JP3548097B2 - Separation and recovery method of bismuth and copper etc. from treatment object containing cuprous oxide and bismuth - Google Patents
Separation and recovery method of bismuth and copper etc. from treatment object containing cuprous oxide and bismuth Download PDFInfo
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- JP3548097B2 JP3548097B2 JP2000217196A JP2000217196A JP3548097B2 JP 3548097 B2 JP3548097 B2 JP 3548097B2 JP 2000217196 A JP2000217196 A JP 2000217196A JP 2000217196 A JP2000217196 A JP 2000217196A JP 3548097 B2 JP3548097 B2 JP 3548097B2
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Description
【０００１】
【産業上の利用分野】
本発明は、非鉄製錬工程等で発生する酸化第一銅及びビスマスを含む処理対象物例えばアルカリ処理をした電解沈殿銅から、有価物を分離回収する方法に関するものであり、更に詳しく述べると有価物であるビスマスを銅等と湿式処理により分離し回収する方法に関するものである。
【０００２】
【従来の技術】
砒素、アンチモン、ビスマスのいわゆる５族元素は、鉛、銅、錫、銀、金などの鉱石中に含まれ、これらの非鉄金属の製錬副産物として産出されている。砒素、アンチモン、ビスマスは、銅や鉛鉱石に随伴して産出されることが多く、乾式製錬によってその粗金属中に残留する。例えば、粗銅中に残留した砒素、アンチモン、ビスマスは、銅の電解精製工程において他の不純物と共に電解液に濃縮される。一方大部分の砒素、アンチモン、ビスマスは、銅製錬の乾式工程で高熱によって揮発し、煙灰として鉛、砒素、アンチモンなどと共にコットレル等に捕集され、これらは更に鉛製錬工程に送られ分離回収される。
【０００３】
銅電解液中に濃縮された砒素、アンチモン、ビスマスは、例えばイオン交換樹脂や脱銅電解で除去される。脱銅電解で発生した殿物が電解沈殿銅と呼ばれており、砒素、アンチモン、ビスマスが濃縮されている。
【０００４】
電解沈殿銅中には砒素が含まれており、この砒素の安定化処理が困難であり、多くの場合貯蔵されている。また電解沈殿銅には砒素、アンチモン、ビスマスの他に有価物である銅が多量に含まれており、有価物回収の観点から貯蔵には問題がある。
【０００５】
また砒素、アンチモン、ビスマスは挙動を共にすることが多く、これらの分離も課題となっている。
【０００６】
【発明が解決しようとする課題】
上記問題点を解決する、湿式法によるビスマスと銅等を分離し、有価物であるビスマスを回収する方法を提供するものである。
【０００７】：
【課題を解決するための手段】本発明者らは、酸化第一銅及びビスマスを含む処理対象物例えばアルカリ処理をした電解沈殿銅からの銅等とビスマスの分離回収方法の種々の検討を行った結果、分離回収方法として、
（１）酸化第一銅及びビスマスを含む処理対象物を１段階目の浸出として５０〜２００ｇ／Ｌの硫酸で浸出し、銅、砒素、ニッケルからなる金属群の内少なくとも一種以上の金属を溶出させた後、２段階目の浸出として該硫酸浸出残渣を２〜３Ｍ／Ｌの塩酸で浸出し、ビスマスを溶出させることを特徴とする酸化第一銅及びビスマスを含む処理対象物から銅等とビスマスの分離回収方法。
（２）硫酸浸出の条件が、液温４０℃以上、処理時間２時間以上、パルプ濃度９０ｄｒｙ−ｇ／Ｌ以下であることを特徴とする（１）に記載の方法。
