WO2019064709A1 - Procédé de lixiviation d'or et procédé de récupération d'or - Google Patents

Procédé de lixiviation d'or et procédé de récupération d'or Download PDF

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WO2019064709A1
WO2019064709A1 PCT/JP2018/022098 JP2018022098W WO2019064709A1 WO 2019064709 A1 WO2019064709 A1 WO 2019064709A1 JP 2018022098 W JP2018022098 W JP 2018022098W WO 2019064709 A1 WO2019064709 A1 WO 2019064709A1
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Prior art keywords
leaching
gold
sulfur
residue
raw material
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PCT/JP2018/022098
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English (en)
Japanese (ja)
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良介 辰巳
和広 関根
昭 吉村
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Ｊｘ金属株式会社
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Priority to AU2018340945A priority Critical patent/AU2018340945B2/en
Priority to PE2020000365A priority patent/PE20201046A1/es
Publication of WO2019064709A1 publication Critical patent/WO2019064709A1/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
    • C22B11/00—Obtaining noble metals
    • 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
    • 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 of leaching gold that can be contained in sulfide minerals and smelting intermediates, and a method of recovering gold using the same, and in particular, proposes a technique that contributes to the improvement of the recovery rate of gold. .
  • smelting intermediates which are leaching residues obtained by leaching gold contained in ores such as chalcopyrite and other sulfide minerals and silicate ore and copper in sulfide ore or leaching iron in pyrite
  • chemicals such as cyanide, thiourea, thiosulfuric acid and halogen gas were used before.
  • cyanide cyanide
  • thiourea thiosulfuric acid and halogen gas
  • gold contained in sulfide minerals generally includes those exposed on the surface, those covered with sulfides, and those covered with gangue components such as SiO 2 .
  • exposed gold in sulfide minerals and the like can be dissolved by forming a halogen complex in the above-described gold leaching step.
  • a roasting step of heating sulfide minerals and the like in a non-oxidizing atmosphere is carried out to sulfide the iron disulfide
  • iron (II) and sulfur By pyrolyzing to iron (II) and sulfur, and performing a roasting step followed by a deironing step with almost the same leaching conditions as the gold leaching step to leach and remove iron sulfide (II),
  • the gold can be dissolved in a subsequent gold leaching step.
  • gold covered with SiO 2 or the like in the sulfide mineral is present in a very small amount, it is considered that it is difficult to leach it.
  • the leaching rate of gold actually leached through the roasting process, the iron removal process, the gold leaching process, etc. as described above analyzes the gold existence form in raw materials such as sulfide minerals and smelting intermediates. It was found to be lower than the theoretical leaching rate obtained. That is, it is considered that not only gold covered with gangue components such as SiO 2 in sulfide minerals but also other forms of gold are sufficiently leached by conventional gold leaching methods. Thus, the prior art has room for improvement in terms of further leaching of gold.
  • the present invention is intended to solve such problems of the prior art, and its object is to increase the leaching rate of gold contained in sulfide minerals and smelting intermediates to recover the gold recovery rate. It is an object of the present invention to provide a method for leaching gold that can contribute to improvement and a method for recovering gold using the same.
  • the gold leaching method of the present invention is contained in a sulfide mineral or a raw material containing gold and sulfur as a smelting intermediate obtained by subjecting the sulfide mineral to a smelting treatment.
  • a method of leaching the gold which is a first leaching step of leaching a portion of the gold in the raw material to obtain a leaching residue containing sulfur and containing gold, and removing sulfur in the leaching residue
  • a second leaching step of leaching at least a portion of the remainder of the gold in the leaching residue that has undergone the sulfur removal step.
  • the sulfur in the leaching residue is removed in the sulfur removal step to expose the gold in the leaching residue.
  • the gold leaching method of the present invention is particularly effective when the first leaching step produces a leaching residue that contains sulfur in the form of at least partially elemental sulfur.
  • the leaching residue can be contacted with an alkaline solution to remove sulfur in the leaching residue in the sulfur removal step.
  • the pH of the alkaline solution to be brought into contact with the leaching residue is preferably 10 or more.
