and rough tailings; thirdly, scavenging the coarse tailings for three times, adding 100-150g/t of collecting agent in each scavenging process, and feeding scavenged tailings serving as flotation tailings into a harmless process; and (4) carrying out concentration on the rough concentrate for three times, wherein 150-300g/t of inhibitor is added in each concentration, and the concentration tailings are the sulfur concentrate.
The method is further set to be characterized in that the inhibitor is guar gum or hydroxymethyl cellulose, the collector is water glass, butyl xanthate and 2# oil in a weight ratio of 8-10; the roughing time is 5-30min, the single scavenging time is 20-60min, and the single concentration time is 20-60min.
The sulfur concentrate containing gold and silver in the leached tailings is separated by flotation, the flotation process is stable, the grade of the sulfur concentrate is high, the recovery of sulfur elements is realized, the entrainment of the sulfur concentrate to co-associated metals such as iron and the like is reduced, the comprehensive utilization value of the leached tailings is improved, and the comprehensive recovery utilization rate of the raw material gold concentrate is further improved.
The refining process is further configured to comprise the following steps: adding a nitric acid solution into the gold mud to remove impurities, adding water to perform suction filtration, wherein the solid obtained by suction filtration is crude gold powder, the obtained liquid phase is silver pregnant solution, adding aqua regia into the crude gold powder to perform gold dissolving operation, then performing suction filtration, adding sodium pyrosulfite into the obtained gold pregnant solution to perform gold reduction reaction, performing suction filtration after the reaction, and smelting the obtained gold powder to obtain gold ingots; and (3) performing precipitation reaction on the silver pregnant solution by adopting sodium chloride, performing suction filtration, adding iron powder into the obtained filter cake to perform silver reduction reaction, performing suction filtration to obtain crude silver powder, and smelting the crude silver powder to form a silver ingot.
Further setting the concentration of the nitric acid solution to be 15-30%, the solid-to-liquid ratio of the gold mud to the nitric acid solution to be 1-1.5, the impurity removal temperature to be 60-90 ℃ and the impurity removal time to be 60-200min in the impurity removal operation; in the gold dissolving operation, the solid-liquid ratio of the crude gold powder to the aqua regia is 1-2, the temperature is 50-90 ℃, and the time is 1-12h; the addition amount of sodium pyrosulfite is 0.5-1% of the weight of the gold pregnant solution, and the time of gold reduction reaction is 10-30min.
Further setting the solid-liquid ratio of the sodium chloride to the silver pregnant solution to be 1.5-3 and the precipitation time to be 40-90min in the precipitation reaction; in the silver reduction reaction, the adding amount of iron powder is 100-300g/kg, the temperature is 20-40 ℃, and the time is 3-6h; the smelting temperature of the gold powder and the crude silver powder is 1000-1200 ℃. The gold mud is refined, so that base metals such as zinc, lead, copper and the like in the gold mud can be further removed, gold and silver simple substances are separated from impurities, and the purity of gold ingots and silver ingots is improved.
The harmless process comprises the following steps: feeding the flotation tailings into a filter press for press filtration and dehydration, feeding backwater into a flotation process for recycling, feeding obtained filter residues into a stirring barrel, adding water to form filter residue slurry with the solid content of 25%, then adding a reagent removing detergent for uniform mixing, feeding the filter residue slurry into a reaction tank, introducing oxidizing gas into the reaction tank for oxidative decomposition reaction, washing reaction products after the reaction is finished, washing the obtained water for recycling, and selling the obtained tailings as a light brick raw material or a cement auxiliary material after filter pressing.
Further setting the concentration of the medicine-removing detergentHydrogen peroxide solution with the concentration of 20-30% and the addition amount of 50-300g/t; the oxidizing gas is ozone, and the ozone is introduced in an amount of 5-20m 3 H; the time of oxidative decomposition reaction is 0.5-5h.
The tailings become recyclable general industrial waste after harmless treatment, and are generally reused as light brick production raw materials or cement industry auxiliary materials, so that pollution of the tailings to the surrounding environment can be avoided, the purposes of environmental protection and emission reduction are achieved, economic benefits can be created, and the recycling development space of waste resources is expanded.
Further setting that during leaching treatment, the underflow fluid is leached under an ultrasonic environment; the ultrasonic environment is provided by sine ultrasonic wave and frequency-variable ultrasonic wave in an alternating sequence of sine-frequency-variable-sine-frequency-variable, wherein the frequency of the sine ultrasonic wave is 20-40KHz, and the power is 300mW/cm 2 (ii) a The frequency of the frequency conversion ultrasonic wave is 30-50KHz, and the power is 250mW/cm 2 。
Ultrasonic intervention is carried out during leaching, the leaching of gold and silver is promoted by utilizing the ultrasonic cavitation effect, ultrasonic waves with different frequencies and powers are adopted, the ultrasonic cavitation bubbles with different sizes can be utilized to reduce dead angles caused by standing waves, the growth and collapse of the cavitation bubbles can generate shearing force in underflow slurry, different elements on the surface of ore are dissociated in different degrees due to the difference of binding force, so that stronger collapse is generated on the surface of the ore, cracks or pores appear on the surface of the ore earlier and faster, the mass transfer speed between a leaching agent and the ore is increased, the mass transfer surface area is increased, the leaching agent is assisted to improve the gold and silver dissolving speed, the extraction rate and the yield, meanwhile, the leaching treatment time can be shortened, and the time cost is saved.
