JP2017066520A - Method for refining bismuth - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a method for refining bismuth of recovering bismuth from a solution obtained after recovering noble metals from a copper electrolytic slime.SOLUTION: There is provided a method for refining bismuth which comprises: 1) a neutralization treatment step of adding alkali to an acidic solution to adjust the pH in the range of 2.0 or more and 3.0 or less, followed by solid-liquid separation to obtain a neutralized filtrate and a neutralized precipitate; 2) an alkali leaching step of adding alkali to the neutralized precipitate obtained in the neutralization treatment step to separate into an alkali leachate and an alkali-leached residue; 3) a sulfuric acid leaching step of adding sulfuric acid to the alkali-leached residue to separate into a sulfuric acid leachate and a sulfuric acid-leached residue; 4) a cooling step of cooling the sulfuric acid leachate obtained in the sulfuric acid leaching step to obtain crystals of bismuth sulfate; 5) a bismuth oxidation step of adding alkali to the crystals of bismuth sulfate obtained in the cooling step to obtain bismuth oxide; and 6) an electrolysis step of electrowinning a dissolving liquid obtained by adding and dissolving an acid solution to the bismuth oxide obtained in the bismuth oxidation step to obtain metallic bismuth.SELECTED DRAWING: Figure 1

Description

  The present invention relates to a method for purifying bismuth. More specifically, the present invention relates to a purification method for recovering bismuth, which is a valuable metal, from copper electrolytic slime generated in the copper electrolytic purification process.

  As a method of recovering copper from ores containing copper, copper concentrates are obtained by subjecting copper-containing ores to a beneficiation process to obtain copper concentrate, and then the copper concentrate is put into a furnace and melted at a high temperature. It is subjected to dry smelting to obtain crude copper, and then this crude copper is immersed in a sulfuric acid acidic solution as an anode, and at the same time, a current is passed between the cathode using a stainless steel plate or a copper plate immersed in the anode. In general, a method for obtaining high-purity electrolytic copper has been generally used by subjecting copper dissolved in the copper to electrolytic purification in which the copper is selectively deposited on the cathode.

  In addition to the target copper, the above ores containing copper contain a wide variety of components that are valuable and impurities such as precious metals such as gold and silver, bismuth, arsenic, antimony, selenium, lead, iron, tellurium, etc. Often done. These components are separated from copper by the above-described dry smelting, or separated from copper by electrolytic refining, such as being deposited as a copper electrolytic slime along with the precious metal at the bottom of the electrolytic cell.

  Since the copper electrolytic slime contains various components as described above, it is necessary to purify the slime and recover the target valuable material.

  Several methods are known as methods for purifying slime, and one of them is the removal of copper by adding sulfuric acid to copper electrolytic slime to dissolve and remove copper mixed in copper electrolytic slime. Then, the copper removal slime obtained by copper removal is put in a furnace and heated to high temperature, selenium and antimony are volatilized and separated, then oxidized to separate lead as an oxide, and then There is a method of separating noble metal and bismuth.

  The above method is a suitable method for handling a large amount of material, but on the other hand, a large facility is required, the energy cost required for processing is high, and precious metals can be recovered in the latter half of the process. There were issues such as an in-progress interest rate.

  Therefore, in recent years, new treatment processes centered on wet methods have been widely put into practical use. These wet treatment processes are roughly classified into the following two methods depending on whether a wet reduction method or a roasting method is adopted for selenium separation.

The first method is a method disclosed in Non-Patent Document 1, Patent Document 1, or Patent Document 2.
In these methods, sulfuric acid and oxygen are added to copper electrolytic slime, and a portion of tellurium and copper are leached under high temperature and pressure. Next, hydrochloric acid and hydrogen peroxide or chlorine are added to the leaching residue to leach gold, platinum group elements, selenium and tellurium.
Next, bis (2-butoxyethyl) ether (hereinafter referred to as DBC), which is an organic extractant, is mixed with this leachate to extract gold into the extractant, and the extract is reduced with sulfur dioxide. Collect selenium, tellurium and platinum group elements. A mixture of selenium, tellurium, and platinum group elements is separated into selenium, tellurium, and platinum group elements by distillation in a metal state. The chlorine leaching residue is leached with silver by treating with ammonia water, and silver is recovered as a powder from the leaching solution.