  • the leaching residue in the gold leaching method of the present invention, in the sulfur removal step, can be heated to remove sulfur in the leaching residue as a gas.
  • the sulfur removal rate in the sulfur removal step is preferably 10% or more, and more preferably 25% or more.
  • the raw material in the first leaching step, is preferably brought into contact with an acidic aqueous solution containing copper ions, iron ions and halide ions under supply of an oxidizing agent.
  • the gold recovery method of the present invention is to recover gold from the raw material using any of the above gold leaching methods.
  • the sulfur removal step of removing sulfur in the leach residue is performed, and then at least a portion of the remaining gold in the leach residue after the sulfur removal step is further leached.
  • the gold from which the surrounding sulfur has been removed in the sulfur removal step can be effectively leached in the second leaching step.
  • the leaching rate of gold contained in sulfide minerals and smelting intermediates is further enhanced, which can contribute to the improvement of the recovery rate of gold.
  • the gold leaching method according to one embodiment of the present invention is, as shown in FIG. 1, a sulfide mineral or a raw material as a smelting intermediate obtained by subjecting the sulfide mineral to a smelting treatment. It is a method for leaching the gold contained therein from its raw material, for those containing gold and sulfur.
  • this method comprises at least a first leaching step of leaching a portion of gold in the raw material to obtain a leaching residue containing sulfur and containing gold, and a sulfur removing step of removing sulfur in the leaching residue And a second leaching step of leaching at least a portion of the remainder of the gold in the leaching residue that has undergone the sulfur removal step, thereby obtaining a gold-containing post leaching solution.
  • the gold leaching method of this embodiment can be applied to a predetermined gold recovery method.
  • a pretreatment step for a raw material containing gold and sulfur obtained from sulfide minerals and smelting intermediates
  • a sulfur removal step for a raw material containing gold and sulfur obtained from sulfide minerals and smelting intermediates
  • an adsorption step, a washing step and an elution step are sequentially performed to obtain a concentrated gold solution. This will be described in detail below.
  • Sulfide minerals and smelting intermediates are selected, for example, from chalcocite, goethite, chalcopyrite, chalcopyrite, pyrite, arsopite, arsenopyrite, galena, sphalerite, arsenopyrite, chromite or pyrrhotite Sulfide minerals containing at least one of the above, sulfide minerals containing gold and sulfur such as silicate ores, or intermediates obtained after smelting the sulfide minerals (herein also referred to as “smelting intermediates”) It can be done.
  • the smelting process is, for example, a process of leaching copper with a predetermined leachate in the case of copper sulfide ore, or a process of leaching iron with a predetermined leachate in the case of pyrite, etc.
  • the leaching residue obtained by the above can be used as a smelting intermediate.
  • Sulfide minerals and smelting intermediates can be made into concentrates through conventional beneficiary treatment such as flotation, ore, and specific gravity selection, if necessary. Further, it is possible to reduce the particle size of the ore by grinding and grinding so that the acidic aqueous solution in the gold leaching step or the like is easily in contact with the gold inside the mineral.
  • the above-mentioned sulfide minerals and smelting intermediates can be used as raw materials containing gold and sulfur to be leached in the present invention.
  • the raw material containing gold and sulfur is, for example, a sulfide mineral itself or a smelting intermediate obtained by performing a predetermined smelting process as described above.
  • the concentration of gold in the gold-containing raw material thus obtained is typically about 1 to 500 mass ppm, and more typically about 10 to 50 mass ppm.
  • the roasting step is performed as the pretreatment step
  • the raw material containing gold and sulfur is reduced by a reducing atmosphere such as ammonia, carbon monoxide, hydrogen sulfide, a rare gas atmosphere such as argon or helium, nitrogen
  • a reducing atmosphere such as ammonia, carbon monoxide, hydrogen sulfide, a rare gas atmosphere such as argon or helium, nitrogen
  • the pyrite in the raw material is heated in an atmosphere of about 450 ° C. to about 800 ° C. for about 30 minutes to about 120 minutes in an inert atmosphere such as an atmosphere or a carbon dioxide atmosphere to form iron sulfide (II) and elemental sulfur. Thermally decompose.