The comprehensive recycling method of the high-grade multi-element gold concentrate provided by the invention has the beneficial effects that the following beneficial effects are realized by means of recycling gold, silver and sulfur and carrying out harmless treatment on tailings:
1) In the invention, the raw material is high-grade multi-element gold concentrate mainly containing gold, silver, sulfur and other elements, gold and silver are leached by adopting an environment-friendly gold extracting agent in the process of comprehensive recycling, zinc powder is adopted for replacement and refining, sulfur concentrate in tailings is recovered by flotation, the gold, silver and sulfur in the gold concentrate are comprehensively and integrally recovered by a multi-stage separation technology, the comprehensive recovery rates of the gold, the silver and the sulfur respectively reach more than 99%, 80% and 80%, and the 'clean and dry squeezing' is realized, so that mineral resources are maximally utilized, the resource utilization rate is improved, and meanwhile, the gold extracting agent such as cyanide and the like which easily causes pollution is not used, and the green and environment-friendly production is realized.
2) The method realizes the purposes of precious metal purification and multi-element comprehensive recovery of gold concentrate, completes the harmless treatment of the tailings, recycles the harmless tailings as a light brick production raw material or a cement industry auxiliary material, avoids the pollution of the tailings to the surrounding environment, has low energy consumption and low pollution in the recovery process, and has positive and remarkable economic benefit, environmental benefit and social benefit.
3) The main products of the invention are gold ingots, silver ingots and sulfur concentrate containing gold and silver, and harmless tailings are recoverable general industrial waste, the method achieves the purposes of fully and efficiently utilizing effective mineral resources and reducing environmental pollution, and when the gold and silver are produced, the method comprehensively recycles the associated mineral resources and tailings, prolongs the chain for comprehensively utilizing the gold concentrate resources, saves energy, protects the environment, has high product quality, improves the resource recycling level, and is beneficial to actively promoting the industrial development of comprehensive utilization, waste resource recycling and the like.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and those skilled in the art can also obtain other drawings according to the drawings without creative efforts.
FIG. 1 is a diagram showing the dissolution rate of gold on a circuit board under different conditions.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention are clearly and completely described below, and it is obvious that the described embodiments are a part of the embodiments of the present invention, but not all of the embodiments. All other embodiments, which can be obtained by a person skilled in the art based on the embodiments of the present invention without any inventive step, also belong to the scope of protection of the present invention.
The comprehensive high-grade multielement gold concentrate recycling method comprises the following steps:
1) Grinding: adding water into raw materials, stirring to form raw pulp with the solid content of 20-40%, adding lime and precious liquid recycled from the leaching process into the raw pulp, stirring to form mixed pulp with the solid content of 20-25% and the pH value of more than 9, then sending the mixed pulp into a ball mill for grinding, then sending the mixed pulp into a cyclone for grading, and sending the ground pulp into the leaching process when the ground pulp obtained by grinding reaches the condition that-200 meshes are more than or equal to 80%.
2) Leaching: and (2) sending the ground pulp into a pre-leaching thickener for solid-liquid separation, then adding a leaching agent and a pH value regulator into bottom flow pulp with the solid content of 65% obtained by the solid-liquid separation, then carrying out leaching treatment, after the leaching is finished, washing and separating leached pulp obtained by the leaching for 4-5 times, sending leaching tailings obtained by the washing and separating into a flotation process, merging the precious liquid obtained by the washing and separating with the precious liquid obtained by the solid-liquid separation in the pre-leaching thickener, then adding zinc powder into the precious liquid for replacement treatment, replacing gold and silver from the precious liquid, and filtering by a plate frame to obtain gold mud.
In a specific embodiment, the leaching agent adopts an environment-friendly gold extraction agent for cicadas, and the addition amount of the environment-friendly gold extraction agent is 300-1000g/t. The pH regulator is lime, and the addition amount of the pH regulator is that the pH value reaches 10-12. The time of leaching treatment is 36h.
In the replacement treatment, the addition amount of the zinc powder is 50-250g/t, and the particle size of the zinc powder is-325 meshes which is more than or equal to 95 percent.