  The second method is a method shown in Non-Patent Document 2. In other words, the process until the copper electrolysis slime is subjected to pressure leaching with sulfuric acid to remove copper and tellurium is the same as the first method above, but the residue is then mixed with sulfuric acid and roasted. At the same time, selenium is volatilized and the silver in the residue is converted to silver sulfate. The sulfuric acid roasting residue first leaches silver using an aqueous calcium nitrate solution, and recovers silver metal by electrolyzing the leaching solution.

  The residue leached from silver leaches gold, platinum group, selenium, and remaining tellurium with hydrochloric acid and chlorine. This leachate is mixed with DBC to extract gold, but the principle is the same as in the first method. Further, the extracted residue is hydrazine reduced to recover platinum group elements and tellurium as metal powder.

  In addition, as a method for recovering silver from the sulfuric acid roasting residue in the second method, a method using ammonia and a method using sodium sulfite have been proposed as in the first method.

  However, in the above two methods, as a method for separating some valuables and impurities, for example, bismuth is not shown to be recovered in a wet process. Generally, bismuth is melted using a conventional dry process and recovered from slag. However, in order to realize the dry process, there are problems such as an investment for providing a furnace, an investment such as energy to be used, and a cost, which are not preferable.

JP-A-9-316559 JP-A-9-316561

K. E. Sutliff et al, JOM, August (1996), pp42-44, J. E. Hoffmann et al, Proceedings of COPPER 95-COBRE 95 International Conference Volume III (1995), The Metallurgical Society of CIM, pp41-57 J. E. Hoffmann et al, HY DROMETALLURGY '94, the Institutionof Mining and Metallurgy and the Society of Chemical Industry, CHAPMAN & HALL (1994), pp69-105

  An object of the present invention is to provide a method for efficiently recovering and purifying bismuth from a liquid obtained after recovering a noble metal from copper electrolytic slime, mainly using a wet process and using a furnace as much as possible.

The first invention is based on an electrolytic slime produced by subjecting crude copper obtained by smelting a mineral containing copper, noble metal, bismuth and impurities to electrolytic purification to recover copper, and then performing electrolytic purification. In the step of recovering a noble metal by a wet method, an acidic solution produced after recovering the noble metal is subjected to the following step, which is a bismuth purification method.
1) Neutralization step of adding an alkali to the acidic solution to adjust the pH to a range of 2.0 to 3.0, and then solid-liquid separation to obtain a neutralized filtrate and a neutralized starch 2) Alkaline leaching step of adding alkali to neutralized starch to separate into alkali leaching solution and alkali leaching residue 3) Sulfuric acid leaching step of adding sulfuric acid to said alkali leaching residue to separate into sulfuric acid leaching solution and sulfuric acid leaching residue 4) Cooling step of cooling the sulfuric acid leachate to obtain bismuth sulfate crystals 5) Bismuth oxidation step of adding alkali to the bismuth sulfate crystals to obtain bismuth oxide 6) Obtaining and dissolving the acid solution in the bismuth oxide Electrolytic process to obtain metal bismuth by electrolyzing the solution

A second invention is the method for purifying bismuth according to the first invention, wherein the impurity is one or more of copper, iron, lead, arsenic, and tellurium.
A third invention is a method for purifying bismuth according to the first invention, wherein the alkali leaching solution obtained in the alkali leaching step is heated to 90 ° C. or higher and then cooled to obtain crystals containing arsenic.
In the fourth invention, the sulfuric acid leaching step in the first invention is performed by first contacting the low-concentration sulfuric acid to leaching the leaching residue to separate the primary leaching solution from the primary leaching residue, and then to the primary leaching residue. It consists of a two-stage leaching process in which a high concentration sulfuric acid is contacted to separate into a secondary leaching solution and a secondary leaching residue, and the obtained secondary leaching solution is supplied to the cooling process of the first invention. This is a purification method of bismuth.
The fifth invention is a method for purifying bismuth, characterized in that the acid solution used in the electrolysis step in the first invention is a solution containing hydrofluoric acid.
The sixth invention uses a sodium hydroxide solution having a concentration of 1 mol / l or more and 5 mol / l or less as an alkali to be added to the neutralized starch in the alkali leaching step of the first invention, and a slurry concentration of 10 g / l or more and 100 g. This is a method for purifying bismuth, characterized in that an alkali leaching solution and an alkali leaching residue are obtained by mixing and dissolving so as to be in a range of 1 / l or less.
The seventh invention is the sulfuric acid leaching step of the first invention, wherein the pH of the slurry after adding sulfuric acid is adjusted to a range of 0 or more and 3.5 or less and leached. A method for purifying bismuth characterized in that a sulfuric acid leaching residue is obtained.