  • the chemical reaction at this time is represented by FeS 2 ⁇ FeS + S.
  • the non-oxidizing atmosphere may contain oxygen to such an extent that the generation of sulfur oxide substantially does not have a substantial adverse effect.
  • various furnaces such as a tubular furnace, a rotary kiln furnace, etc. can be used, for example.
  • the pretreatment step is an optional step and can be omitted.
  • the above-described raw material is contacted with a predetermined acidic aqueous solution and an oxidizing agent supplied as it is or after the pretreatment step, to leach iron and gold.
  • an acidic aqueous solution containing copper ions and iron ions, and halide ions such as chloride ions and bromide ions.
  • Iron sulfide (II) converted from iron disulfide in the above-described roasting step can be removed by leaching by the reaction of FeS ⁇ Fe + S. Thereby, gold covered with sulfides in the raw material can be exposed, which can be leached out.
  • the gold covered with sulfides in the raw material is exposed, so that, for a given sulfide mineral, theoretically it was covered with a gangue component such as SiO 2 in the raw material
  • a gold leaching rate of 99.9% should be obtained with the exception of gold.
  • the remaining 0.1% corresponds to gold covered with gangue components, and it is difficult to leach out this gold.
  • the actual gold leaching rate was 94% and that nearly 6% of gold was not leached.
  • the inventor has found the following about the reason why gold that can be leached remains in the leaching residue.
  • the metal component of the sulfide dissolves, but the sulfur component is generally leached residue as elemental sulfur (elementary sulfur) etc.
  • elemental sulfur elemental sulfur
  • Remain in Sulfur, such as elemental sulfur is often present surrounding the gold particle on its periphery, and inhibits the leaching of gold due to its slow rate of dissolution in acid. Therefore, after the first leaching step, the inventor removes the sulfur in the leaching residue, and the second leaching step in which at least a portion of the remainder of the gold in the leaching residue is removed. It is thought that the remaining gold can be effectively leached out by The details of the sulfur removal step and the second leaching step will be described later.
  • the leaching of gold in the first leaching step proceeds by reacting the eluted gold with chloride ions or bromide ions to form a chloride complex of gold or a bromide complex of gold.
  • a chloride complex of gold or a bromide complex of gold in particular, by using a bromide ion, a complex is formed in a lower potential state, so that the leaching efficiency of gold can be improved.
  • iron ions work to oxidize gold under the supply of an oxidizing agent and oxidized trivalent iron ions or originally trivalent iron ions.
  • the acidic aqueous solution preferably contains copper ions. Although copper ions do not directly participate in the reaction, the presence of copper ions accelerates the oxidation of iron ions.
  • bromide ion As the halide ion in the acidic aqueous solution, only bromide ion can be used. Alternatively, it is possible to further contain chloride ion in addition to bromide ion, but in this case, it is preferable that the chloride ion concentration is lower.
  • the concentration of bromide ion is preferably 50 g / L or more, more preferably 80 g / L or more, and particularly preferably 150 g / L or more from the viewpoint of further improving the gold leaching rate. Although there is no particularly preferred upper limit value of the bromide ion concentration, it is desirable that the bromide ion concentration be equal to or less than the solubility of the metal bromide to be added.
  • the concentration of chloride ion can be, for example, 40 g / L or less, and particularly preferably 25 g / L or less. Furthermore, it is even more preferable that the halide ion in the acidic aqueous solution is only bromide ion and no chloride ion is present in the acidic aqueous solution.
  • the iron ion concentration in the acidic aqueous solution can be 50 g / L or less, preferably 0.01 g / L to 10 g / L.
  • the copper ion concentration is preferably 1 g / L or more, and more preferably 5 g / L or more.
  • the concentration of copper ions is generally 30 g / L or less, preferably 20 g / L or less.
  • each concentration of said bromide ion, a chloride ion, a copper ion, and an iron ion means the density
  • the source of bromide ion is not particularly limited, and examples thereof include hydrogen bromide, hydrobromic acid, metal bromide and bromine gas, and in the form of metal bromide in consideration of economy and safety. It is preferable to supply.