（３）塩酸浸出の条件が、液温２０℃以上、処理時間１時間以上、パルプ濃度７５ｄｒｙ−ｇ／Ｌ以下であることを特徴とする（１）に記載の方法。
（４）上記（１）記載の塩酸処理後の処理液をｐＨ＝２〜３とし、ビスマスを残渣中に回収することを特徴とする請求項１記載の方法。
を提供する。
【作用】以下本発明の構成を詳しく説明する。なお構成は例を挙げて説明しているが、本発明はこの例に制限されるものではない。
【０００８】
砒素、アンチモン、ビスマスのいわゆる５族元素は、鉛、銅、錫、銀、金などの鉱石中に含まれ、これらの非鉄金属の製錬副産物として産出されている。砒素、アンチモン、ビスマスは、銅や鉛鉱石に随伴して産出されることが多く、乾式製錬によってその粗金属中に残留する。例えば、粗銅中に残留した砒素、アンチモン、ビスマスは、銅の電解精製工程において他の不純物と共に電解液に濃縮される。一方大部分の砒素、アンチモン、ビスマスは、銅製錬の乾式工程で高熱によって揮発し、煙灰として鉛、砒素、アンチモンなどと共にコットレル等に捕集され、これらは更に鉛製錬工程に送られ分離回収される。
【０００９】
銅電解液中に濃縮された砒素、アンチモン、ビスマスは、例えばイオン交換樹脂や脱銅電解で除去される。この脱銅電解で発生した殿物が電解沈殿銅と呼ばれており、銅、砒素、アンチモン、ビスマスが濃縮されている。
【００１０】
電解沈殿銅中には砒素が含まれており、この砒素の安定化処理が困難なため、多くの場合貯蔵されている。また電解沈殿銅には砒素、アンチモン、ビスマスの他に有価物である銅が多量に含まれており、有価物回収の観点から貯蔵には問題がある。
【００１１】
本発明者らは、酸化第一銅及びビスマスを含む処理対象物例えばアルカリ処理をした電解沈殿銅からの銅等とビスマスの分離回収の種々の検討を行った結果、アルカリ浸出をした電解沈殿銅を硫酸浸出して銅、砒素、ニッケルを溶出させた後、浸出残渣を塩酸浸出しビスマスを溶出させることによりビスマスと銅等との分離ができるとの知見を得た。
【００１２】
すなわちアルカリ処理をした電解沈殿銅を硫酸で浸出すると銅、砒素、ニッケルの大部分が浸出される。このときビスマスは浸出されず残渣に残留濃縮する。このアルカリ処理をした電解沈殿銅中の銅の形態は、アルカリ処理により酸化第一銅に変換されており、この酸化第一銅は硫酸に容易に溶解する。このため、銅とビスマスの分離が効率よく行われる。アルカリ処理後の電解沈殿銅品位は、例えばビスマス１〜１０％、銅５０〜７０％、砒素１〜１０％、ニッケル１〜１０％である。この硫酸浸出残渣を塩酸で浸出することにより、ビスマスが溶出するため銅等とビスマスの分離が可能であることを見い出した。
【００１３】
硫酸で浸出された銅、砒素、ニッケルの回収は、例えば中和処理が適用可能である。ここで発生した中和残渣は非鉄金属製錬の乾式工程に繰返すことが可能である。また浸出液は、液中に硫酸が残留しているため、再度硫酸浸出工程へ繰返すことが可能である。
【００１４】
硫酸濃度が高くなるとＢｉが浸出されるため、硫酸濃度は５０〜２００ｇ／Ｌ、さらに詳細に述べると８０から１００ｇ／Ｌが好ましい。この時の硫酸浸出後液中の硫酸濃度は約２０ｇ／Ｌ程度であり、硫酸濃度を調整した後再度硫酸浸出に繰返すことが可能である。また硫酸浸出後液のブリードオフ時、硫酸濃度が比較的低いため、中和処理による銅等の有価物回収が容易に行えるメリットもある。
【表１】
硫酸浸出の処理時間は、２時間以上更に詳しく述べると３〜５時間が好ましい。処理時間が短いと特に銅の浸出率が低くなる。処理時間が５時間を超えるとＢｉが溶出する傾向であるため好ましくない。
【表２】
硫酸処理の液温が低いと銅の浸出率が低くなるため、銅等とビスマスの分離は困難となる。液温は４０℃以上、更に詳しく述べると５５〜６５℃が好ましい。液温が６０℃より高いと、銅の浸出率はさほど上昇せず熱エネルギーのロスとなるため好ましくない。
【表３】
