WO2014156350A1 - 硫化鉱物からの金の回収方法 - Google Patents
硫化鉱物からの金の回収方法 Download PDFInfo
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- WO2014156350A1 WO2014156350A1 PCT/JP2014/053193 JP2014053193W WO2014156350A1 WO 2014156350 A1 WO2014156350 A1 WO 2014156350A1 JP 2014053193 W JP2014053193 W JP 2014053193W WO 2014156350 A1 WO2014156350 A1 WO 2014156350A1
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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
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B11/00—Obtaining noble metals
- C22B11/04—Obtaining noble metals by wet 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
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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
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.
- Japanese Patent Application Laid-Open No. 2009-235525 states that “an appropriate oxidizing agent for leaching gold present in copper concentrate and the leached gold are reduced again and do not precipitate as metallic gold.
- gold is stably eluted by producing gold chloride using chlorine ions, but when bromine ions are used in combination, gold bromide is produced. Gold leaching can be further facilitated ”(paragraph 0014).
- the bromine ion concentration for use in the gold leaching reaction is necessary to form gold bromide and elute gold to form a complex.
- solubility there is an upper limit of solubility because it is also affected by the concentration, and it is 1 to 80 g / L in consideration of solubility, but it is described that about 10 to 26 g / L is desirable in view of economical use of chemicals. (Paragraph 0017).
- bromine ions in the leachate are added in the form of sodium bromide, and the higher the concentration, the better.
- the solubility changes due to the influence of chlorine ion concentration and temperature at the same time, It is also described that the bromine ion concentration may be practically 1 to 50 g / L, preferably 10 to 26 g / L (paragraph 0025).
- alkali bromide in the leaching solution is reduced to 0. It is proposed to be 5-30 g / L.
- the halogen ions in the leachate used for gold leaching are mainly chlorine ions, and bromine ions are supplementarily added to the method to recover gold from the sulfide ore by a wet method. It proposes a commercially feasible technology.
- gold leaching is performed using the conventional technique, gold exists in a high concentration in the solution after gold leaching immediately after leaching gold.
- the conventional technique has a problem that the gold concentration in the solution after leaching of gold rapidly decreases with time.
- the gold recovery process is not always performed immediately after the gold leaching process, and the gold leaching is performed for about 1 to 3 days due to the solid-liquid separation operation and operation schedule.
- the gold recovery process may be performed after storing the post-solution. Therefore, a method capable of maintaining the dissolved gold concentration as much as possible while storing the solution after gold leaching is desired.
- the gold complex contained in the solution after leaching after the gold leaching process is adsorbed on the activated carbon.
- the activated carbon is incinerated, the amount of adsorption per unit activated carbon weight has a direct impact on the production cost and has a large effect. Therefore, development of a method for increasing the unit adsorption amount is desired. In any case, no study has been made on improving the adsorptivity of gold to activated carbon, and generally, there are problems such as the type of activated carbon and the contamination of the liquid after leaching, and an appropriate method has not been known.
- the present invention provides a method for recovering gold from sulfide minerals that can suppress a decrease in gold concentration in the solution after gold leaching with time and can improve the amount of gold adsorbed on activated carbon.
- the present inventor has found that by increasing the bromine ion concentration in a gold leaching solution based on an aqueous alkali chloride solution extremely high, the state in which the gold in the leaching solution is dissolved can be stably maintained. . And, when adsorbing the gold complex in the liquid after leaching with activated carbon, the amount of gold adsorbed on the activated carbon is reduced by reducing the concentration of monovalent copper ions in the liquid after leaching which becomes an adsorption competing substance in advance. We found that it can be significantly improved.
- the leaching residue after leaching treatment of sulfide mineral or sulfide mineral is performed under the supply of an acidic aqueous solution containing chlorine ions, bromine ions, copper ions, and iron ions and an oxidizing agent.
- Step 1 for leaching the gold component in the leaching residue by contact, and the bromine ion concentration in the gold leached solution after leaching the gold to 40 g / L or more and the oxidation-reduction potential to 500 mV (reference electrode, silver / silver chloride) )
- Step 2 to preserve while maintaining the above, and after adding cuprous chloride to the gold leaching solution obtained in step 2, adding an oxidizing agent to adjust the oxidation-reduction potential to 520 mV or more and after gold leaching
- It is a method for recovering gold from sulfide minerals which includes Step 3 for reducing monovalent copper ions in the liquid and Step 4 for adsorbing gold in the liquid after gold leaching obtained in Step 3 to activated carbon.