  • metal bromides include copper bromide (cuprous bromide and cupric bromide), iron bromide (ferrous bromide and 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.
  • copper bromide and iron bromide are also preferably used because they can be used as sources of copper ions and iron ions.
  • the source is not particularly limited, but hydrogen chloride, hydrochloric acid, metal chloride and chlorine gas may, for example, be mentioned, and in the form of metal chloride in view of economy and safety. It is preferable to supply.
  • the metal chloride include copper chloride (cuprous chloride and cupric chloride), iron chloride (ferrous chloride and ferric chloride), and alkali metals (lithium, sodium, potassium, rubidium, cesium, francium) Chlorides and chlorides of alkaline earth metals (beryllium, magnesium, calcium, strontium, barium, radium) may be mentioned, and sodium chloride is preferred from the viewpoint of economy and availability.
  • copper chloride and iron chloride can also be used because they can also be used as sources of copper ions and iron ions.
  • Copper ions and iron ions are usually supplied in the form of these salts, and can be supplied, for example, in the form of halogenated salts. Copper ions are preferably supplied as copper bromide and / or copper chloride, and iron ions are preferably supplied as iron bromide and / or iron chloride, from the viewpoint that they can also be used as a source of chloride ions and / or bromide ions.
  • copper chloride and iron chloride cupric chloride (CuCl 2 ), cuprous chloride (CuCl), ferric chloride (FeCl 3 ), ferrous chloride (FeCl 2 ) and the like are used.
  • cupric bromide (CuBr 2 ), cuprous bromide (CuBr), ferric bromide (FeBr 3 ), ferrous bromide (FeBr 2 ), etc. are used Be done.
  • an acidic aqueous solution at least one of hydrochloric acid and bromic acid, at least one of cupric chloride and copper bromide, at least one of ferric chloride and ferric bromide, sodium chloride and odor
  • a mixture containing at least one of sodium borate can be used.
  • the redox potential (vs Ag / AgCl) of the acidic aqueous solution at the start of the first leaching step is preferably 500 mV or more, more preferably 600 mV or more, from the viewpoint of promoting gold leaching. Also, from the viewpoint of increasing the leaching rate of gold, it is preferable to maintain the pH of the acidic aqueous solution at 2.0 or less, but since the higher pH is promoted at the oxidation rate of iron, the pH of the acidic aqueous solution is 0. It is more preferable to maintain 5 to 1.9.
  • the first leaching step is carried out while supplying an oxidizing agent to control the redox potential. If the oxidizing agent is not added, the redox potential is lowered halfway and the leaching reaction does not proceed.
  • the oxidizing agent is not particularly limited, and examples thereof include oxygen, air, chlorine, bromine and hydrogen peroxide. There is no need for an oxidant with an extremely high redox potential, air is sufficient.
  • the pulp concentration of the acidic aqueous solution to which the raw material is added is preferably high, because the leaching of copper can be suppressed, but if it is too high, the leaching rate of gold decreases. From this viewpoint, the pulp concentration is preferably 200 g / L or less, and more preferably 15 g / L to 50 g / L.
  • the pulp concentration means the ratio of the dry weight of the raw material (g) to the volume (L) of the acidic aqueous solution.
  • the redox potential at the time of gold leaching is not particularly adjusted, but the redox potential of the solution after leaching sufficiently after gold leaching is about 450 to 600 mV, typically about 500 to 580 mV.
  • Monovalent copper is known as a very soft element, has a high affinity for activated carbon, and competes with the adsorption of gold complexes. This decrease in monovalent copper makes it possible to realize efficient recovery of gold by increasing the selectivity to gold for the adsorption active site in activated carbon.
  • Such a first leaching step is terminated when the leaching rate of iron from the raw material is, for example, 5% or more, preferably 15% or more, more preferably 30% or more, although it depends on the type of ore. can do. Also, the first leaching step is terminated when the leaching rate of iron from the raw material becomes the above ratio and the leaching rate of copper from the raw material becomes, for example, 5% or more, preferably 15% or more. It is also good. At this time, the leaching rate of gold from the raw material is preferably 85% or more, more preferably 90% or less, and particularly preferably 95% or less.