硫酸浸出のパルプ濃度が上昇するとＣｕ、Ａｓ、Ｎｉの浸出率が低下しＢｉとの分離が困難となる。パルプ濃度は９０ｄｒｙ−ｇ／Ｌ以下、さらに詳しく述べると４０〜７０ｄｒｙ−ｇ／Ｌが好ましい。
【表４】
硫酸浸出で得られた残渣はビスマスが主成分であり、ビスマスの形態は酸化ビスマスと考えられる。このビスマス化合物は、酸類、例えば塩酸に溶解する。
【００１９】
塩酸浸出の塩酸濃度は２〜３モル／Ｌ以上が好ましい。塩酸濃度が薄いとビスマス浸出率が上がらない。
【表５】
塩酸溶解の液温は、２０℃以上更に詳しく述べると５５〜６５℃が好ましい。
【表６】
塩酸浸出の浸出時間は、１時間以上更に詳しく述べると２時間以上が好ましい。
【表７】
塩酸浸出のパルプ濃度は、７５ｄｒｙ−ｇ／Ｌ以下、更に詳しく述べると４５〜６０ｄｒｙ−ｇ／Ｌが好ましい。パルプ濃度が高いとＢｉ浸出率が低下する。
【表８】
塩酸浸出されたビスマスの回収方法は、例えば加水分解法の適用が可能である。この加水分解法は、含ビスマス塩酸溶液のｐＨを上げていくとＢｉが加水分解を起こしオキシ塩化ビスマス（ＢｉＯＣｌ）として回収する方法である。
【００２４】
本発明により、アルカリ処理をした電解沈殿銅から銅等とビスマスを分離回収することが可能となった。
【００２５】
以上説明したように、銅等とビスマスとを分離する簡便な方法を確立した。
【実施例】
【００２６】
以下本発明の実施例を説明する。なお本発明は実施例に限定されるものではない。
【００２７】
銅製錬工程中間処理物として産出されるアルカリ処理をした電解沈殿銅の組成は表の通りである。この電解沈殿銅中の銅の形態は酸化第一銅である。
【００２８】
【表９】
電解沈殿銅９６０ｗｅｔ−ｇを硫酸濃度８０ｇ／Ｌの液１２Ｌにリパルプし、６０℃４ｈｒ攪拌放置後、固液分離を行った。このとき残渣は３３９ｗｅｔ−ｇ（付着水分３４．５％）得られた。分析値を表１０に示す。
【００３０】
【表１０】
硫酸浸出残渣２４０ｗｅｔ−ｇを常温の２モル／Ｌ塩酸溶液３Ｌにリパルプした。１時間のリパルプ後、濾過による固液分離を実施し、１６７．７ｗｅｔ−ｇ（付着水分５３．２％）の残渣を得た。
【００３２】
【表１１】
６０℃に加温した塩酸浸出後液２．９Ｌに２００ｇ／ＬのＮａＯＨ０．９８Ｌを添加し、ｐＨ２．２５とし４時間攪拌放置した。その後固液分離を実施し、２７．４ｗｅｔ−ｇ（付着水分５８．５％）の残渣を得た。この残渣の品位を表に示す。
【表１２】
【００３４】
アルカリ処理を行っていない電解沈殿銅１６．４ｄｒｙ−ｇを８０ｇ／Ｌの硫酸０．２５Ｌにリパルプし、６０℃×４ｈｒ攪拌放置した。その後、固液分離を実施し、浸出率を算出した結果、次のようになった。
表１に示す銅の浸出率８５％以上に比べ、８．２％と比べはるかに悪い値であり、銅、ビスマスの効率的分離回収が不可能であった。
【表１３】
【発明の効果】
以上説明したように、本発明により電解沈殿銅から有価物であるビスマスと銅等とを分離回収することが可能となった。
【図面の簡単な説明】
【図１】は、本発明の処理フローの一態様を示す。[0001]
[Industrial applications]
The present invention relates to a method for separating and recovering valuable resources from an object to be treated containing cuprous oxide and bismuth generated in a non-ferrous smelting process or the like, for example, electrolytically precipitated copper that has been subjected to alkali treatment. The present invention relates to a method for separating and recovering bismuth as a substance from copper or the like by wet processing.