According to the first invention, in the neutralization treatment step, since the pH is 2 to 3, impurities can be separated in the form of hydroxide, the concentration of bismuth can be maximized, and bismuth is contained by solid-liquid separation. It can be separated into Japanese starch and neutralized filtrate. In the alkali leaching step, the alkali leaching residue in which bismuth remains and the alkali leaching solution can be separated. In the sulfuric acid leaching step, it can be separated into a sulfuric acid leaching solution containing bismuth and a sulfuric acid leaching residue. Crystals of bismuth sulfate can be obtained in the cooling step, and bismuth oxide can be obtained in the bismuth oxidation step. In the electrolysis step, a solution obtained by adding an acid solution to bismuth oxide can be electrolytically collected to finally obtain electrodeposited metal bismuth.
As described above, according to the present invention, high-purity metal bismuth can be recovered from a copper smelting process by a wet process, and since it does not require large-scale equipment necessary for a dry process, it can be operated at a low cost.

According to the second invention, if the impurity is one or more of copper, iron, lead, arsenic, and tellurium, the behavior with bismuth in neutralization and electrolytic refining is somewhat different, so the method of the present invention is used. Can be separated efficiently and bismuth can be concentrated as much, so that it does not interfere with bismuth recovery.
According to the third invention, the alkali leaching solution is heated to 90 ° C. or higher and then cooled to obtain crystals containing arsenic, whereby arsenic can be selectively separated and arsenic can be easily reused.
According to the fourth aspect of the invention, when a two-step process is performed in which a secondary process using a high concentration of sulfuric acid is performed after a primary process using a low concentration of sulfuric acid, the solubility of bismuth increases and the concentration becomes easier. .
According to the fifth aspect of the invention, since the electrolytic solution containing bismuth fluorofluoride is used, high-purity metal bismuth in which impurities are sufficiently separated can be obtained.
According to the alkali concentration and the slurry concentration of the sixth invention, it is possible to improve the separation rate when separating arsenic, and to improve the efficiency such as prevention of a decrease in filterability during solid-liquid separation.
According to the seventh aspect of the present invention, it is possible to reduce a loss in which bismuth cannot be recovered by electrolytic collection.

It is process drawing of the bismuth refinement | purification method which concerns on this invention. It is explanatory drawing of the product obtained at each process of the bismuth refinement | purification method of FIG.

The bismuth purification method using the wet method according to the present invention will be described below.
The present invention is a method of subjecting crude copper obtained by smelting a mineral containing copper, a noble metal, bismuth and impurities to electrolytic purification to recover copper, and then wet from electrolytic slime produced by electrolytic purification. In the step of recovering the noble metal by the method, the acidic solution produced after recovering the noble metal is subjected to the following step.

FIG. 1 shows each step of bismuth purification, and FIG. 2 is an explanatory diagram of a product obtained in each step shown in FIG. The following symbols 1) to 6) correspond to those in the figure.
1) Neutralization treatment step An alkali is added to the acidic solution produced after the precious metal is recovered to adjust the pH to a range of 2.0 or more and 3.0 or less, followed by solid-liquid separation and neutralization filtrate and neutralization starch. Get things.
2) Alkaline leaching step An alkali is added to the neutralized starch obtained in the neutralization treatment step to separate into an alkaline leaching solution and an alkaline leaching residue.
3) Sulfuric acid leaching step Sulfuric acid is added to the alkali leaching residue obtained in the alkali leaching step to separate into a sulfuric acid leaching solution and a sulfuric acid leaching residue.
4) Cooling step The sulfuric acid leaching solution obtained in the sulfuric acid leaching step is cooled to obtain bismuth sulfate crystals.
5) Bismuth oxidation step An alkali is added to the bismuth sulfate crystals obtained in the cooling step to obtain bismuth oxide.
6) Electrolysis step An acid solution is added to and dissolved in the bismuth oxide obtained in the bismuth oxidation step, and the resulting solution is electrolyzed to obtain metal bismuth.