  • leaching can also be performed under the conditions described in JP-A-2005-523992 and the like. That is, under this condition, the gold in the raw material is dissolved by leaching while supplying an oxygen-containing gas using a copper (II) chloride-sodium chloride aqueous solution under atmospheric pressure conditions.
  • the redox potential can be less than 650 mV, preferably 530 mV to 620 mV, and the pH can be maintained in the range of 1 to 3.
  • the leaching under these conditions most of the iron and sulfur components in the raw material are not dissolved, but a certain amount of sulfur component is converted to elemental sulfur and remains in the leaching residue, and gold leaching is performed as described above. May inhibit. Therefore, even when the leaching is performed under this condition, it is effective to carry out the sulfur removal step and the second leaching step described later from the viewpoint of further improving the recovery rate of gold.
  • the leaching residue obtained in the first leaching step is subjected to a sulfur removal step for removing sulfur contained in the leaching residue.
  • This sulfur removal step is performed as a separate step from the leaching of the first leaching step.
  • gold covered with sulfur such as elemental sulfur in the leaching residue is exposed, it can be effectively leached in the second leaching step described later.
  • the sulfur removal step the leaching residue is heated under a predetermined atmosphere to remove sulfur in the leaching residue as a gas, or the leaching residue is washed with an alkaline solution to dissolve and remove sulfur, etc. It can be mentioned.
  • the leaching residue can be heated, for example, maintained at a temperature above 450 ° C., which is the boiling point of sulfur, to remove sulfur in the leaching residue as a gas.
  • the temperature can be set to 1000 ° C. or less.
  • the retention temperature of the leaching residue is set to 500 ° C to 700 ° C.
  • the time for which the temperature is maintained is preferably 30 minutes to 180 minutes, more preferably 30 minutes to 60 minutes.
  • the atmosphere at the time of heating can be an inert atmosphere including a rare gas atmosphere such as argon or helium, a nitrogen atmosphere, a carbon dioxide atmosphere, etc.
  • a rare gas atmosphere such as argon or helium
  • nitrogen atmosphere such as a nitrogen atmosphere
  • a carbon dioxide atmosphere such as a carbon dioxide atmosphere
  • sulfur is removed as sulfur gas.
  • an oxidizing atmosphere such as air may be used, and in this case, it is removed as SO 2 gas.
  • various furnaces such as a tubular furnace and a rotary kiln furnace, for this heating.
  • an alkaline solution having a pH of preferably 10 to 14 and more preferably 10 to 12 can be used.
  • the alkaline solution sodium hydroxide solution, water Sodium oxide, sodium carbonate and the like can be mentioned.
  • the pH of the alkaline solution is too high, not only a large amount of alkali is required to raise the pH so much, but also a large amount of acid during processing of the solution after the second leaching step of the next step or sulfur is dissolved. It is considered necessary to increase costs.
  • gold becomes a thiosulfate complex or the like and can be dissolved in alkali.
  • the gold can be recovered using activated carbon, but when the pH is high, a large amount of sodium is contained and the gold to the activated carbon There is also a possibility that adsorption and elution may be inhibited.
  • the pH is too low, the pH is further lowered due to the dissolution of sulfur and the hydrolysis reaction of the components in the liquid, and particularly when the pH is 7 or less, although depending on the redox potential, hydrogen sulfide gas May occur.
  • the liquid temperature at the time of washing with an alkaline solution can be set to 20 (room temperature) ° C. to 90 ° C., and particularly preferably 50 ° C. to 80 ° C.
  • the washing time may be, for example, 60 minutes to 360 minutes, preferably 60 minutes to 180 minutes. If the washing time is too short, there is a concern that the sulfur in the leaching residue can not be sufficiently removed, while if the washing time is too long, the treatment efficiency is reduced.
  • the sulfur removal step as described above can be performed to remove sulfur from the leaching residue preferably by 10% or more, more preferably 25% or more. If any sulfur is removed here, gold can be further leached in the second leaching step described later, which leads to an improvement in the gold leaching rate.
  • a second leaching step for leaching gold in the leaching residue is carried out, and gold leaching is performed again.