3) A flotation process: adding 300-500g/t of activated carbon into the leaching tailings for removing the pesticide, then adding sulfuric acid to adjust the pH value of the leaching tailings to be 4.5-5.5, then adding 400-500g/t of inhibitor, 200-300g/t of collecting agent and 20-50g/t of foaming agent into the leaching tailings, and performing primary roughing to obtain rough concentrate and rough tailings; thirdly, scavenging the coarse tailings for three times, adding 100-150g/t of collecting agent in each scavenging process, and feeding scavenged tailings serving as flotation tailings into a harmless process; and (4) carrying out concentration on the rough concentrate for three times, wherein 150-300g/t of inhibitor is added in each concentration, and the concentration tailings are the sulfur concentrate.
In a specific embodiment, the inhibitor is guar gum or hydroxymethyl cellulose, the collector is water glass, butyl xanthate and 2# oil in a weight ratio of 8-10.
The roughing time is 5-30min, the single scavenging time is 20-60min, and the single concentration time is 20-60min.
4) A refining procedure: adding a nitric acid solution into the gold mud to remove impurities, adding water to perform suction filtration, wherein the solid obtained by suction filtration is crude gold powder, the obtained liquid phase is silver pregnant solution, adding aqua regia into the crude gold powder to perform gold dissolving operation, then performing suction filtration, adding sodium pyrosulfite into the obtained gold pregnant solution to perform gold reduction reaction, performing suction filtration after the reaction, and smelting the obtained gold powder to obtain gold ingots; and (3) performing precipitation reaction on the silver pregnant solution by adopting sodium chloride, then performing suction filtration, adding iron powder into the obtained filter cake to perform silver reduction reaction, then performing suction filtration to obtain crude silver powder, and smelting the crude silver powder to form a silver ingot.
In a specific embodiment, in the impurity removal operation, the concentration of the nitric acid solution is 15-30%, the solid-to-liquid ratio of the gold mud to the nitric acid solution is 1-1.5, the impurity removal temperature is 60-90 ℃, and the impurity removal time is 60-200min.
In the gold dissolving operation, the solid-liquid ratio of the crude gold powder to the aqua regia is 1-2, the temperature is 50-90 ℃, and the time is 1-12h.
The addition amount of the sodium pyrosulfite is 0.5-1% of the weight of the gold pregnant solution, and the time of gold reduction reaction is 10-30min.
In the precipitation reaction, the solid-liquid ratio of the sodium chloride to the silver pregnant solution is 1.5-3, and the precipitation time is 40-90min.
In the silver reduction reaction, the addition amount of the iron powder is 100-300g/kg, the temperature is 20-40 ℃, and the time is 3-6h.
The smelting temperature of the gold powder and the crude silver powder is 1000-1200 ℃.
5) A harmless procedure: feeding the flotation tailings into a filter press for press filtration and dehydration, feeding backwater into a flotation process for recycling, feeding obtained filter residues into a stirring barrel, adding water to form filter residue slurry with the solid content of 25%, then adding a reagent removing detergent for uniform mixing, feeding the filter residue slurry into a reaction tank, introducing oxidizing gas into the reaction tank for oxidative decomposition reaction, washing reaction products after the reaction is finished, washing the obtained water for recycling, and selling the obtained tailings as a light brick raw material or a cement auxiliary material after filter pressing.
In a specific embodiment, the pesticide-removing detergent is a hydrogen peroxide solution with the concentration of 20-30%, and the addition amount is 50-300g/t. The oxidizing gas is ozone, and the ozone is introduced in an amount of 5-20m 3 H is used as the reference value. The time of oxidative decomposition reaction is 0.5-5h.
As an improvement to the foregoing implementation, in the leaching treatment, the underflow slurry is leached in an ultrasonic environment; the ultrasonic environment is provided by sine ultrasonic wave and frequency-variable ultrasonic wave in an alternating sequence of sine-frequency-variable-sine-frequency-variable, wherein the frequency of the sine ultrasonic wave is 20-40KHz, and the power is 300mW/cm 2 (ii) a The frequency of the frequency conversion ultrasonic wave is 30-50KHz, and the power is 250mW/cm 2 。
Ultrasonic intervention is carried out during leaching, the gold and silver are promoted to be dissolved out by utilizing the ultrasonic cavitation effect, ultrasonic waves with different frequencies and powers are adopted, the ultrasonic cavitation bubbles with different sizes can be utilized to reduce dead angles caused by standing waves, the growth and collapse of the cavitation bubbles can generate shearing force in bottom flow slurry, different elements on the surface of ore are dissociated in different degrees due to the difference of binding force, so that stronger collapse is generated on the surface of the ore, cracks or pores appear on the surface of the ore earlier and faster, the mass transfer speed between a leaching agent and the ore is increased, the mass transfer surface area is increased, the leaching agent is assisted to improve the gold and silver dissolution speed, the extraction rate and the yield, meanwhile, the leaching treatment time can be shortened, and the time cost is saved.
As a further improvement to the implementation, in the leaching treatment, 50-200g/t of leaching auxiliary agent is also added into the underflow slurry, and the leaching auxiliary agent comprises mercaptosuccinic acid and dimethylolurea in a weight ratio of 1-2.
