JP4016680B2 - Method for dissolving selenium platinum group element-containing material - Google Patents
Method for dissolving selenium platinum group element-containing material Download PDFInfo
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Description
【０００１】
【発明の属する技術分野】
本発明は、セレンと白金族元素を含む滓などからセレンを効率良く浸出して白金族元素と分離することができる溶解処理方法に関する。
【０００２】
【従来の技術】
白金族元素は、銀製錬工程からでる銀アノードスライムや、このスライムに硝酸を加えて金以外の成分を浸出した後に還元して得たスライムなどを原料として回収されている。従来、これらのスライムを溶解するには、王水による溶解、または塩酸と過酸化水素による溶解、または塩酸と塩素ガス吹込みによる溶解が利用されている。
【０００３】
【発明が解決しようとする課題】
白金族元素と共に大量のセレンが共存していると、これを還元によって沈殿化すると白金族のセレン化物が形成される場合が多い。この白金族セレン化物は従来から使用している王水溶解や塩酸および過酸化水素では溶解し難く、特に過酸化水素を使用した場合にはセレン化物の表面で過酸化水素が分解するため酸化剤としての効果を発揮しない。このため従来の溶解法ではセレン化物を完全に溶解するのは困難であった。一方、焙焼によってセレンを酸化セレンの形で気化させて原料から除去する方法では、セレンが６価になる割合が高く、その後の排水処理工程での負荷が大きい。
【０００４】
本発明はセレンが共存する白金族元素含有物を溶解する方法について、従来の上記問題を解決したものであり、セレンを効率良く浸出して白金族元素と分離することができる溶解処理方法を提供する。
【０００５】
【課題を解決する手段】
すなわち、本発明によれば以下の溶解処理方法が提供される。
〔１〕セレン白金族元素含有物に、苛性ソーダと硝酸ソーダのモル比が７５：２５〜８５：１５の混合物からなるフラックスを添加し、該フラックスの共晶温度以上に加熱して溶融し、この溶融物を水浸出して固液分離し、亜セレン酸ソーダを含む液分と白金族元素を含む残渣とに分離することを特徴とするセレン白金族元素含有物の溶解処理方法。
〔２〕白金族元素を含有する水浸出残渣に、過酸化水素と共に塩酸を添加して白金族元素を溶解する請求項１の溶解処理方法。
〔３〕セレン白金族元素含有物が、脱銅製錬スライムの塩酸浸出液から溶媒抽出によって金を分離した抽出残液に二酸化イオウを添加してセレンとテルルを順に還元して沈澱分離した後に、白金族元素とセレンを含む沈殿物を加熱して濃縮すると共にセレンを蒸留分離した蒸留残渣である請求項１または請求項２の溶解処理方法
〔４〕脱銅製錬スライムを塩酸および過酸化水素によってスラリーにし、これを濾過して浸出滓と、金、白金族元素およびセレン、テルルを含む浸出液とに分離し、次に、この浸出液の濃度調整した後に溶媒抽出によって浸出液から金を分離する一方、抽出残液に二酸化イオウを添加してセレンとテルルを順に還元して沈澱分離した後に、白金族元素とセレンを含む沈殿物を加熱して濃縮すると共にセレンを蒸留分離し、この蒸留残渣に苛性ソーダと硝酸ソーダの混合物からなるフラックスを添加して加熱溶融し、この溶融物を水浸出して固液分離し、亜セレン酸ソーダを含む液分と白金族元素を含む残渣とに分離することを特徴とするセレン白金族元素含有物の溶解処理方法。
【０００６】
【発明の実施の形態】
以下、本発明を実施例と共に具体的に説明する。
本発明の溶解処理方法の概略を図１に示す。図示するように本発明の溶解処理方法は、セレン白金族元素含有物に苛性ソーダと硝酸ソーダの混合物からなるフラックスを添加し、該フラックスの共晶温度以上に加熱して溶融し、この溶融物を水浸出して固液分離し、亜セレン酸ソーダを含む液分と白金族元素を含む残渣とに分離することを特徴とするセレン白金族元素含有物の溶解処理方法である。
【０００７】