  • the second leaching step can be performed under substantially the same conditions as the first leaching step described above, but here the sulfur covering the gold remaining in the leaching residue after the first leaching step It is removed in the sulfur removal step, and the gold can be effectively leached since the gold is exposed.
  • the leaching rate of gold from the leaching residue can be preferably 10% or more, more preferably 30% or more.
  • gold can be recovered from the solution after gold leaching obtained by solid-liquid separation using activated carbon adsorption.
  • the contact of gold with activated carbon can be carried out by continuously passing the acidic leach solution through a batch batch system or an adsorption column packed with activated carbon.
  • the stirring speed is not particularly limited, and the amount of activated carbon added is 50 times to 10000 times the weight of gold.
  • the flow rate is not particularly limited (generally, SV1 to 25).
  • the activated carbon may show a decrease in its adsorption capacity. Therefore, the stripping and regeneration of gold from activated carbon can be performed with this amount of adsorption as a standard.
  • the activated carbon can be regenerated by various methods such as generally known sulfur compounds and nitrogen compounds, or acids.
  • the activated carbon to which gold is adsorbed in the adsorption step can be washed with an acidic solution or alkaline solution as a washing agent.
  • an alkaline solution such as NaOH
  • sulfur that may be adsorbed on activated carbon can be effectively removed
  • an acidic solution such as hydrochloric acid
  • copper that is adsorbed on activated carbon And iron can be removed effectively. Only one of the acid cleaning and the alkali cleaning can be performed, or both of them can be performed, or it is possible not to perform this cleaning step without performing either.
  • the gold adsorbed on the activated carbon is eluted with an alkaline solution, preferably NaOH or a mixture of NaOH and Na 2 S.
  • an alkaline solution preferably NaOH or a mixture of NaOH and Na 2 S.
  • NaOH its concentration is preferably 0.05 to 1 M, and more preferably 0.1 to 0.5 M.
  • Na 2 S is preferably used at a lower amount due to the price and difficulty in handling, but the lower the concentration of Na 2 S, the lower the effect of gold elution.
  • the amount of Na 2 S added is preferably 0.1 to 10 times the molar amount of NaOH, 0.5 to 1.5 It is more preferable to use a molar amount.
  • Elution can be performed by batch batch method or continuous water flow method, however, in order to lose charge by oxidizing sulfide by oxygen, to prevent gold from being re-adsorbed to activated carbon and to be deposited in the reactor.
  • batchwise elution it is preferable not to stir vigorously. If stirring is required, air is replaced with non-oxidizing gas and stirred.
  • the amount of sodium sulfide to be added may be set to a relatively large amount, or added appropriately.
  • elution is preferably performed under atmospheric pressure.
  • the concentrated gold solution means a solution containing 50 to 5000 mg / L of gold.
  • reduction with sodium oxalate, chemical reduction with sulfur dioxide, or solvent extraction-electrowinning method is known, and either method may be used to form a simple substance. You can get money.
  • the second leaching step was performed on the leaching residue without performing the sulfur removal step.
  • the second leaching step using an acidic aqueous solution with a liquid composition of Cu: 18 g / L, Fe: 2 g / L, Cl: 40 g / L, Br: 80 g / L, the temperature of 85 ° C. Leaching for 6 hours.
  • the grade of each leaching residue before and after the second leaching step is shown in Table 2.
  • the grade shown in Table 2 is the amount of each element when the above-mentioned leaching residue used in the second leaching step is 100 g, and in Table 2, "S-0" means elemental sulfur.
  • Table 3 also shows the percentage of removal of sulfur and the percentage of leaching of gold calculated from the change in the amount of each component before and after the second leaching step.
  • the analysis of each component was performed by high frequency inductively coupled plasma emission spectrometry (ICP-AES).
  • the gold leaching rate in the second leaching step was as low as 12%. This is considered to be due to the fact that the gold is covered with sulfur because the removal rate of sulfur is only 10% and the dissolution rate of sulfur inhibiting gold leaching is slow.