The leaching auxiliary agent is added to be capable of being linked with elements with high activity on the surface of the ore by virtue of active groups of the leaching auxiliary agent, so that the hydrophilicity of the ore is increased, the dispersibility of the ore in the underflow fluid is better, the contact and collision chances of the ore and the leaching agent are increased, the gold element in the underflow fluid is fully complexed, the dissolving speed of gold and silver is accelerated, the leaching rate of the gold and silver is promoted, the leaching time is shortened, and the extraction rate, the recovery rate and the production efficiency of the gold and silver are improved. Meanwhile, the leaching auxiliary agent can increase the connectivity of gaps between insoluble calcium salts and ores by utilizing hydrophilicity, and effectively slow down the gold and silver leaching efficiency of the later stage of leaching treatment caused by the deposition of calcium carbonate or calcium sulfate on the surfaces of the ores by calcium ions in an alkaline environment, so that the higher leaching rate of the gold and silver can be still maintained in the later stage of the leaching treatment.
The present invention will be described in further detail with reference to examples.
Example 1:
in this example, the main components and contents of the gold concentrate raw material are shown in table 1 below.
TABLE 1 Main Components and contents (%) of gold concentrates (Au, ag units: g/t)
In this embodiment, the method for comprehensively recycling high-grade multi-element gold concentrate includes the following steps:
1) Grinding: adding water into the raw materials, stirring to form a primary pulp with the solid content of 20%, adding lime and the pregnant solution recycled from the leaching process into the primary pulp, stirring to form a mixed pulp with the solid content of 20% and the pH value of more than 9, then sending the mixed pulp into a ball mill for grinding, then sending into a swirler for grading, and sending the ground pulp into the leaching process when the ground pulp obtained by grinding reaches the condition that-200 meshes is more than or equal to 80%.
2) Leaching: feeding the ground pulp into a pre-leaching thickener for solid-liquid separation, adding 300g/t of a leaching agent-cicada environmental-friendly gold extraction agent and a pH value regulator-lime into bottom flow pulp with the solid content of 65% obtained by solid-liquid separation, regulating the pH of the bottom flow pulp to 10 by using lime, then carrying out leaching treatment for 36h, after the leaching is finished, washing and separating the leached pulp obtained by leaching for 4 times, feeding the leached tailings obtained by washing and separating into a flotation process, combining the precious liquid obtained by washing and separating with the precious liquid obtained by solid-liquid separation in the pre-leaching thickener, then adding 50g/t of zinc powder with the particle size of-325 meshes being more than or equal to 95% into the precious liquid for displacement treatment, displacing gold and silver from the precious liquid, and filtering by using a plate frame to obtain gold mud.
3) A flotation process: adding 300g/t of activated carbon into the leaching tailings for reagent removal, then adding sulfuric acid to adjust the pH value of the leaching tailings to be 4.5, then adding 400g/t of inhibitor, 200g/t of collecting agent and 20g/t of foaming agent into the leaching tailings, and performing primary roughing to obtain rough concentrate and rough tailings; thirdly, scavenging the coarse tailings for three times, adding 100g/t of collecting agent in each scavenging process, and feeding scavenged tailings serving as flotation tailings into a harmless process; and (4) carrying out concentration on the rough concentrate for three times, and adding 150g/t of inhibitor in each concentration, wherein the concentration tailings are the sulfur concentrate.
The inhibitor is Guerban, the collecting agent is water glass, butyl xanthate and No. 2 oil with the weight ratio of 8.
The roughing time is 10min, the single scavenging time is 20min, and the single selecting time is 20min.
4) A refining procedure: adding a nitric acid solution with the concentration of 15% into the gold mud according to the solid-to-liquid ratio of 1, removing impurities at the temperature of 60 ℃ for 60min, adding water for suction filtration, wherein the obtained solid is crude gold powder, the obtained liquid phase is silver pregnant solution, adding aqua regia into the crude gold powder for gold dissolving, then suction filtration, adding sodium metabisulfite accounting for 0.5% of the weight of the gold pregnant solution into the obtained gold pregnant solution for gold reduction reaction for 10min, suction filtration after the reaction, and smelting the obtained gold powder at the temperature of 1000-1200 ℃ to obtain gold ingots. In the gold dissolving operation, the solid-liquid ratio of the crude gold powder to the aqua regia is 1, the temperature is 50 ℃, and the time is 2h.
Adding sodium chloride into the silver pregnant solution according to the solid-to-liquid ratio of 1.5 for precipitation reaction for 40min, suction filtering, adding 100g/kg of iron powder into the obtained filter cake, carrying out silver reduction reaction for 3h at the temperature of 20 ℃, then suction filtering to obtain crude silver powder, and smelting the crude silver powder at the temperature of 1000-1200 ℃ to form silver ingots.