- the leaching residue after the leaching treatment of sulfide mineral or sulfide mineral is performed by supplying an acidic aqueous solution containing chlorine ions, bromine ions, copper ions, and iron ions and an oxidizing agent.
- step 3 includes adjusting the oxidation-reduction potential (reference electrode, silver / silver chloride) to 520 mV to 570 mV.
- step 3 includes adjusting the redox potential by blowing air.
- the present invention it is possible to provide a method for recovering gold from sulfide minerals that can suppress a decrease in gold concentration in the solution after gold leaching with time and can improve the amount of gold adsorbed on activated carbon.
- an acidic aqueous solution (gold leaching solution) containing chlorine ions, bromine ions, copper ions, and iron ions is brought into contact with the raw material while supplying an oxidizing agent, and the gold component in the raw material is leached. It is possible to adjust the chlorine ion concentration in the acidic aqueous solution to 40 to 200 g / L, the bromine ion concentration to 20 to 100 g / L, the copper ion concentration to 5 to 25 g / L, and the iron ion concentration to 0.01 to 10 g / L. preferable.
- the raw material to be treated in the present invention is sulfide mineral or leaching residue after leaching treatment is performed on sulfide mineral.
- a sulfide mineral typically, the primary copper sulfide ore (example: chalcopyrite) containing gold, the copper sulfide ore containing the silicate ore containing gold, and the pyrite containing gold are mentioned.
- intermediate products generated in various processes of sulfide minerals are also handled as sulfide minerals.
- Gold leaching proceeds when the eluted gold reacts with chlorine ions or bromine ions to form gold chloride complexes or gold bromide complexes.
- bromine ions in combination, the complex is formed at a lower potential, so that the leaching time can be shortened and the gold leaching efficiency can be improved, that is, the gold concentration in the liquid after leaching can be increased.
- the bromine ion concentration in the gold leaching solution is remarkably increased, so that the leached gold can exist stably for a long time in a dissolved state.
- the redox potential of the leachate also depends on the temperature, and when the liquid temperature is lowered by about 10 ° C., the redox potential is also lowered by about 10 mV. Therefore, if it is left as it is from a general leaching temperature of about 80 ° C., the temperature of the leaching solution is lowered, the oxidation-reduction potential is also lowered, and it becomes difficult to maintain the dissolution of gold.
- the concentration of bromide ions in the gold leaching solution may be about 5 g / L only from the viewpoint of reaction rate and solubility, but the gold concentration in the leaching solution is stably dissolved at 2 mg / L or more.
- the temperature of the solution after leaching is lowered from about 80 ° C. which is a general leaching temperature to room temperature, it is necessary to be 40 g / L or more.
- 80 g / L or more more preferably 100 g / L or more, and still more preferably 120 g / L or more.
- the bromine ion concentration in the gold leachate is generally low, and is preferably 80 to 100 g / L.
- the concentration of chlorine ions in the gold leachate is preferably 5 g / L or more, and more preferably 15 g / L or more, from the viewpoint of Cu (I) production.
- the chlorine ion concentration is too high, the ion concentration in the bath will increase and problems of precipitation will occur during operation, so it should be 200 g / L or less, and 20-40 g / L. preferable.
- Iron ions which are trivalent iron ions oxidized under the supply of an oxidizing agent or trivalent iron ions from the beginning, function to oxidize gold.
- concentration of iron ions in the gold leaching solution is preferably 0.01 g / L or more, and more preferably 3 g / L or more.
- Copper ions are not directly involved in the reaction, but the presence of copper ions increases the oxidation rate of iron ions.
- divalent copper ions function as oxidation.
- the concentration of copper ions in the leachate is preferably 5 g / L or more, and more preferably 20 g / L or more.
- 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.
- At least one of hydrochloric acid and bromic acid, cupric chloride, and copper chloride are selected on the condition that the gold leaching solution is selected to contain both chlorine ions and bromine ions.
- a mixed solution containing at least one of cupric bromide, at least one of ferric chloride and ferric bromide, and at least one of sodium chloride and sodium bromide can be used.