  • FIG. 3 the graph which plotted the relationship between a gold recovery rate (gold leaching rate) and a sulfur removal rate about the said comparative example and invention example is shown in FIG. It can be seen from FIG. 3 that the relationship between the gold recovery rate and the sulfur removal rate is linear with an inclination of approximately 1 and an intercept of zero. In this case, even if sulfur is removed as little as possible, the recovery rate of gold increases, and if sulfur is removed, the recovery rate of gold increases as much as the removed amount.

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Abstract

L'invention concerne un procédé de lixiviation d'or, destiné à la lixiviation de l'or compris dans une matière première qui comprend des minéraux sulfurés ou de l'or et du soufre en tant qu'intermédiaire de raffinage obtenu par un traitement de raffinage de minéraux sulfurés, le procédé de lixiviation d'or comprenant : une première étape de lixiviation, destinée à lixivier une partie de l'or dans la matière première et à obtenir un résidu de lixiviation présentant un résidu d'or et comprenant du soufre ; une étape d'élimination de soufre, destinée à éliminer le soufre dans le résidu de lixiviation ; et une seconde étape de lixiviation, destinée à lixivier au moins une partie de l'or résiduel dans le résidu de lixiviation qui est passé par l'étape d'élimination de soufre.
PCT/JP2018/022098 2017-09-26 2018-06-08 Procédé de lixiviation d'or et procédé de récupération d'or WO2019064709A1 (fr)

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AU2018340945A AU2018340945B2 (en) 2017-09-26 2018-06-08 Gold leaching method and gold recovery method
PE2020000365A PE20201046A1 (es) 2017-09-26 2018-06-08 Metodo de lixiviacion de oro y metodo de recuperacion de oro

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JP2017-185364 2017-09-26
JP2017185364A JP6953258B2 (ja) 2017-09-26 2017-09-26 金の浸出方法および、金の回収方法

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JP7344512B2 (ja) * 2019-11-22 2023-09-14 国立大学法人九州大学 硫化物の浸出方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH01156432A (ja) * 1987-11-07 1989-06-20 British Petroleum Co Plc:The 分離方法
WO2005064023A1 (fr) * 2003-12-23 2005-07-14 Bateman Luxembourg Sa Procede de recuperation de metaux precieux de concentres et de minerais sulfures refractaires
JP2011058018A (ja) * 2009-09-07 2011-03-24 Sumitomo Metal Mining Co Ltd 硫化銅鉱物浸出残渣からの金濃縮物の回収方法
JP2012214865A (ja) * 2011-03-30 2012-11-08 Jx Nippon Mining & Metals Corp 金の浸出方法
WO2014038236A1 (fr) * 2012-09-04 2014-03-13 Jx日鉱日石金属株式会社 Procédé pour lixivier de l'or à partir de minerai d'or contenant de la pyrite
CN104805281A (zh) * 2015-05-05 2015-07-29 中南大学 一种氧压酸浸与氧压碱浸联合浸出硫化物金精矿的方法

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5902474A (en) * 1993-07-29 1999-05-11 Cominco Engineering Services Ltd. Chloride assisted hydrometallurgical extraction of metal
WO2016104113A1 (fr) * 2014-12-26 2016-06-30 Ｊｘ金属株式会社 Procédé de récupération d'or à partir de charbon actif

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH01156432A (ja) * 1987-11-07 1989-06-20 British Petroleum Co Plc:The 分離方法
WO2005064023A1 (fr) * 2003-12-23 2005-07-14 Bateman Luxembourg Sa Procede de recuperation de metaux precieux de concentres et de minerais sulfures refractaires
JP2011058018A (ja) * 2009-09-07 2011-03-24 Sumitomo Metal Mining Co Ltd 硫化銅鉱物浸出残渣からの金濃縮物の回収方法
JP2012214865A (ja) * 2011-03-30 2012-11-08 Jx Nippon Mining & Metals Corp 金の浸出方法
WO2014038236A1 (fr) * 2012-09-04 2014-03-13 Jx日鉱日石金属株式会社 Procédé pour lixivier de l'or à partir de minerai d'or contenant de la pyrite
CN104805281A (zh) * 2015-05-05 2015-07-29 中南大学 一种氧压酸浸与氧压碱浸联合浸出硫化物金精矿的方法

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