セレン白金族元素含有物として、例えば、脱銅製錬スライムの塩酸浸出液から溶媒抽出によって金を分離した抽出残液の処理滓が用いられる。この脱銅製錬スライムには金、銀、白金族元素、セレン、テルル等の有価金属が多量に含まれている。この処理方法の一例を図２に示す。図示するように、上記脱銅スライムを塩酸および過酸化水素によってスラリーにし、これを濾過して主に銀を含む浸出滓と、金、白金族元素およびセレン、テルルを含む浸出液とに分離する。次に、この浸出液の液性を調整した後に溶媒抽出によって浸出液から金を分離する。一方、抽出残液には白金族元素、セレン、テルルが残留している。そこで、この抽出残液に二酸化イオウを添加してセレンとテルルを順に還元して沈澱分離する。因みに、テルルはセレンより還元電位が低く、セレンが沈澱した後にテルルが沈澱するので、両者を分離することができる。この還元により白金族元素はセレンと共に沈澱するので、白金族元素とセレンを含む沈殿物を加熱して濃縮すると共にセレンを蒸留分離する。セレンを蒸留分離した後の残渣には白金族元素と未蒸留のセレンとが含まれている。
【０００８】
上記蒸留残渣などのセレン白金族元素含有物に苛性ソーダ(NaOH)と硝酸ソーダ(NaNO3)の混合物からなるフラックスを添加し、これをフラックスの共晶温度以上に加熱して溶融する。この加熱溶融によってセレンは主に４価になり、亜セレン酸ソーダ(Na2SeO3)を生じて溶解する。苛性ソーダと硝酸ソーダの混合物をフラックスとして使用するのは、苛性ソーダを単独に用いると雰囲気からの酸素の供給が不十分となってセレン化ナトリウム(Na2Se)が生成し、これは水浸出時にセレンがメタルに転化して析出するために白金族とセレンを物理的に分離することができなくなる。また、硝酸ソーダを単独に用いると酸化力が強くなり過ぎ、６価のセレンになる割合が高くなるので好ましくない。
【０００９】
溶融温度を下げるため、フラックスの組成は共晶組成近傍が好ましい。具体的には、苛性ソーダ：硝酸ソーダ＝７５：２５〜８５：１５（モル比）であるものが良い。また、加熱温度はフラックスの共晶温度（258℃）以上であり、フラックスが十分な流動性を有してセレン化物を浸出する必要があるため、加熱温度は３５０℃〜４５０℃が望ましい。なお、硝酸ソーダ(NaNO3)はこの温度範囲内では酸素を発生し、ＮＯxは発生し難いが、この温度範囲より高いとＮＯxが発生する割合が高くなり、かつ酸化力が強くなるため６価のセレンになる割合が大きくなる。
【００１０】
セレン白金族元素含有物に上記フラックスを添加して加熱溶融した後に、この溶融物を水浸出して固液分離する。亜セレン酸ソーダは水に溶解し、白金族元素は渣物に残るので、上記溶融物を水浸出して濾過することにより、亜セレン酸ソーダを含む濾液と白金族元素を含む残渣とに分離することができる。この濾液には白金族元素が実質的に含まれておらず、セレンと白金族元素の分離性が良い。一方、残渣に含まれる白金族元素はこの残渣に過酸化水素等の酸化剤と共に塩酸を加えることによって溶出する。これを濾過して白金族元素を含む濾液を回収することができる。
【００１１】
【実施例および比較例】
〔実施例１〕
セレン化パラジウムを主成分とする白金族含有物２０gを原料とし、これに苛性ソーダ２１.７ｇと硝酸ソーダ１１.５ｇを混合し、４００℃で２時間加熱して溶融物とした。この溶融物を冷却した後、水５００mlを入れて１時間攪拌した後に濾過した。この濾液には上記原料中のセレンの９７.４wt％が浸出された。また、この濾液には白金およびパラジウムは検出されなかった。さらに、濾液中の６価セレンは１０wt％以下であった。一方、濾渣を３規定濃度の塩酸でリパルプし、過酸化水素で酸化して溶解した。この結果、溶解液中にパラジウム９５wt％および白金９９wt％以上が浸出された。
【００１２】
〔実施例２〕
苛性ソーダ２０.３ｇと硝酸ソーダ１４.４ｇを用いた他は実施例１と同様にして、セレン化パラジウムを主成分とする白金族含有物20gを加熱溶融し、この溶融物を水浸出して濾過した。この濾液中のセレンの浸出率は９８.２wt％であった。濾液には白金およびパラジウムは検出されなかった。また、濾液中の６価セレンの割合は１０wt％以下であった。一方、濾滓を３規定濃度の塩酸でリパルプし、過酸化水素で酸化して溶解したところ、溶解液中のパラジウムの浸出率は９５wt％、白金の浸出率は９９wt％以上であった。