[0002]
[Prior art]
The so-called Group 5 elements of arsenic, antimony, and bismuth are contained in ores such as lead, copper, tin, silver, and gold, and are produced as by-products of smelting these nonferrous metals. Arsenic, antimony, and bismuth are often produced in association with copper and lead ore, and remain in the crude metal by dry smelting. For example, arsenic, antimony, and bismuth remaining in the blister copper are concentrated together with other impurities in the electrolytic solution in the copper electrolytic purification step. On the other hand, most of arsenic, antimony, and bismuth are volatilized by high heat in the copper smelting dry process, and are collected as fumes along with lead, arsenic, antimony, etc. in cotrels and the like. Is done.
[0003]
Arsenic, antimony, and bismuth concentrated in the copper electrolyte are removed by, for example, an ion exchange resin or copper removal electrolysis. The deposit generated by the copper removal electrolysis is called electrolytic precipitated copper, and arsenic, antimony, and bismuth are concentrated.
[0004]
The electrolytically precipitated copper contains arsenic, which is difficult to stabilize, and is often stored. Further, electrolytically precipitated copper contains a large amount of valuable copper in addition to arsenic, antimony and bismuth, and there is a problem in storage from the viewpoint of recovering valuable resources.
[0005]
In addition, arsenic, antimony, and bismuth often behave together, and their separation is also an issue.
[0006]
[Problems to be solved by the invention]
An object of the present invention is to provide a method of solving the above-mentioned problems, separating bismuth, copper, and the like by a wet method and recovering bismuth which is a valuable resource.
[0007]:
Means for Solving the Problems The present inventors have conducted various studies on a method for separating and recovering bismuth and copper etc. from an object to be treated containing cuprous oxide and bismuth, for example, electrolytically precipitated copper subjected to alkali treatment. As a result, as a separation and recovery method,
(1) The object to be treated including cuprous oxide and bismuth is leached with 50 to 200 g / L sulfuric acid as a first stage leaching to elute at least one or more metals from the metal group consisting of copper, arsenic and nickel. after the sulfuric acid leach residue as second stage leach leached with hydrochloric acid 2 to 3 m / L, copper from the processing object including a first copper and bismuth oxide and feature eluting the bismuth And recovery of bismuth and bismuth.
(2) The method according to (1), wherein the conditions for sulfuric acid leaching are a liquid temperature of 40 ° C. or more, a treatment time of 2 hours or more, and a pulp concentration of 90 dry-g / L or less.
(3) The method according to (1), wherein the conditions for hydrochloric acid leaching are a liquid temperature of 20 ° C. or more, a treatment time of 1 hour or more, and a pulp concentration of 75 dry-g / L or less.
(4) The method according to (1), wherein the treatment solution after the hydrochloric acid treatment described in (1) is adjusted to pH = 2 to 3, and bismuth is recovered in a residue.
I will provide a.
The structure of the present invention will be described below in detail. Although the configuration has been described using an example, the present invention is not limited to this example.
[0008]
The so-called Group 5 elements of arsenic, antimony, and bismuth are contained in ores such as lead, copper, tin, silver, and gold, and are produced as by-products of smelting these nonferrous metals. Arsenic, antimony, and bismuth are often produced in association with copper and lead ore, and remain in the crude metal by dry smelting. For example, arsenic, antimony, and bismuth remaining in the blister copper are concentrated together with other impurities in the electrolytic solution in the copper electrolytic purification step. On the other hand, most of arsenic, antimony, and bismuth are volatilized by high heat in the copper smelting dry process, and are collected as fumes along with lead, arsenic, antimony, etc. in cotrels and the like. Is done.
[0009]
Arsenic, antimony, and bismuth concentrated in the copper electrolyte are removed by, for example, an ion exchange resin or copper removal electrolysis. The deposit generated by this copper removal electrolysis is called electrolytic precipitated copper, and copper, arsenic, antimony, and bismuth are concentrated.
