WO2014156349A1 - Procédé de récupération d'or à partir de minerai de sulfure - Google Patents

Procédé de récupération d'or à partir de minerai de sulfure Download PDF

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WO2014156349A1
WO2014156349A1 PCT/JP2014/053192 JP2014053192W WO2014156349A1 WO 2014156349 A1 WO2014156349 A1 WO 2014156349A1 JP 2014053192 W JP2014053192 W JP 2014053192W WO 2014156349 A1 WO2014156349 A1 WO 2014156349A1
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gold
leaching
copper
ions
chloride
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PCT/JP2014/053192
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English (en)
Japanese (ja)
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和浩 波多野
浩至 勝川
佐野　正樹
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Jx日鉱日石金属株式会社
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Priority to AU2014245389A priority Critical patent/AU2014245389B2/en
Priority to CA2908688A priority patent/CA2908688C/fr
Publication of WO2014156349A1 publication Critical patent/WO2014156349A1/fr

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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
    • C22B3/22—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
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B11/00—Obtaining noble metals
    • C22B11/04—Obtaining noble metals by wet processes
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
    • 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

Definitions

  • the present invention relates to a method for recovering gold from sulfide minerals.
  • alkali metal or alkaline earth metal chlorides and bromides and copper and iron chlorides or bromides are used, and the gold leaching process is performed on the residue after the copper leaching process.
  • An implementation method is known (Japanese Patent Laid-Open No. 2009-235519). According to this method, it is said that copper and gold in copper sulfide ore can be leached and recovered at a high leaching rate only by using air without using a special oxidizing agent.
  • the technique described in the above document proposes a commercially feasible technique for a method for recovering copper and gold by a wet method from sulfide ore, but improves the separation efficiency of copper and gold and improves the recovery rate of gold. There is still room for improvement.
  • the accompanying gold is separated and concentrated in advance to a residue and then leached in a halogen bath, or leached in a halogen bath at the same time as the main component ore leaching. Remains a gold complex having a halide as a ligand.
  • the gold complex is adsorbed and recovered on activated carbon, the yield increases as the amount of adsorption increases.
  • the activated carbon is incinerated, the amount of adsorption per unit activated carbon weight directly affects the production cost and has a great effect.
  • Patent Documents 1 and 2 have been studied for improving the activated carbon adsorption property of gold, and generally the type of activated carbon and after leaching. There is a problem such as liquid contamination, and an appropriate method is not known.
  • an object of the present invention is to provide a method for recovering gold from sulfide minerals that can improve the separation efficiency of copper and gold and increase the amount of gold adsorbed on activated carbon.
  • the present inventor found that after gold leaching, when gold was adsorbed using activated carbon to the gold leaching solution after raising the redox potential in the gold leaching process and sufficiently leaching the gold leaching. It was found that monovalent copper ions in the liquid became a competitive adsorbate to activated carbon. And it discovered that the adsorption amount of gold
  • a first acidic aqueous solution containing chlorine ions, copper ions and iron ions and not containing bromine ions is brought into contact with a sulfide mineral under the supply of an oxidant, whereby the copper component in the sulfide mineral is obtained.
  • Step 2 for leaching Step 2 for separating the leaching reaction liquid obtained in Step 1 into a leaching residue and a liquid after leaching by solid-liquid separation, and a second containing chlorine ions, bromine ions, copper ions and iron ions
  • An acidic aqueous solution is brought into contact with the leaching residue obtained in step 2 under the supply of an oxidizing agent, and the gold component in the residue is leached, and the post-gold leaching solution obtained in step 3 is added to cuprous chloride.
  • an oxidizing agent is added to adjust the redox potential to 520 mV or more to reduce monovalent copper ions in the solution after gold leaching, and in the solution after gold leaching obtained in step 4 Step 5 for adsorbing gold on activated carbon
  • the method for recovering gold from sulfide mineral according to the present invention includes adjusting the oxidation-reduction potential (reference electrode, silver / silver chloride) from 520 mV to 570 mV.
  • step 4 includes adjusting the redox potential by blowing air.
  • a method for recovering gold from sulfide mineral that can increase the amount of gold adsorbed on activated carbon can be provided. Furthermore, it is possible to economically improve the separation efficiency of copper and gold by using a leachate not containing bromine ions in the copper leaching process, and use a leachate containing bromine ions in the subsequent gold leaching process. By doing so, a high gold recovery rate can be obtained.