5) A harmless procedure: feeding flotation tailings into a filter press for press filtration and dehydration, feeding backwater into a flotation process for recycling, feeding obtained filter residues into a stirring barrel, adding water to form filter residue slurry with the solid content of 25%, then adding 50g/t of pesticide removal detergent-hydrogen peroxide solution with the concentration of 20%, uniformly mixing, feeding the filter residue slurry into a reaction tank, and introducing 5m of the mixture into the reaction tank 3 Oxidizing and decomposing the oxidizing gas-ozone for 5 hours, washing the reaction product after the reaction is finished, recycling the washed water, and selling the obtained tailings as a light brick raw material or a cement auxiliary material after the obtained tailings are subjected to filter pressing.
Example 2:
in this embodiment, the difference between the method for comprehensively recycling high-grade multi-element gold concentrate and embodiment 1 is only that:
1) Grinding: the solid content of the primary pulp is 40%, then lime and precious liquid recycled from the leaching process are added into the primary pulp, and the primary pulp is stirred to form mixed pulp with the solid content of 25% and the pH value of more than 9.
2) Leaching: the amount of a leaching agent-cicada environmental-friendly gold extraction agent added into the underflow slurry is 1000g/t, and the pH value of the underflow slurry is adjusted to 12 by a pH value adjusting agent-lime; in the replacement treatment, 250g/t of zinc powder is added to the pregnant solution.
3) A flotation process: the adding amount of the active carbon is 500 g/l, and the pH value of the tailings is adjusted to 5.5 by sulfuric acid; during rough concentration, 500g/t of inhibitor, 300g/t of collecting agent and 50g/t of foaming agent are added, and the rough concentration time is 30min; adding 150g/t of collecting agent for each scavenging, wherein the time for single scavenging is 60min; 300g/t inhibitor was added for each concentration, and the time for a single concentration was 60min.
The inhibitor is hydroxymethyl cellulose, the collector is water glass, butyl xanthate and 2# oil in a weight ratio of 10.
4) A refining procedure: in the impurity removal operation, the concentration of the nitric acid solution is 30%, the solid-to-liquid ratio of the gold mud to the nitric acid solution is 1.5, the impurity removal temperature is 90 ℃, and the impurity removal time is 200min. In the gold dissolving operation, the solid-liquid ratio of the crude gold powder to the aqua regia is 1. The addition amount of sodium pyrosulfite is 1 percent of the weight of the gold pregnant solution, and the time of gold reduction reaction is 30min. In the precipitation reaction, the solid-liquid ratio of the sodium chloride to the silver pregnant solution is 1. In the silver reduction reaction, the addition amount of iron powder is 300g/kg, the temperature is 40 ℃, and the time is 6 hours.
5) A harmless procedure: the pesticide-removing detergent is 30% hydrogen peroxide solution, and the addition amount is 300g/t. The oxidizing gas is ozone, and the ozone is introduced at a flow rate of 20m 3 H is the ratio of the total weight of the catalyst to the total weight of the catalyst. The time of oxidative decomposition reaction is 0.5h.
Example 3:
in this embodiment, the difference between the method for comprehensively recycling high-grade multi-element gold concentrate and embodiment 1 is only that:
1) Grinding: the solid content of the primary pulp is 30%, then lime and precious liquid recycled from the leaching process are added into the primary pulp, and the primary pulp is stirred to form mixed pulp with the solid content of 23% and the pH value of more than 9.
2) Leaching: the amount of a leaching agent-cicada environmental-friendly gold extracting agent added into the underflow slurry is 850g/t, and the pH value of the underflow slurry is adjusted to 11 by a pH value adjusting agent-lime; in the replacement treatment, 200g/t of zinc powder is added into the pregnant solution.
3) A flotation process: the adding amount of the active carbon is 450 g/and the pH value of the tailings is adjusted to 5 by sulfuric acid; during rough concentration, 450g/t of inhibitor, 230g/t of collector and 25g/t of foaming agent are added, and the rough concentration time is 20min; adding 140g/t of collecting agent in each scavenging, wherein the scavenging time of each time is 40min; 200g/t inhibitor is added for each concentration, and the time of a single concentration is 40min.
The inhibitor is hydroxymethyl cellulose, the collecting agent is water glass, butyl xanthate and No. 2 oil in a weight ratio of 8.5.
4) A refining procedure: in the impurity removal operation, the concentration of the nitric acid solution is 20%, the solid-to-liquid ratio of the gold mud to the nitric acid solution is 1.5, the impurity removal temperature is 70 ℃, and the impurity removal time is 100min. In the gold dissolving operation, the solid-liquid ratio of the crude gold powder to the aqua regia is 1.5, the temperature is 90 ℃, and the time is 6h. The addition amount of sodium pyrosulfite is 0.8% of the weight of the gold pregnant solution, and the time of gold reduction reaction is 30min. In the precipitation reaction, the solid-liquid ratio of the sodium chloride to the silver pregnant solution is 1.5, and the precipitation time is 60min. In the silver reduction reaction, the addition amount of the iron powder is 180g/kg, the temperature is 35 ℃, and the time is 4.5h.