[0010]
Since arsenic is contained in electrolytically precipitated copper, and it is difficult to stabilize this arsenic, it is often stored. Further, electrolytically precipitated copper contains a large amount of valuable copper in addition to arsenic, antimony and bismuth, and there is a problem in storage from the viewpoint of recovering valuable resources.
[0011]
The present inventors have conducted various studies on the separation and recovery of bismuth and copper and the like from a treatment object containing cuprous oxide and bismuth, such as alkali-treated electrolytically precipitated copper. It was found that bismuth can be separated from copper and the like by eluting copper, arsenic and nickel by leaching sulfuric acid to elute copper, arsenic and nickel, and then leaching the leaching residue with hydrochloric acid to elute bismuth.
[0012]
That is, when electrolytically precipitated copper subjected to alkali treatment is leached with sulfuric acid, most of copper, arsenic, and nickel are leached. At this time, the bismuth is not leached and is concentrated in the residue. The form of the copper in the electrolytically precipitated copper that has been subjected to the alkali treatment has been converted to cuprous oxide by the alkali treatment, and the cuprous oxide is easily dissolved in sulfuric acid. For this reason, copper and bismuth are efficiently separated. The quality of electrolytically precipitated copper after the alkali treatment is, for example, 1 to 10% of bismuth, 50 to 70% of copper, 1 to 10% of arsenic, and 1 to 10% of nickel. By leaching the sulfuric acid leaching residue with hydrochloric acid, bismuth was eluted, and it was found that bismuth could be separated from copper and the like.
[0013]
For recovery of copper, arsenic, and nickel leached with sulfuric acid, for example, a neutralization treatment can be applied. The neutralized residue generated here can be repeated in the dry process of nonferrous metal smelting. In addition, since the sulfuric acid remains in the leaching solution, the leaching solution can be repeated to the sulfuric acid leaching step again.
[0014]
Since Bi is leached when the sulfuric acid concentration increases, the sulfuric acid concentration is preferably from 50 to 200 g / L, and more preferably from 80 to 100 g / L. At this time, the sulfuric acid concentration in the solution after sulfuric acid leaching is about 20 g / L, and the sulfuric acid leaching can be repeated again after adjusting the sulfuric acid concentration. In addition, since the sulfuric acid concentration is relatively low at the time of bleed-off of the solution after sulfuric acid leaching, there is an advantage that it is possible to easily recover valuable materials such as copper by neutralization.
[Table 1]
The treatment time of sulfuric acid leaching is preferably 3 to 5 hours, more specifically, 2 hours or more. If the processing time is short, the leaching rate of copper is particularly low. If the treatment time exceeds 5 hours, Bi tends to elute, which is not preferable.
[Table 2]
If the liquid temperature of the sulfuric acid treatment is low, the leaching rate of copper becomes low, so that it becomes difficult to separate bismuth from copper or the like. The liquid temperature is preferably 40 ° C. or more, more preferably 55 to 65 ° C. If the liquid temperature is higher than 60 ° C., the leaching rate of copper does not increase so much, and heat energy is lost, which is not preferable.
[Table 3]
When the pulp concentration of sulfuric acid leaching increases, the leaching rate of Cu, As, and Ni decreases, and separation from Bi becomes difficult. The pulp concentration is preferably 90 dry-g / L or less, more preferably 40 to 70 dry-g / L.
[Table 4]
The residue obtained by sulfuric acid leaching is mainly composed of bismuth, and the form of bismuth is considered to be bismuth oxide. This bismuth compound dissolves in acids, for example, hydrochloric acid.
[0019]
The hydrochloric acid concentration in the hydrochloric acid leaching is preferably 2 mol / L or more. If the hydrochloric acid concentration is low, the leaching rate of bismuth does not increase.
[Table 5]
The liquid temperature for dissolving hydrochloric acid is preferably from 20 to 55 ° C, more specifically 55 to 65 ° C.
[Table 6]
The leaching time of hydrochloric acid leaching is preferably 1 hour or more, and more preferably 2 hours or more.
[Table 7]
The pulp concentration in the hydrochloric acid leaching is preferably 75 dry-g / L or less, more preferably 45 to 60 dry-g / L. If the pulp concentration is high, the Bi leaching rate decreases.