  • step 1 a leaching solution (first acidic aqueous solution) containing chlorine ions, copper ions and iron ions and not containing bromine ions is brought into contact with the sulfide mineral under the supply of an oxidizing agent, and the copper component in the sulfide mineral is then removed.
  • Leaching That is, in step 1, copper in the sulfide mineral is leached by using a chloride bath as the leaching solution, and copper ions and iron ions generally contained in the sulfide mineral are allowed to exist in the leaching solution. It aims to promote the leaching reaction of copper.
  • the contact method between the leachate and the sulfide mineral is not particularly limited, and there are methods such as spraying and dipping. From the viewpoint of reaction efficiency, a method in which the sulfide mineral is immersed in the leachate and stirred is preferred.
  • a sulfide mineral typically, the copper sulfide ore containing the silicate ore containing the primary copper sulfide ore containing gold
  • money is mentioned.
  • the supply source of chlorine ions is not particularly limited, and examples thereof include hydrogen chloride, hydrochloric acid, metal chloride, and chlorine gas. In consideration of economy and safety, supply in the form of metal chloride is preferable.
  • the metal chloride include copper chloride (cuprous chloride, cupric chloride), iron chloride (ferrous chloride, ferric chloride), and alkali metals (lithium, sodium, potassium, rubidium, cesium, francium). Chlorides and chlorides of alkaline earth metals (beryllium, magnesium, calcium, strontium, barium, radium) can be mentioned, and sodium chloride is preferable from the viewpoint of economy and availability.
  • it can utilize also as a supply source of copper ion and iron ion, it is also preferable to utilize copper chloride and iron chloride.
  • Copper ions and iron ions are usually supplied in the form of these salts.
  • they can be supplied in the form of halide salts.
  • copper ions and iron ions are preferably supplied as copper chloride and iron chloride.
  • copper chloride and iron chloride it is desirable to use cupric chloride (CuCl 2 ) and ferric chloride (FeCl 3 ) from the viewpoint of oxidizing power, respectively, but cuprous chloride (CuCl) and ferrous chloride are preferable.
  • the concentration of chlorine ions in the leachate (first acidic aqueous solution) used in step 1 is preferably 70 g / L or more, and 140 g / L or more from the viewpoint of realizing a copper dissolution reaction with high efficiency. It is more preferable.
  • the leaching solution In order to increase the leaching efficiency of copper from sulfide minerals, the leaching solution should be acidic, and since it can be used as a supply source of chloride ions, it is preferable to make it acidic with hydrochloric acid.
  • the pH of the leaching solution is preferably about 0 to 3 and more preferably about 1.0 to 2.0 for securing the solubility of the leached copper.
  • the oxidation-reduction potential (reference electrode, silver / silver chloride) of the leaching solution at the start of Step 1 is preferably 500 mV or more, more preferably 550 mV or more from the viewpoint of promoting copper leaching.
  • the leachate (first acidic aqueous solution) used in step 1 does not contain bromine ions. This is because if bromine ions are contained in the leaching solution, the oxidation-reduction potential at which gold leaching starts decreases, so that the overlap region where gold leaching starts while copper leaching does not proceed sufficiently increases. In other words, in the present invention, since the leaching solution (first acidic aqueous solution) used in step 1 does not contain bromine ions, the redox potential at the end point of the copper leaching step is increased while suppressing gold leaching. , Copper leaching efficiency can be increased.
  • a mixture of hydrochloric acid, cupric chloride, ferric chloride and sodium chloride can be used as the leachate (first acidic aqueous solution) in step 1.
  • the copper leaching process of step 1 is performed while supplying an oxidizing agent, thereby managing the redox potential. If an oxidizing agent is not added, the redox potential is lowered in the middle, and the leaching reaction does not proceed.
  • an oxidizing agent For example, oxygen, air, chlorine, hydrogen peroxide, etc. are mentioned. However, it is not preferable to use a bromine compound as the oxidizing agent. An oxidant with an extremely high redox potential is not necessary and air is sufficient. Air is also preferable from the viewpoint of economy and safety.