【００１３】
〔実施例３〕
苛性ソーダ２３.０ｇと硝酸ソーダ８.６ｇを用いた他は実施例１と同様にしてセレン化バラジウムを主成分とする白金族含有物２０ｇを加熱溶融し、この溶融物を水浸出して濾過した。この濾液中のセレンの浸出率は９７.２wt％であった。濾液には白金およびパラジウムは検出されなかった。また濾液中の６価セレンの割合は１０wt％以下であった。一方、濾滓を３規定濃度の塩酸でリパルプし、過酸化水素で酸化して溶解したところ、溶解液中のパラジウムの浸出率は９５wt％であり、白金の浸出率は９９wt％以上であった。
【００１４】
〔実施例４〕
脱銅電解スライム５kgを塩酸５Ｌおよび水２Ｌでリパルプした後、過酸化水素を徐々に添加し、液温を７０℃に維持して酸化浸出した。冷却後、塩化物浸出滓を濾別し、濾液の酸濃度を調整して、ジブチルカルビトール１.５Ｌと接触させて金をジブチルカルビトールに抽出した。抽出後液中の成分濃度は金３０mg/L、セレン５８.９g/L、白金１５m/L、パラジウム１７２mg/Lであった。この液に亜硫酸ガスを吹き込み、液温８０℃でセレンを還元し、冷却後、濾別した。このセレン滓９０１ｇを大気中、７５０℃でセレンを蒸留除去し、蒸留残６.９ｇを回収したところ、その品位はパラジウム４５.２wt％、白金４.２wt％、金１５.３wt％、セレン３４.２wt％であった。この蒸留残に苛性ソーダ５.７ｇと硝酸ソーダ３.０ｇを加え、その他は実施例１と同様にして加熱溶融し、この溶融物を水浸出して濾過した。この濾液中のセレンの浸出率は９８.４wt％であった。濾液には白金およびパラジウムは検出されなかった。また濾液中の６価セレンの割合は１０％以下であった。一方、濾滓を３規定濃度の塩酸でリパルプし、過酸化水素で酸化して溶解したところ、溶解液中のバラジウムの浸出率は９５wt％、白金の浸出率は９９wt％以上であった。
【００１５】
〔比較例１〕
苛性ソーダと硝酸ソーダの混合物に代えて、苛性ソーダを単独に２７ｇ用いた他は実施例１と同様にして、セレン化パラジウムを主成分とする白金族含有物を加熱溶融し、この溶融物を水浸出して濾過した。この濾液中のセレンの浸出率は３３.６wt％であり、実施例１に比べて大幅に低かった。濾液には白金およびパラジウムは検出されなかった。また、濾液中の６価セレンは１０wt％以下であった。一方、濾渣を３規定濃度の塩酸でリパルプし、過酸化水素で酸化して溶解したところ、溶解液中のパラジウムの浸出率は９５wt％、白金の浸出率は９９wt％以上であった。
【００１６】
〔比較例２〕
苛性ソーダと硝酸ソーダの混合物に代えて、硝酸ソーダを単独に５７.６ｇ用いた他は実施例１と同様にして、セレン化パラジウムを主成分とする白金族含有物を加熱溶融し、この溶融物を水浸出して濾過した。この濾液中のセレンの浸出率は９８.５wt％であった。濾液には白金およびパラジウムは検出されなかった。一方、濾液中の６価セレンは２５wt％であり、実施例１より大幅に多かった。また、濾渣を３規定濃度の塩酸でリパルプし、過酸化水素で酸化して溶解したところ、溶解液中のパラジウムの浸出率は９５wt％、白金の浸出率は９９wt％以上であった。
【００１７】
【発明の効果】
本発明の処理方法によれば、従来、工業的湿式プロセスでは溶解不可能であった白金族セレン化物をほぼ完全に溶解でき、かつ乾式法で問題となっていた６価セレンの生成も低く抑えられる。また、溶融物からセレンを溶解するには水だけで十分であり、処理コストを低減することができる。
【図面の簡単な説明】
【図１】本発明の溶解処理方法の概略を示す工程図。
【図２】脱銅スライムの処理から本発明の処理方法に至る概略を示す工程図。[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a dissolution treatment method capable of efficiently leaching selenium from a soot containing selenium and a platinum group element and separating it from the platinum group element.