- the pH of the gold leaching solution is preferably about 0 to 3 and more preferably about 0.5 to 2.0 for ensuring the dissolution of trivalent iron ions.
- the redox potential (reference electrode, silver / silver chloride) of the leaching solution at the start of the gold leaching process is preferably 500 mV or more, more preferably 550 mV or more because of the effect of bromine ions.
- the temperature of the gold leaching solution is preferably 60 ° C. or more from the viewpoint of leaching efficiency and material of the apparatus, and more preferably 70 to 90 ° C. from the viewpoint of leaching speed.
- the gold leaching process is carried out while supplying the oxidizing agent, thereby managing the redox potential.
- 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 bromine ion concentration in the solution after gold leaching is adjusted during the storage period. Specifically, when the bromine ion concentration in the acidic aqueous solution leached with gold is 40 g / L or more, the oxidation-reduction potential of the solution after leaching with gold is 500 mV or more (reference electrode, silver / silver chloride) at room temperature or higher (25 ° C. It is possible to maintain the dissolution of gold by managing the above. This is a value 40 mV or more lower than the redox potential immediately after leaching.
- the redox potential of the solution after gold leaching is controlled at 480 mV or more (reference electrode, silver / silver chloride) at room temperature or higher (25 ° C. or higher). It is also possible to do. Further, the higher the control temperature, the higher the solubility of gold, but the higher the cost for heat retention, it is preferable to store at room temperature (20 to 60 ° C., typically 25 to 40 ° C.).
- the stability of the gold dissolved in the solution after leaching after gold leaching is high, so that after the gold leaching process is finished, the storage period until the gold recovery process is started can be extended. it can.
- the storage period can be 5 days or more, and can be 1 week or more. However, since there are few merits even if it preserve
- a bromine ion source can be added to the leached solution within 1 day, preferably within half a day, more preferably within 6 hours, and even more preferably within 1 hour.
- the bromine ion supply source include the compounds described above, and sodium bromide is preferred from the viewpoints of economy and availability.
- 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 4 is performed in which gold is recovered by activated carbon adsorption 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 by the copper leaching step contains a large amount of copper component, copper can be recovered from the liquid after leaching. Although there is no restriction
- 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 In the test, gold was leached to the residue after leaching the copper in the copper sulfide concentrate containing gold. The gold quality in the residue was 26 g / t, and the copper quality was 1.2%.
- the Cl ion concentration was adjusted to 40 g / L
- the Cu ion concentration was adjusted to 20 g / L
- the Fe ion concentration was adjusted to 2 g / L
- the Br ion concentration was adjusted to 20 to 120 g / L. went.
- the oxidation-reduction potential at 80 ° C. was 537 to 557 mV (reference electrode, silver / silver chloride).
- the solution after leaching was allowed to stand at room temperature (15 to 25 ° C.), and the concentration of gold dissolved in the leaching solution after 1 to 7 days was measured.
- the sampled leachate was filtered through a 0.1 ⁇ m membrane filter and then subjected to ICP analysis. The oxidation-reduction potential during the storage period was measured after the temperature of the solution after leaching dropped to 25 ° C.