  • the temperature of the leachate used in step 1 is preferably 60 ° C. or higher, more preferably 70 to 90 ° C., from the viewpoint of leaching efficiency and material of the apparatus. It is possible to carry out step 1 under pressure for the purpose of increasing the leaching efficiency, but it is sufficient under atmospheric pressure. In order to promote copper leaching, it is preferable to previously grind and grind the sulfide mineral to be treated.
  • step 1 Taking chalcopyrite, which is a typical copper sulfide mineral, as an example, in step 1, it is considered that copper leaching occurs according to the following reaction formula.
  • the cuprous chloride and ferrous chloride generated as a result of these leaching reactions in parallel with the progress of the reaction of formula (1) or formula (2) are as follows: In a simple reaction, they are oxidized to cupric chloride and ferric chloride, respectively.
  • the leachate used in Step 1 initially has a high redox potential (reference electrode, silver / silver chloride) (eg, 500 mV or higher), but when it comes into contact with a sulfide mineral and starts the leaching reaction, the redox potential is Plummet. Thereafter, the oxidation-reduction potential gradually increases as the copper leaching reaction proceeds under the supply of the oxidizing agent. In the case of the above leaching solution not containing bromine ions, copper is sufficiently leached if the oxidation-reduction potential (reference electrode, silver / silver chloride) is 450 mV or higher.
  • redox potential reference electrode, silver / silver chloride
  • the oxidation-reduction potential when the oxidation-reduction potential is increased, gold leaching starts, but in the case of the above-described leaching solution not containing bromine ions, most of the gold is present if the oxidation-reduction potential (reference electrode, silver / silver chloride) is 500 mV or less. Does not leach. Therefore, when the redox potential (reference electrode, silver / silver chloride) is in the range of 450 to 500 mV, and preferably in the range of 450 to 475 mV, the copper leaching reaction in step 1 is completed, so that the high separation efficiency of copper and gold can be achieved. It will be obtained.
  • step 1 can be completed when the leaching rate of copper is 90% by mass or more and the leaching rate of gold is 10% by mass or less, In a more preferred embodiment, Step 1 can be completed when the copper leaching rate is 95% by mass or more and the gold leaching rate is 10% by mass or less.
  • Step 2 Solid-liquid separation step>
  • the leaching reaction liquid obtained in step 1 is separated into a leaching residue and a liquid after leaching by solid-liquid separation.
  • the solid-liquid separation method is not particularly limited, but a filter press or thickener can be used. Gold remains in the leaching residue, and copper is dissolved in the liquid after leaching.
  • Process 1 can be a copper leaching process in one stage, but the copper leaching process can be performed in a plurality of stages in order to sufficiently leached copper in the sulfide mineral. Specifically, in the copper leaching process using multiple stages, after completing the copper leaching operation in the first stage, solid-liquid separation is performed with a filter press or thickener, and the next stage copper leaching operation is performed on the leaching residue. Can be implemented. Typically, the copper leaching process can consist of 2 to 4 stages. In this case, the solid-liquid separation operation performed at each leaching stage corresponds to step 2.
  • step 3 a leachate (second acidic aqueous solution) containing chlorine ions, bromine ions, copper ions and iron ions was obtained in step 2 under the supply of an oxidizing agent (step 1 was performed in multiple stages, step 2 When it is carried out a plurality of times, it is brought into contact with the leaching residue (which is finally obtained) and the gold component in the residue is leached.
  • Gold leaching proceeds by the elution of gold reacting with chlorine ions or bromine ions to form gold chloride complexes or gold bromide complexes. By using bromine ions in combination, the complex is formed at a lower potential, so that the gold leaching efficiency can be improved.
  • iron ions function to oxidize gold by trivalent iron ions oxidized under the supply of an oxidizing agent or trivalent iron ions from the beginning. Copper ions are not directly involved in the reaction, but the presence of copper ions increases the oxidation rate of iron ions.
  • the method of contacting the leachate with the residue is not particularly limited, and there are methods such as spraying and dipping. From the viewpoint of reaction efficiency, a method of immersing the residue in the leachate and stirring is preferred.
  • the supply source of chlorine ions is not particularly limited, and examples thereof include hydrogen chloride, hydrochloric acid, metal chloride, and chlorine gas. In consideration of economy and safety, supply in the form of metal chloride is preferable.