[0002]
[Prior art]
The platinum group elements are recovered using, as a raw material, silver anode slime from the silver smelting process, slime obtained by adding nitric acid to the slime and leaching components other than gold, and the like. Conventionally, in order to dissolve these slimes, dissolution by aqua regia, dissolution by hydrochloric acid and hydrogen peroxide, or dissolution by blowing hydrochloric acid and chlorine gas is used.
[0003]
[Problems to be solved by the invention]
When a large amount of selenium coexists with the platinum group element, precipitation of the selenium by reduction often forms a platinum group selenide. This platinum group selenide is difficult to dissolve with the conventional aqua regia solution or hydrochloric acid and hydrogen peroxide. Especially when hydrogen peroxide is used, the hydrogen peroxide is decomposed on the surface of the selenide, so that the oxidizing agent As an effect. For this reason, it has been difficult to completely dissolve the selenide by the conventional dissolution method. On the other hand, in the method in which selenium is vaporized in the form of selenium oxide by roasting and removed from the raw material, the ratio of selenium to hexavalent is high, and the load in the subsequent wastewater treatment process is large.
[0004]
The present invention solves the above-mentioned conventional problems with respect to a method for dissolving a platinum group element-containing material in which selenium coexists, and provides a dissolution treatment method capable of leaching selenium efficiently and separating it from the platinum group element. To do.
[0005]
[Means for solving the problems]
That is, according to the present invention, the following dissolution treatment method is provided.
[1] A flux composed of a mixture of caustic soda and sodium nitrate having a molar ratio of 75:25 to 85:15 is added to the selenium platinum group element-containing material, and the mixture is heated and melted above the eutectic temperature of the flux. A method for dissolving a selenium platinum group element-containing material, wherein the melt is leached with water and separated into a solid and a liquid, and separated into a liquid containing sodium selenite and a residue containing a platinum group element.
[2] The dissolution treatment method according to
[3] After the selenium platinum group element-containing material is precipitated and separated by sequentially reducing selenium and tellurium by adding sulfur dioxide to an extraction residue obtained by separating the gold from the hydrochloric acid leaching solution of the decopper smelting slime by solvent extraction. 3. The dissolution treatment method of [1] or [2], wherein the precipitate containing the group element and selenium is concentrated by heating and selenium is separated by distillation. to a leaching slag this was filtered, gold, platinum group elements and selenium, and separated into a leachate containing tellurium, then while separating gold from the leachate by a solvent extraction after adjusting the concentration of the leaching solution, extracted Sulfur dioxide is added to the residual liquid to reduce selenium and tellurium in order and precipitate, and then the precipitate containing platinum group elements and selenium is heated and concentrated, and selenium is distilled. Then, a flux composed of a mixture of caustic soda and sodium nitrate is added to the distillation residue and heated and melted. The melt is leached with water and separated into solid and liquid, containing a liquid containing sodium selenite and a platinum group element. A method for dissolving a selenium platinum group element-containing material, which is separated into residues.