[Table 8]
As a method for recovering bismuth leached with hydrochloric acid, for example, a hydrolysis method can be applied. In this hydrolysis method, Bi is hydrolyzed as the pH of the bismuth-containing hydrochloric acid solution is increased, and is recovered as bismuth oxychloride (BiOCl).
[0024]
According to the present invention, it has become possible to separate and recover copper and the like and bismuth from electrolytically precipitated copper subjected to alkali treatment.
[0025]
As described above, a simple method of separating copper and the like from bismuth has been established.
【Example】
[0026]
Hereinafter, embodiments of the present invention will be described. Note that the present invention is not limited to the embodiments.
[0027]
The composition of the alkali-treated electrolytically precipitated copper produced as an intermediate in the copper smelting process is as shown in the table. The form of copper in the electrolytically precipitated copper is cuprous oxide.
[0028]
[Table 9]
960 wet-g of electrolytically precipitated copper was repulped into 12 L of a solution having a sulfuric acid concentration of 80 g / L, and left at 60 ° C. with stirring for 4 hours, followed by solid-liquid separation. At this time, a residue of 339 wet-g (adhered moisture of 34.5%) was obtained. The analytical values are shown in Table 10.
[0030]
[Table 10]
240 wet-g of the sulfuric acid leaching residue was repulped in 3 L of a 2 mol / L hydrochloric acid solution at room temperature. After 1 hour of repulping, solid-liquid separation was performed by filtration to obtain a residue of 167.7 wet-g (adhered water 53.2%).
[0032]
[Table 11]
0.98 L of 200 g / L NaOH was added to 2.9 L of the hydrochloric acid leached solution heated to 60 ° C. to adjust the pH to 2.25, and the mixture was left to stir for 4 hours. Thereafter, solid-liquid separation was performed to obtain a residue of 27.4 wet-g (attached moisture: 58.5%). The quality of this residue is shown in the table.
[Table 12]
[0034]
16.4 dry-g of electrolytically precipitated copper that had not been subjected to alkali treatment was repulped in 0.25 L of 80 g / L sulfuric acid, and allowed to stand at 60 ° C. for 4 hours with stirring. Thereafter, solid-liquid separation was performed, and the leaching rate was calculated. As a result, the result was as follows.
Compared with the leaching rate of copper of 85% or more shown in Table 1, the value was much worse than 8.2%, and efficient separation and recovery of copper and bismuth was impossible.
[Table 13]
【The invention's effect】
As described above, according to the present invention, it has become possible to separate and recover bismuth, copper, and the like, which are valuable resources, from electrolytically precipitated copper.
[Brief description of the drawings]
FIG. 1 shows one embodiment of the processing flow of the present invention.
Claims (4)
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| JP2000217196A JP3548097B2 (en) | 2000-07-18 | 2000-07-18 | Separation and recovery method of bismuth and copper etc. from treatment object containing cuprous oxide and bismuth |
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| JP2000217196A JP3548097B2 (en) | 2000-07-18 | 2000-07-18 | Separation and recovery method of bismuth and copper etc. from treatment object containing cuprous oxide and bismuth |
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| US20050193863A1 (en) * | 2004-03-05 | 2005-09-08 | Muinonen Mika E.S. | Selective reduction of cupriferous calcine |
| CN101775619B (en) * | 2010-03-26 | 2011-11-23 | 中南大学 | Clean metallurgical method for bismuth or antimony by wet process |
| CN102102154A (en) * | 2010-12-22 | 2011-06-22 | 中南大学 | Low-temperature fused salt clean smelting method for tin |
| CN102952941B (en) * | 2012-04-01 | 2016-02-24 | 东北大学 | A kind of method utilizing copper oxide ore |
| CN102732720B (en) * | 2012-04-01 | 2016-02-24 | 东北大学 | A kind of method processing copper oxide ore |
| CN105350026B (en) * | 2015-11-17 | 2018-02-23 | 郴州市金贵银业股份有限公司 | The method that metal is reclaimed from bismuth slag |
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