  • the metal chloride include copper chloride (cuprous chloride, cupric chloride), iron chloride (ferrous chloride, ferric chloride), and alkali metals (lithium, sodium, potassium, rubidium, cesium, francium). Chlorides and chlorides of alkaline earth metals (beryllium, magnesium, calcium, strontium, barium, radium) can be mentioned, and sodium chloride is preferable from the viewpoint of economy and availability.
  • it can utilize also as a supply source of copper ion and iron ion, it is also preferable to utilize copper chloride and iron chloride.
  • the bromine ion supply source is not particularly limited, and examples thereof include hydrogen bromide, hydrobromic acid, metal bromide, bromine gas, and the like. In consideration of economy and safety, it is in the form of metal bromide. It is preferable to supply.
  • the metal bromide include copper bromide (cuprous bromide, cupric bromide), iron bromide (ferrous bromide, ferric bromide), alkali metals (lithium, sodium, potassium, Examples thereof include bromides of rubidium, cesium, and francium) and bromides of alkaline earth metals (beryllium, magnesium, calcium, strontium, barium, and radium), and sodium bromide is preferable from the viewpoint of economy and availability.
  • it can utilize also as a supply source of copper ion and iron ion, it is also preferable to utilize copper bromide and iron bromide.
  • the supply source of copper ions and iron ions is usually supplied in the form of these salts.
  • it can be supplied in the form of a halide salt.
  • copper ions are preferably supplied as copper chloride and / or copper bromide
  • iron ions are preferably supplied as iron chloride and / or iron bromide.
  • copper chloride and iron chloride it is preferable to use cupric chloride (CuCl 2 ) and ferric chloride (FeCl 3 ) from the viewpoint of oxidizing power, respectively, but cuprous chloride (CuCl) and ferrous chloride are preferable. Even if (FeCl 2 ) is used, there is no great difference.
  • the concentration of chlorine ions in the leachate (second acidic aqueous solution) used in step 3 can be 30 to 200 g / L, but may be lower than that of the first acidic aqueous solution, and 30 g / L to 125 g. / L may be used.
  • the concentration of bromine ions in the leachate (second acidic aqueous solution) used in step 3 is preferably 1 g / L to 100 g / L from the viewpoint of reaction rate and solubility.
  • the weight concentration ratio of bromine ions to chlorine ions in the second acidic aqueous solution is preferably 1 or more, but since the gold concentration is sufficiently low, special considerations are do not need.
  • the oxidation-reduction potential (reference electrode, silver / silver chloride) of the leaching solution at the start of Step 3 is preferably 550 mV or more, more preferably 600 mV or more from the viewpoint of promoting gold leaching.
  • At least hydrochloric acid and bromic acid are selected on the condition that the leachate (second acidic aqueous solution) in step 3 is selected to contain both chlorine ions and bromine ions.
  • the leachate (second acidic aqueous solution) in step 3 is selected to contain both chlorine ions and bromine ions.
  • a mixture containing at least one of cupric chloride and cupric bromide, at least one of ferric chloride and ferric bromide, and at least one of sodium chloride and sodium bromide is used. be able to.
  • the gold leaching step of step 3 is performed while supplying the oxidizing agent, thereby managing the redox potential. If an oxidizing agent is not added, the redox potential is lowered in the middle, and the leaching reaction does not proceed.
  • an oxidizing agent For example, oxygen, air, chlorine, a bromine, hydrogen peroxide, etc. are mentioned. An oxidant with an extremely high redox potential is not necessary and air is sufficient. Air is also preferable from the viewpoint of economy and safety.
  • the oxidation-reduction potential of the solution after gold leaching after sufficient gold leaching is about 500 to 520 mV.
  • CuCl is further added and stirred, and once the oxidation-reduction potential is lowered to 520 mV or less, more preferably 500 mV or less, an oxidizing agent is added to again adjust the ORP to 520 mV or more.
  • monovalent copper ions in the solution after gold leaching which inhibits the adsorption of gold by activated carbon, are oxidized and reduced to divalent copper ions, and there are fewer adsorbing competitors on the activated carbon in the solution after gold leaching. Further, the adsorption rate of gold on activated carbon is further improved.
  • the oxidizing agent is not particularly limited, but air is used from the viewpoint of cost.
  • the liquid temperature is not particularly limited, but considering the fact that gold leaching is warm leaching and the aspect of oxidation efficiency, the liquid temperature of the liquid after gold leaching is preferably maintained at 45 ° C. or more, more preferably It is 50 ° C. or higher.