[0006]
DETAILED DESCRIPTION OF THE INVENTION
Hereinafter, the present invention will be specifically described together with examples.
An outline of the dissolution treatment method of the present invention is shown in FIG. As shown in the figure, in the dissolution treatment method of the present invention, a flux comprising a mixture of caustic soda and sodium nitrate is added to a selenium platinum group element-containing material, and the melt is heated to a temperature equal to or higher than the eutectic temperature of the flux. A method for dissolving a selenium platinum group element-containing material, which comprises leaching with water and solid-liquid separation to separate into a liquid containing sodium selenite and a residue containing a platinum group element.
[0007]
As the selenium platinum group element-containing material, for example, a processing residue of an extraction residual liquid obtained by separating gold by solvent extraction from a hydrochloric acid leaching solution of a decopper smelting slime is used. This copper removal smelting slime contains a large amount of valuable metals such as gold, silver, platinum group elements, selenium and tellurium. An example of this processing method is shown in FIG. As shown in the figure, the decopperized slime is slurried with hydrochloric acid and hydrogen peroxide and filtered to separate into a leach cake containing mainly silver and a leach solution containing gold, platinum group elements, selenium and tellurium. Next, after adjusting the liquidity of the leachate, gold is separated from the leachate by solvent extraction. On the other hand, platinum group elements, selenium, and tellurium remain in the extraction residual liquid. Therefore, sulfur dioxide is added to this extraction residue to reduce selenium and tellurium in order and precipitate and separate them. By the way, tellurium has a lower reduction potential than selenium, and tellurium precipitates after selenium precipitates, so that both can be separated. Since the platinum group element is precipitated together with selenium by this reduction, the precipitate containing the platinum group element and selenium is concentrated by heating and selenium is separated by distillation. The residue after separation of selenium by distillation contains platinum group elements and undistilled selenium.
[0008]
A flux composed of a mixture of caustic soda (NaOH) and sodium nitrate (NaNO 3 ) is added to a selenium platinum group element-containing material such as the above distillation residue, and this is heated and melted above the eutectic temperature of the flux. By this heating and melting, selenium mainly becomes tetravalent, and soda selenite (Na 2 SeO 3 ) is generated and dissolved. A mixture of caustic soda and sodium nitrate is used as a flux because when sodium hydroxide is used alone, oxygen supply from the atmosphere is insufficient and sodium selenide (Na 2 Se) is produced. Since it is converted to metal and deposited, the platinum group and selenium cannot be physically separated. Moreover, it is not preferable to use sodium nitrate alone because the oxidizing power becomes too strong and the ratio of hexavalent selenium increases.
[0009]
In order to lower the melting temperature, the flux composition is preferably near the eutectic composition. Specifically, it is preferable to use caustic soda: sodium nitrate = 75: 25 to 85:15 (molar ratio). Further, the heating temperature is equal to or higher than the eutectic temperature (258 ° C.) of the flux, and since the flux has sufficient fluidity to leach selenide, the heating temperature is preferably 350 ° C. to 450 ° C. It should be noted that sodium nitrate (NaNO 3 ) generates oxygen within this temperature range and hardly generates NO x , but if it is higher than this temperature range, the rate of generation of NO x increases and the oxidizing power increases. The ratio of hexavalent selenium increases.
[0010]
After the flux is added to the selenium platinum group element-containing material and heated and melted, the melt is leached with water and subjected to solid-liquid separation. Since sodium selenite dissolves in water and platinum group elements remain in the residue, the above melt is leached and filtered to separate the filtrate containing sodium selenite and the residue containing platinum group elements. can do. This filtrate is substantially free of platinum group elements and has good separability between selenium and platinum group elements. On the other hand, platinum group elements contained in the residue are eluted by adding hydrochloric acid to the residue together with an oxidizing agent such as hydrogen peroxide. This can be filtered to recover the filtrate containing the platinum group element.