5) A harmless procedure: the pesticide-removing detergent is 25% hydrogen peroxide solution, and the addition amount is 200g/t. The oxidizing gas is ozone, and the ozone is introduced at a flow rate of 15m 3 H is used as the reference value. The time of oxidative decomposition reaction is 2.5h.
Example 4:
in this embodiment, the difference between the method for comprehensively recycling high-grade multi-element gold concentrate and embodiment 3 is only that:
2) Leaching: during leaching treatment, the underflow fluid is leached under an ultrasonic environment; the ultrasonic environment is provided by sine ultrasonic wave and frequency conversion ultrasonic wave in alternating sequence of sine-frequency conversion-sine-frequency conversion, the frequency of the sine ultrasonic wave is 30KHz, and the power is 300mW/cm 2 (ii) a The frequency of the frequency conversion ultrasonic wave is 45KHz, and the power is 250mW/cm 2 。
Example 5:
in this embodiment, the difference between the method for comprehensively recycling high-grade multielement gold concentrate and embodiment 3 is only that:
2) Leaching: in the leaching treatment, 120g/t of leaching auxiliary agent is also added into the bottom stream, and the leaching auxiliary agent comprises mercaptosuccinic acid and dimethyloluamide with the weight ratio of 1.
Example 6:
in this embodiment, the difference between the method for comprehensively recycling high-grade multi-element gold concentrate and embodiment 4 is only that:
2) Leaching: in the leaching treatment, 120g/t of leaching auxiliary agent is also added into the bottom stream, and the leaching auxiliary agent comprises mercaptosuccinic acid and dimethyloluamide with the weight ratio of 1.
Comparative example 1:
in this embodiment, the difference between the method for comprehensively recycling high-grade multi-element gold concentrate and embodiment 3 is only that:
2) Leaching: leaching outDuring treatment, the bottom flow is leached under an ultrasonic environment; the ultrasonic environment is provided by sine ultrasonic wave with frequency of 30KHz and power of 300mW/cm 2 。
Comparative example 2:
in this embodiment, the difference between the method for comprehensively recycling high-grade multi-element gold concentrate and embodiment 4 is only that:
2) Leaching: during leaching treatment, 120g/t of leaching aid is also added into the bottom stream, and the leaching aid is mercaptosuccinic acid.
Comparative example 3:
in this embodiment, the difference between the method for comprehensively recycling high-grade multi-element gold concentrate and embodiment 4 is only that:
2) Leaching: during leaching treatment, 120g/t of leaching auxiliary agent is also added into the bottom flow pulp, and the leaching auxiliary agent is the hydroxymethyl urea.
Test example 1:
evaluating production indexes: the comprehensive recovery of gold concentrate was carried out according to the methods of example 3-example 6 and comparative example 1-comparative example 3, respectively, and the recovery rates of the finally obtained products (gold ingot, silver ingot, sulfur concentrate) were uniformly measured and calculated using the raw material of example 1 as a uniform raw material, and the results are shown in table 2. Each example and comparative example was provided with 3 sets of replicates and averaged.
TABLE 2 quality index of products of different processes
From the comparison of the results, the recovery rate of gold, silver and sulfur shows significant difference due to different methods, wherein, the recovery rate of the example 4 and the recovery rate of the example 5 are better than that of the example 3 and the recovery rate of the example 6 are optimal; the results of comparative example 1 are better than example 3, but worse than example 4; the results of comparative example 2 and comparative example 3 are better than example 4, but worse than example 6. It is shown that, on the basis of example 3, the recovery method is optimized to improve the recovery rate of the main element (gold and silver), and the recovery rate of sulfur element is not greatly influenced, such as the effect of adopting ultrasonic waves with different frequencies and powers in example 4 is better than the effect of single ultrasonic wave in comparative example 1; example 5 also improves the recovery of gold and silver by using leaching aids, but compared with example 6, the effect of combining ultrasonic leaching and leaching aids in example 6 is found to be the best.
Test example 2:
leaching Rate test
The test method comprises the following steps: carrying out leaching tests according to parameters related to the leaching procedure in the methods of the examples 3-6 and the comparative examples 1-3 respectively, preparing mixed slurry of a leaching agent and a pH value regulator, taking gold-containing waste circuit boards as raw materials, respectively putting the circuit boards into each group of mixed slurry, carrying out leaching operation according to the parameters of leaching treatment in each group of methods, taking out and weighing the circuit boards at intervals, taking the weight difference as a weighing value of the dissolving speed, simultaneously observing the dissolving condition of gold on the circuit boards, and comparing the dissolving speed of the gold in the whole leaching treatment process. Each example and comparative example was provided with 3 sets of replicates and averaged. The results are shown in FIG. 1.