  • An increase in ORP indicates a decrease in monovalent copper ions in the solution after gold leaching.
  • Monovalent copper is known as a very soft element, has a high affinity for activated carbon, and competes with the adsorption of gold complexes. By reducing the monovalent copper, the adsorption active sites in the activated carbon are increased in selectivity to gold, thereby achieving efficient recovery of gold.
  • the ORP can be adjusted to 520 mV or more, thereby reducing the monovalent copper concentration in the liquid and improving the adsorption rate of gold on activated carbon.
  • the upper limit is not particularly limited, but considering the time required for adjustment and the reduction efficiency of monovalent copper, it is preferably 570 mV or less, more preferably 530 to 560 mV.
  • Step 5 of recovering gold by activated carbon adsorption is performed from a gold solution obtained by solid-liquid separation.
  • the contact of gold with activated carbon may be carried out by batch feeding or by continuously passing an acidic leachate through an adsorption tower packed with activated carbon.
  • the stirring speed is not specified.
  • the amount of activated carbon added is 50 to 10,000 times the weight of gold.
  • the flow rate is not particularly limited (generally SV1 to 25), but when the gold adsorption amount per unit weight of the activated carbon reaches 20000 to 30000 g / t, the activated carbon does not satisfy the required capacity. . Therefore, gold strips from activated carbon and regeneration are performed based on this amount of adsorption.
  • the method for regenerating activated carbon is carried out with a generally known sulfur compound, nitrogen compound, or acid, and is not particularly limited.
  • ⁇ Other processes> (Copper recovery) Since the liquid after leaching obtained in step 1 contains a large amount of copper component, copper can be recovered from the liquid after leaching.
  • recovery method For example, solvent extraction, ion exchange, substitution precipitation with a base metal, electrowinning, etc. can be utilized.
  • the copper in the solution after leaching contains both monovalent and divalent states, but in order to perform solvent extraction and ion exchange smoothly, all of them should be oxidized beforehand to be divalent copper ions. Is preferred.
  • the method of oxidation is not particularly limited, but a method of leaching air or oxygen into the liquid after leaching is simple.
  • Example 1 As the sulfide mineral, a copper concentrate containing Cu: 16% by mass, Fe: 26% by mass, S: 28% by mass and containing 63 g / t of Au was prepared. After heating 16 L of a leachate (first acidic aqueous solution) having the composition shown in Table 1 to 70 to 85 ° C., 480 g of the copper concentrate is added, and air is blown into the leachate (0.2 L / min) and stirred. The leaching test was conducted while continuing. The metal analysis was performed by ICP emission spectroscopic analysis.
  • Table 2 and FIG. 1 show the relationship between the redox potential ORP (vs. Ag / AgCl) during leaching and the leaching rate of Cu and Au obtained in Example 1 above.
  • the leaching rate was calculated by calculating backward from the content in the leaching residue, with the content in the sulfide mineral being 100%. From Table 2 and FIG. 1, Cu has no change in the leaching rate between the leaching solutions A and B, the leaching rate reaches about 90% by mass with ORP of 450 mV, and the leaching rate of 99% by mass or more with ORP of 500 mV. became.
  • Example 1 solid-liquid separation between the copper leaching step and the gold leaching step is not carried out, but from the above results, using the leachate A containing no bromide ions in the copper leaching step, It can be understood that the leaching rate of gold can be increased by using the leaching solution B containing bromide ions in the gold leaching step while suppressing the leaching of gold.
  • the ORP that is the end point of the copper leaching process is set between 450 and 500 mV using the leaching liquid A, and after the solid-liquid separation, the gold leaching process is performed by switching to the leaching liquid B, thereby separating copper and gold at a high level. It can be understood that gold can be recovered at a high recovery rate while being separated with efficiency.
  • the copper leaching step can be completed under the conditions that the copper leaching rate is 95% by mass or more and the gold leaching rate is 10% by mass or less.
  • Example 2 In a gold leaching solution obtained after the gold leaching step using a gold leaching solution containing 50 g / L chloride ion, 80 g / L bromide ion, 18 g / L copper, and 0.2 g / L iron. Leached gold.
  • the solution after gold leaching contained NaCl: 84 g / L, NaBr: 103 g / L, Cu: 20 g / L, Fe: 2 g / L, Au: 8 mg / L, and pH was 1.2.