[0011]
Examples and Comparative Examples
[Example 1]
20 g of a platinum group-containing material mainly composed of palladium selenide was used as a raw material, 21.7 g of caustic soda and 11.5 g of sodium nitrate were mixed, and heated at 400 ° C. for 2 hours to obtain a melt. After cooling the melt, 500 ml of water was added and stirred for 1 hour, followed by filtration. In this filtrate, 97.4 wt% of selenium in the raw material was leached. Also, platinum and palladium were not detected in this filtrate. Furthermore, hexavalent selenium in the filtrate was 10 wt% or less. On the other hand, the residue was repulped with 3N hydrochloric acid, oxidized with hydrogen peroxide and dissolved. As a result, 95 wt% of palladium and 99 wt% or more of platinum were leached into the solution.
[0012]
[Example 2]
Except that 20.3 g of caustic soda and 14.4 g of sodium nitrate were used, 20 g of a platinum group-containing material mainly composed of palladium selenide was heated and melted, and this melt was leached with water and filtered. did. The leaching rate of selenium in this filtrate was 98.2 wt%. Platinum and palladium were not detected in the filtrate. The ratio of hexavalent selenium in the filtrate was 10 wt% or less. On the other hand, when the filter cake was repulped with 3N hydrochloric acid, oxidized with hydrogen peroxide and dissolved, the leaching rate of palladium in the solution was 95 wt%, and the leaching rate of platinum was 99 wt% or more.
[0013]
Example 3
Except for using 23.0 g of caustic soda and 8.6 g of sodium nitrate, 20 g of a platinum group-containing material mainly composed of barium selenide was heated and melted in the same manner as in Example 1, and this melt was leached with water and filtered. . The leaching rate of selenium in this filtrate was 97.2 wt%. Platinum and palladium were not detected in the filtrate. The ratio of hexavalent selenium in the filtrate was 10 wt% or less. On the other hand, when the filter cake was repulped with 3N hydrochloric acid, oxidized with hydrogen peroxide and dissolved, the leaching rate of palladium in the solution was 95 wt%, and the leaching rate of platinum was 99 wt% or more. .
[0014]
Example 4
After repulping 5 kg of copper removal electrolytic slime with 5 L of hydrochloric acid and 2 L of water, hydrogen peroxide was gradually added, and the temperature of the liquid was maintained at 70 ° C., and leaching was performed. After cooling, the chloride leachate was filtered off, the acid concentration of the filtrate was adjusted, and contacted with 1.5 L of dibutyl carbitol to extract gold into dibutyl carbitol. The component concentrations in the liquid after extraction were gold 30 mg / L, selenium 58.9 g / L, platinum 15 m / L, palladium 172 mg / L. Sulfurous acid gas was blown into this liquid, selenium was reduced at a liquid temperature of 80 ° C., cooled, and filtered. Selenium was distilled off from 901 g of this selenium soot at 750 ° C. in the atmosphere, and 6.9 g of distillation residue was recovered. The quality was palladium 45.2 wt%, platinum 4.2 wt%, gold 15.3 wt%, selenium 34 It was 2 wt%. To this distillation residue, 5.7 g of caustic soda and 3.0 g of sodium nitrate were added, and the others were heated and melted in the same manner as in Example 1. The melt was leached with water and filtered. The leaching rate of selenium in this filtrate was 98.4 wt%. Platinum and palladium were not detected in the filtrate. The ratio of hexavalent selenium in the filtrate was 10% or less. On the other hand, when the filter cake was repulped with 3N hydrochloric acid, oxidized with hydrogen peroxide and dissolved, the leach rate of barium in the solution was 95 wt%, and the leach rate of platinum was 99 wt% or more.
[0015]
[Comparative Example 1]
In place of the mixture of caustic soda and sodium nitrate, 27 g of caustic soda alone was used, and the platinum group-containing material mainly composed of palladium selenide was heated and melted in the same manner as in Example 1, and this melt was leached with water. And filtered. The selenium leaching rate in the filtrate was 33.6 wt%, which was significantly lower than that in Example 1. Platinum and palladium were not detected in the filtrate. The hexavalent selenium in the filtrate was 10 wt% or less. On the other hand, when the residue was repulped with 3N hydrochloric acid, oxidized with hydrogen peroxide and dissolved, the leaching rate of palladium in the solution was 95 wt% and the leaching rate of platinum was 99 wt% or more.