It was observed that example 6 first started to dissolve, example 4 started to dissolve after 10min, and then comparative examples 2 and 3 after 17min, and then example 5 and comparative example 1 started to dissolve after 13min, and example 3 finally started to dissolve, and at 6.5h in total, all gold on the circuit board was substantially not dissolved.
FIG. 1 is a diagram showing the dissolution rate of gold on a circuit board under different conditions. As can be seen from the results of fig. 1 and observation, the dissolution rate of example 6 is the fastest, and the dissolution rate of example 3 is the slowest, and it is found by comparing examples 3, 4 and 6 that the dissolution rate of example 6 is still very fast at the later stage of the leaching treatment, while the dissolution rates of examples 3 and 4 are in a significantly decreasing trend at the later stage.
Comprehensively, ultrasonic intervention is carried out by adopting ultrasonic waves with different frequencies and powers during leaching treatment, so that cracks or pores can appear on the surface of the ore earlier and faster, the mass transfer speed between the leaching agent and the ore is increased, the mass transfer surface area is increased, the leaching agent is assisted to improve the dissolving speed, the extraction rate and the yield of gold and silver, and the leaching treatment time can be shortened. Meanwhile, the addition of the leaching auxiliary agent increases the contact and collision opportunities of the ore and the leaching agent, so that the dissolving speed of gold and silver is increased, the leaching rate of gold and silver is promoted, the leaching time is shortened, and the leaching auxiliary agent can keep the leaching rate of gold and silver higher in the later stage of leaching treatment, thereby being beneficial to improving the extraction rate, recovery rate and production efficiency of gold and silver.
It should be noted that, in the present invention, concentrations, ratios, and the like which are not specifically described are weight concentrations, weight ratios, and the like, which belong to the common writing habits of those skilled in the art, and therefore, are not described in detail herein.
It should be noted that, in the present invention, specific details of a part of operations are not described in detail, but belong to the prior art known to those skilled in the art, and therefore, are not described herein again.
Finally, it should be noted that the above embodiments are only used for illustrating the technical solutions of the present invention, and not for limiting the same; while the invention has been described in detail and with reference to the foregoing embodiments, those skilled in the art will appreciate that; the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and these modifications or substitutions do not depart from the spirit of the corresponding technical solutions of the embodiments of the present invention.
Claims (10)
1. A comprehensive recycling method of high-grade multi-element gold concentrate is characterized by comprising the following steps: grinding and grading the raw materials to obtain ground pulp; a leaching process of leaching and replacing the ground pulp to obtain gold mud and leaching tailings; performing flotation treatment on the leached tailings to obtain a sulfur concentrate and flotation tailings; refining the gold mud to obtain gold ingots and silver ingots; and a harmless treatment step of performing harmless treatment on the flotation tailings;
the grain size of the ground pulp is-200 meshes and is more than or equal to 80 percent;
the leaching agent used in the leaching treatment is an environment-friendly gold extracting agent for cicadas; the replacement treatment adopts zinc powder for replacement;
in the raw materials, the content of gold is more than 200.00g/t, the content of silver is more than 10.00g/t, and the content of sulfur is more than 3%.
2. The method for comprehensively recycling high-grade multi-element gold concentrate according to claim 1, characterized by comprising the following steps: the leaching process comprises the following steps: feeding the ground pulp into a pre-leaching thickener for solid-liquid separation, adding a leaching agent and a pH value regulator into bottom flow pulp with the solid content of 65% obtained by solid-liquid separation, then performing leaching treatment, after the leaching is finished, performing washing separation on leached pulp obtained by leaching for 4-5 times, feeding leaching tailings obtained by washing separation into a flotation process, combining the pregnant solution obtained by washing separation with the pregnant solution obtained by solid-liquid separation in the pre-leaching thickener, then adding zinc powder into the pregnant solution for replacement treatment, replacing gold and silver from the pregnant solution, and filtering by a plate frame to obtain gold mud.
3. The method for comprehensively recycling high-grade multielement gold concentrate according to claim 2, characterized by comprising the following steps: the addition amount of the leaching agent is 300-1000g/t; the pH value regulator is lime, and the addition amount of the pH value regulator is that the pH value reaches 10-12; the leaching treatment time is 36h; the addition amount of the zinc powder is 50-250g/t, and the particle size of the zinc powder is-325 meshes which is more than or equal to 95%.
4. The method for comprehensively recycling high-grade multi-element gold concentrate according to claim 1, characterized by comprising the following steps: the flotation process comprises the following steps: adding 300-500g/t of activated carbon into the leaching tailings for pesticide removal, then adding sulfuric acid to adjust the pH value of the leaching tailings to be 4.5-5.5, then adding 400-500g/t of inhibitor, 200-300g/t of collecting agent and 20-50g/t of foaming agent into the leaching tailings, and carrying out primary roughing to obtain coarse concentrate and coarse tailings; thirdly, scavenging the coarse tailings for three times, adding 100-150g/t of collecting agent in each scavenging process, and feeding scavenged tailings serving as flotation tailings into a harmless process; and (4) carrying out concentration on the rough concentrate for three times, wherein 150-300g/t of inhibitor is added in each concentration, and the concentration tailings are the sulfur concentrate.