  • CuCl was added to adjust the ORP to 510 mV. After leaching, the liquid was heated to 55 ° C. and stirred while blowing 0.4 L of air per minute.
  • This gold leaching solution was passed through a glass column filled with approximately 14 ml of coconut shell-derived activated carbon (Yaikol MC manufactured by Taihei Chemical Sangyo Co., Ltd.) to adsorb gold onto the activated carbon.
  • the column diameter was 11 mm and the height was 150 mm.
  • the liquid supply rate was 11.9 ml / min, and the space velocity was 50 (1 / h).
  • Gold in the discharged solution after adsorption was diluted with hydrochloric acid and quantified by ICP-AES. The relationship between the ORP and the post-adsorption liquid is shown in FIG.
  • the gold concentration contained in the post-adsorption liquid is significantly reduced in the liquid in which the ORP is adjusted to 520 mV or more.
  • the upper limit of ORP is not set, it is understood that even if the potential is raised excessively, the gold concentration in the solution after adsorption does not drop dramatically, and it is sufficient to oxidize to at least 520 mV, but it does not prevent excessive oxidation. .
  • Example 3 While continuously supplying liquid using the post-gold leaching solution and the activated carbon packed column used in Example 2, the gold concentration of the post-adsorption solution was measured by changing the ORP by adding CuCl and blowing air. The results are shown in FIG.
  • FIG. 3 also shows that the relationship between the adsorption of ORP and gold on activated carbon is clear, and gold can be recovered well when the gold leaching solution is ORP 520 mV or higher and brought into contact with activated carbon. It can also be seen that it is Cu (I) that affects the ORP.
  • Cu (I) tends to be oxidized to Cu (II) in an aqueous solution, but exists relatively stably in an aqueous solution containing a relatively high concentration of halide as in the present system. Therefore, it is presumed that the same result can be obtained by oxidizing Cu (I) with an oxidizing agent such as hydrogen peroxide or hypochlorous acid in addition to air blowing. preferable.
  • an oxidizing agent such as hydrogen peroxide or hypochlorous acid in addition to air blowing.

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Abstract

Ce procédé de récupération d'or à partir de minerai de sulfure comprend : une première étape dans laquelle une première solution acide contenant des ions chlore, des ions cuivre et des ions fer mais ne contenant pas d'ions brome est mise en contact avec un minerai de sulfure tout en étant introduite avec un agent d'oxydation pour lixivier le composant de cuivre du minerai de sulfure ; une deuxième étape dans laquelle la solution de réaction de lixiviation obtenue par la première étape est séparée en un résidu de lixiviation et un lixiviat par séparation solide/liquide ; une troisième étape dans laquelle une seconde solution aqueuse acide contenant des ions chlore, des ions brome, des ions cuivre et des ions fer est mise en contact avec le résidu de lixiviation obtenu par la deuxième étape, tout en étant introduite avec un agent d'oxydation, ce qui permet de lixivier le composant d'or dans le résidu ; une quatrième étape dans laquelle après ajout de chlorure de cuivre (I) au lixiviat d'or obtenu dans la troisième étape, un agent oxydant est ajouté pour ajuster le potentiel redox à au moins 520 mV pour réduire la quantité d'ions cuivre monovalents dans le lixiviat d'or ; et une cinquième étape dans laquelle l'or dans le lixiviat d'or obtenu dans la quatrième étape est adsorbé par du charbon actif.
PCT/JP2014/053192 2013-03-29 2014-02-12 Procédé de récupération d'or à partir de minerai de sulfure WO2014156349A1 (fr)

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AU2014245389A AU2014245389B2 (en) 2013-03-29 2014-02-12 Method for recovering gold from sulfide ore
CA2908688A CA2908688C (fr) 2013-03-29 2014-02-12 Procede de recuperation d'or a partir de minerai de sulfure

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JP2013075226A JP5840642B2 (ja) 2013-03-29 2013-03-29 硫化鉱物からの金の回収方法
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CN114555840A (zh) * 2019-11-18 2022-05-27 贺利氏德国有限两合公司 用于回收贵金属的方法

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JP6849482B2 (ja) * 2016-03-31 2021-03-24 Ｊｘ金属株式会社 金を含む鉱石もしくは精錬中間物からの金の回収方法
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