- 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 high-concentration halide as in this 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
Description
金浸出工程では、塩素イオン、臭素イオン、銅イオン及び鉄イオンを含有する酸性水溶液(金浸出液)を酸化剤の供給下で原料に接触させて、原料中の金成分を浸出する。酸性水溶液中の塩素イオン濃度を40~200g/L、臭素イオン濃度を20~100g/L、銅イオン濃度を5~25g/L、鉄イオン濃度を0.01~10g/Lに調整することが好ましい。本発明の処理対象となる原料は、硫化鉱物、又は硫化鉱物に対して浸出処理を行った後の浸出残渣である。硫化鉱物としては特に制限はないが、典型的には金を含有する一次硫化銅鉱(例:黄銅鉱)、金を含むケイ酸鉱を含有する硫化銅鉱、金を含有する黄鉄鉱が挙げられる。また、硫化鉱物の様々な処理過程で生じる中間生成物も硫化鉱物として取り扱う。
金浸出工程終了後の金浸出後液中で金が安定して溶解している状態を長期間保持するために、保存期間中に金浸出後液中の臭素イオン濃度を調整する。具体的には、金を浸出した酸性水溶液中の臭素イオン濃度が40g/L以上のとき、金浸出後液の酸化還元電位を500mV以上(参照電極、銀/塩化銀)で室温以上(25℃以上)で管理することにより金の溶解を維持可能である。これは浸出直後の酸化還元電位よりも40mV以上低い値である。金を浸出した酸性水溶液中の臭素イオン濃度が80g/L以上であれば、金浸出後液の酸化還元電位を480mV以上(参照電極、銀/塩化銀)で室温以上(25℃以上)で管理することも可能である。また、管理温度が高いほうが金の溶解性は高くなるが、保温のための費用がかかるため、室温(20~60℃、典型的には25~40℃)で保存することが好ましい。
保存工程を経た金浸出後液に対して、CuClを加えて撹拌し、一度酸化還元電位(ORP)を520mV以下に、より好ましくは500mV以下に下げた後に、酸化剤を加えて再度ORPを520mV以上に調整する。これにより、金の活性炭吸着を阻害する金浸出後液中の一価の銅イオンが二価の銅イオンに酸化されて減少し、金浸出後液中の活性炭への吸着競合物が少なくなるため、活性炭への金の吸着率がより向上する。
金の浸出反応後、固液分離することによって得られた金溶解液から、活性炭吸着により金を回収する工程4を実施する。金の活性炭への接触はバッチ回分式もしくは活性炭を充填した吸着塔に酸性浸出液を連続通液することで行ってもよい。
(銅回収)
銅浸出工程によって得られた浸出後液は銅成分を多量に含んでいるので、浸出後液から銅を回収することができる。銅の回収方法としては特に制限はないが、例えば溶媒抽出、イオン交換、卑な金属との置換析出及び電解採取などを利用することができる。浸出後液中の銅は1価及び2価の状態が混在しているが、溶媒抽出やイオン交換を円滑に行うために、全部が2価の銅イオンとなるように予め酸化しておくことが好ましい。酸化の方法は特に制限はないが空気や酸素を浸出後液中に吹き込む方法が簡便である。
試験では、金を含有する硫化銅精鉱中の銅を浸出した後の残渣に対して金浸出した。残渣中の金品位は26g/tで、銅品位は1.2%であった。金浸出は、Clイオン濃度を40g/L、Cuイオン濃度を20g/L、Feイオン濃度を2g/L、Brイオン濃度を20~120g/Lに調整し、空気を吹き込みながら液温80℃で行った。80℃での酸化還元電位は537~557mV(参照電極、銀/塩化銀)であった。
また、酸化還元電位を480mVにした場合、Br濃度が60g/Lの浸出液の金濃度は1日後には半分以下に低下したが、Br濃度が80g/Lの浸出液の金濃度は5日後でも当初の金濃度を保持していた。
50g/Lの塩化物イオン、80g/Lの臭化物イオン、18g/Lの銅、及び0.2g/Lの鉄を含む金浸出液を用いて、金浸出工程後に得られた金浸出後液中の金を浸出した。金浸出後液は、NaCl:84g/L、NaBr:103g/L、Cu:20g/L、Fe:2g/L、Au:8mg/L含有し、pHは1.2であった。CuClを添加してORPを510mVに調整した。浸出後液を55℃に加温し、空気を1分当たり0.4L吹き込みながら攪拌した。この金浸出後液をヤシ殻由来活性炭(太平化学産業社製ヤシコールMC)およそ14mlを充填したガラス製カラムに通し、金を活性炭に吸着させた。カラムの直径は11mm、高さ150mmとした。液の供給速度は11.9ml/分、空間速度は50(1/h)とした。排出される吸着後液中の金を塩酸で希釈しICP-AESにより定量した。ORPと吸着後液の関係を図2に示す。
実施例2で使用した金浸出後液と活性炭充填カラムとを用いて連続的に給液する中で、CuClの添加と空気吹き込みによりORPを変化させて吸着後液の金濃度を測定した。結果を図3に示す。
Claims (4)
- 硫化鉱物又は硫化鉱物に対して浸出処理を行った後の浸出残渣を、塩素イオン、臭素イオン、銅イオン、及び鉄イオンを含有する酸性水溶液と酸化剤の供給下で接触させて、浸出残渣中の金成分を浸出する工程1と、
金を浸出した金浸出後液中の臭素イオン濃度を40g/L以上に、酸化還元電位を500mV(参照電極、銀/塩化銀)以上に保持しながら保存する工程2と、
工程2で得られた金浸出後液に塩化第一銅を添加した後、酸化剤を加えて酸化還元電位を520mV以上に調整して金浸出後液中の一価の銅イオンを低減させる工程3と、
工程3で得られた金浸出後液中の金を活性炭に吸着させる工程4と
を含むことを特徴とする硫化鉱物からの金の回収方法。 - 硫化鉱物又は硫化鉱物に対して浸出処理を行った後の浸出残渣を、塩素イオン、臭素イオン、銅イオン、及び鉄イオンを含有する酸性水溶液と酸化剤の供給下で接触させて、浸出残渣中の金成分を浸出する工程1と、