5. The method for comprehensively recycling high-grade multi-element gold concentrate according to claim 4, characterized by comprising the following steps: the inhibitor is guar gum or hydroxymethyl cellulose, the collector is water glass, butyl xanthate and 2# oil in a weight ratio of 8-10;
the roughing time is 5-30min, the single scavenging time is 20-60min, and the single concentration time is 20-60min.
6. The method for comprehensively recycling high-grade multi-element gold concentrate according to claim 1, characterized by comprising the following steps: the refining process comprises the following steps: adding a nitric acid solution into the gold mud to remove impurities, adding water to perform suction filtration, wherein the solid obtained by suction filtration is crude gold powder, the obtained liquid phase is silver pregnant solution, adding aqua regia into the crude gold powder to perform gold dissolving operation, then performing suction filtration, adding sodium pyrosulfite into the obtained gold pregnant solution to perform gold reduction reaction, performing suction filtration after the reaction, and smelting the obtained gold powder to obtain gold ingots;
and (3) performing precipitation reaction on the silver pregnant solution by adopting sodium chloride, performing suction filtration, adding iron powder into the obtained filter cake to perform silver reduction reaction, performing suction filtration to obtain crude silver powder, and smelting the crude silver powder to form a silver ingot.
7. The method for comprehensively recycling high-grade multielement gold concentrate according to claim 6, characterized by comprising the following steps: in the impurity removal operation, the concentration of the nitric acid solution is 15-30%, the solid-to-liquid ratio of the gold mud to the nitric acid solution is 1-1.5, the impurity removal temperature is 60-90 ℃, and the impurity removal time is 60-200min;
in the gold dissolving operation, the solid-liquid ratio of the crude gold powder to the aqua regia is 1-2, the temperature is 50-90 ℃, and the time is 1-12h;
the addition amount of the sodium pyrosulfite is 0.5-1% of the weight of the gold pregnant solution, and the time of gold reduction reaction is 10-30min;
in the precipitation reaction, the solid-liquid ratio of the sodium chloride to the silver pregnant solution is 1.5-3, and the precipitation time is 40-90min;
in the silver reduction reaction, the adding amount of iron powder is 100-300g/kg, the temperature is 20-40 ℃, and the time is 3-6h;
the smelting temperature of the gold powder and the coarse silver powder is 1000-1200 ℃.
8. The method for comprehensively recycling high-grade multielement gold concentrate according to claim 1, characterized by comprising the following steps: the steps of the decontamination process are as follows: feeding the flotation tailings into a filter press for press filtration and dehydration, feeding backwater into a flotation process for recycling, feeding obtained filter residues into a stirring barrel, adding water to form filter residue slurry with the solid content of 25%, then adding a reagent removing detergent for uniform mixing, feeding the filter residue slurry into a reaction tank, introducing oxidizing gas into the reaction tank for oxidative decomposition reaction, washing reaction products after the reaction is finished, washing the obtained water for recycling, and selling the obtained tailings as a light brick raw material or a cement auxiliary material after filter pressing.
9. The method for comprehensively recycling high-grade multi-element gold concentrate according to claim 8, characterized by comprising the following steps: the pesticide-removing detergent is a hydrogen peroxide solution with the concentration of 20-30%, and the addition amount is 50-300g/t; the oxidizing gas is ozone, and the introduction amount of the ozone is 5-20m 3 H; the time of the oxidative decomposition reaction is 0.5-5h.
10. The method for comprehensively recycling high-grade multielement gold concentrate according to any one of claims 1 to 9, characterized by comprising the following steps: during the leaching treatment, the bottom flow is leached under an ultrasonic environment; the ultrasonic environment is provided by sine ultrasonic wave and frequency-changing ultrasonic wave in an alternating sequence of sine-frequency-changing-sine-frequency-changing, the frequency of the sine ultrasonic wave is 20-40KHz, and the power is 300mW/cm 2 (ii) a The frequency of the frequency conversion ultrasonic wave is 30-50KHz, and the power is 250mW/cm 2 。
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| CN117947282A (en) * | 2024-03-26 | 2024-04-30 | 中国矿业大学(北京) | Heap leaching method and heap leaching device for improving gold ore leaching efficiency |
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| AU2021104912A4 (en) * | 2021-08-04 | 2021-09-30 | Dawei Feng | Method for Recovering Gold from Auriferous Tailings |
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| CN117947282A (en) * | 2024-03-26 | 2024-04-30 | 中国矿业大学(北京) | Heap leaching method and heap leaching device for improving gold ore leaching efficiency |
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