[0016]
[Comparative Example 2]
In place of the mixture of caustic soda and sodium nitrate, a platinum group-containing material mainly composed of palladium selenide was heated and melted in the same manner as in Example 1 except that 57.6 g of sodium nitrate was used alone. Was leached with water and filtered. The leaching rate of selenium in this filtrate was 98.5 wt%. Platinum and palladium were not detected in the filtrate. On the other hand, hexavalent selenium in the filtrate was 25 wt%, which was much more than in Example 1. Further, when the residue was repulped with 3N hydrochloric acid, oxidized with hydrogen peroxide and dissolved, the leaching rate of palladium in the solution was 95 wt%, and the leaching rate of platinum was 99 wt% or more.
[0017]
【The invention's effect】
According to the treatment method of the present invention, platinum group selenide, which has heretofore been impossible to dissolve in an industrial wet process, can be almost completely dissolved, and the production of hexavalent selenium, which has been a problem in the dry method, is also kept low. It is done. Also, water alone is sufficient to dissolve selenium from the melt, and the processing cost can be reduced.
[Brief description of the drawings]
FIG. 1 is a process diagram showing an outline of a dissolution treatment method of the present invention.
FIG. 2 is a process diagram showing an outline from the treatment of copper removal slime to the treatment method of the present invention.
Claims (4)
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| JP2002072848A JP4016680B2 (en) | 2002-03-15 | 2002-03-15 | Method for dissolving selenium platinum group element-containing material |
| CN038106884A CN1653198B (en) | 2002-03-15 | 2003-03-14 | Method for separating platinum group element |
| KR1020107002024A KR20100019577A (en) | 2002-03-15 | 2003-03-14 | Method for separating platinum group element |
| PCT/JP2003/003108 WO2003078670A1 (en) | 2002-03-15 | 2003-03-14 | Method for separating platinum group element |
| DE2003192375 DE10392375T5 (en) | 2002-03-15 | 2003-03-14 | Separation process for platinum group elements |
| KR20047014284A KR100956050B1 (en) | 2002-03-15 | 2003-03-14 | Method for separating platinum group element |
| US10/506,613 US7479262B2 (en) | 2002-03-15 | 2003-03-14 | Method for separating platinum group element |
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| DE10392375T5 (en) | 2002-03-15 | 2005-06-30 | Mitsubishi Materials Corp. | Separation process for platinum group elements |
| CA2730558C (en) * | 2002-11-29 | 2011-11-15 | Mitsubishi Materials Corporation | Separation process for platinum group elements |
| JP4656508B2 (en) * | 2005-05-31 | 2011-03-23 | 財団法人電力中央研究所 | Determination of selenium by chemical form |
| DE102006030731A1 (en) * | 2006-06-30 | 2008-01-03 | H.C. Starck Gmbh | Recycling of superalloys |
| JP2010077510A (en) | 2008-09-29 | 2010-04-08 | Nippon Mining & Metals Co Ltd | Method of separating rhodium from platinum and/or palladium |
| CN104928483B (en) * | 2015-05-15 | 2017-07-14 | 西北矿冶研究院 | Method for comprehensively recovering silver, selenium, tellurium and copper from copper telluride residues |
| JP6585955B2 (en) * | 2015-07-31 | 2019-10-02 | Ｊｘ金属株式会社 | Method for separating Ru, Rh and Ir from a selenium platinum group element-containing material |
| JP6400047B2 (en) * | 2016-06-03 | 2018-10-03 | Ｊｘ金属株式会社 | Method for treating metal-containing acidic aqueous solution |
| JP6905402B2 (en) * | 2017-07-03 | 2021-07-21 | 住友電気工業株式会社 | Separation method of metal components |
| JP7198036B2 (en) * | 2018-10-17 | 2022-12-28 | Ｊｘ金属株式会社 | Selenium production method |
| JP7331744B2 (en) | 2020-03-13 | 2023-08-23 | 三菱マテリアル株式会社 | Method for leaching sparingly soluble platinum group elements |
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