金を浸出した金浸出後液中の臭素イオン濃度を80g/L以上に、酸化還元電位を480mV(参照電極、銀/塩化銀)以上に保持しながら保存する工程2と、
工程2で得られた金浸出後液に塩化第一銅を添加した後、酸化剤を加えて酸化還元電位を520mV以上に調整して金浸出後液中の一価の銅イオンを低減させる工程3と、
工程3で得られた金浸出後液中の金を活性炭に吸着させる工程4と
を含むことを特徴とする硫化鉱物からの金の回収方法。 - 工程3が、酸化還元電位(参照電極、銀/塩化銀)を520mV~570mVに調整することを含む、請求項1又2に記載の硫化鉱物からの金の回収方法。
- 工程3が、空気の吹き込みにより酸化還元電位を調整することを含む請求項1~3のいずれか1項に記載の硫化鉱物からの金の回収方法。
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Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN104789791A (zh) * | 2015-04-14 | 2015-07-22 | 吉林省有色金属地质勘查局研究所 | 泡沫吸附金的自动解脱装置 |
CN107109528A (zh) * | 2014-10-29 | 2017-08-29 | 奥图泰(芬兰)公司 | 用于回收金的工艺 |
US20180298465A1 (en) * | 2016-03-31 | 2018-10-18 | Jx Nippon Mining & Metals Corporation | Method for recovering gold from an ore or a refining intermediate containing gold |
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Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2009235525A (ja) * | 2008-03-27 | 2009-10-15 | Nippon Mining & Metals Co Ltd | 金の浸出方法 |
JP2012184462A (ja) * | 2011-03-04 | 2012-09-27 | Jx Nippon Mining & Metals Corp | 硫化鉱からの銅及び金の浸出方法 |
JP2013112879A (ja) * | 2011-11-30 | 2013-06-10 | Jx Nippon Mining & Metals Corp | 硫化鉱からの金の浸出方法 |
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Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2009235525A (ja) * | 2008-03-27 | 2009-10-15 | Nippon Mining & Metals Co Ltd | 金の浸出方法 |
JP2012184462A (ja) * | 2011-03-04 | 2012-09-27 | Jx Nippon Mining & Metals Corp | 硫化鉱からの銅及び金の浸出方法 |
JP2013112879A (ja) * | 2011-11-30 | 2013-06-10 | Jx Nippon Mining & Metals Corp | 硫化鉱からの金の浸出方法 |
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Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN107109528A (zh) * | 2014-10-29 | 2017-08-29 | 奥图泰(芬兰)公司 | 用于回收金的工艺 |
US10669608B2 (en) | 2014-10-29 | 2020-06-02 | Outotec (Finland) Oy | Process for recovering gold |
CN104789791A (zh) * | 2015-04-14 | 2015-07-22 | 吉林省有色金属地质勘查局研究所 | 泡沫吸附金的自动解脱装置 |
CN104789791B (zh) * | 2015-04-14 | 2017-06-23 | 吉林省有色金属地质勘查局研究所 | 泡沫吸附金的自动解脱装置 |
US20180298465A1 (en) * | 2016-03-31 | 2018-10-18 | Jx Nippon Mining & Metals Corporation | Method for recovering gold from an ore or a refining intermediate containing gold |
US10883155B2 (en) | 2016-03-31 | 2021-01-05 | Jx Nippon Mining & Metals Corporation | Method for recovering gold from an ore or a refining intermediate containing gold |
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CA2908364C (en) | 2017-11-21 |
AU2014245390A1 (en) | 2015-10-22 |
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