  In the mineral to which the present invention is applied, the impurities include one or more of iron, lead, arsenic, and tellurium. If these impurities are used, the behavior with bismuth in neutralization, electrolytic purification, etc. is somewhat different, so that the method of the present invention can be used for efficient separation, and bismuth can be concentrated accordingly. Therefore, there is no hindrance to bismuth recovery. On the other hand, if impurities such as antimony other than the above are contained in a high concentration, the behavior with bismuth is similar, and therefore, it becomes difficult to concentrate efficiently.

Hereafter, each process of this invention is demonstrated in detail.
1). Neutralization step An alkaline solution is added to the acidic solution after the noble metal is recovered from the electrolytic slime by the wet method to neutralize the acidic solution.
When the neutralization treatment is performed, the product is separated into a neutralized filtrate that forms a neutralized starch such as a hydroxide according to each element and a neutralized filtrate that dissolves without forming from the relationship between the solubility product and pH. Therefore, it can isolate | separate into a neutralization filtrate and a neutralization starch by adjusting pH finely.

  In the alkali leaching step and the sulfuric acid leaching step, which are the subsequent steps of the present invention, it is difficult to effectively separate antimony and iron contained as impurities from bismuth. For this reason, it is important to sufficiently separate antimony and iron in advance in the neutralization step.

In this neutralization step, an acidic solution containing impurities such as iron, lead, arsenic, tellurium, antimony, nickel ions in addition to copper, noble metals and bismuth is first adjusted to a pH of 2.0 to 3.0 using an alkali. Adjust to the range, then solid-liquid separate into neutralized filtrate and neutralized starch. If the pH is less than 2.0, the separation efficiency of bismuth is weak, and if the pH is more than 3.0, copper, antimony, arsenic, nickel, etc. start to precipitate simultaneously with bismuth. Absent. When the pH is in the range of 2.0 to 3.0, only bismuth can be separated at a high concentration.
It is optimal in terms of handling that impurities such as iron and antimony are separated in the form of hydroxide, and the pH is in the range of 2.0 to 3.0, preferably 2.4 to 2.8. By controlling it, the bismuth concentration can be maximized.

  For solid-liquid separation, known methods such as Nutsche and filter bottles, centrifuges, filter presses, Denver filters and the like can be used, which can be divided into neutralized filtrates and starches.

2). Alkali leaching process Some elements dissolve on the acid side or the alkali side. In the present invention, the alkali leaching solution and the alkali leaching residue are separated by adding an alkali. When an alkali is added to the neutralized starch, a phenomenon occurs in which an element that dissolves even in an alkaline state, such as an amphoteric compound such as arsenic, is dissolved, and can be divided into an alkaline leaching solution and an alkaline leaching residue.

  Considering the study of leaching using sulfuric acid in the subsequent process, the ratio of iron, lead, and arsenic produced in the neutralization process and distributed to the residue needs to be suppressed to 50% or less. Become.

  As the alkali to be added, slaked lime or sodium hydroxide can be used. As the addition method, a method of mixing slaked lime with water to form a slurry, or adding a solution of sodium hydroxide dissolved in water using a metering pump can be used. When slaked lime is used, calcium sulfate (gypsum) may be generated and become an impurity with respect to the recovered bismuth. Therefore, it is preferable to use sodium hydroxide in which the product after neutralization is water-soluble.

  In an example of the alkaline leaching step, arsenic contained in the neutralized starch is leached into an alkaline leaching solution using sodium hydroxide. The leached arsenic can be separated through a boiling step in which the alkaline leaching solution is heated to 90 ° C. or higher and then cooled to obtain crystals containing arsenic. That is, arsenic is selectively separated by utilizing the change in the crystal structure of arsenic at a high temperature. Through this boiling step, there is an advantage that arsenic can be easily reused.

  In order to remove more arsenic, a solution of sodium hydroxide may be added to the neutralized starch and reacted as a slurry. The concentration of sodium hydroxide and the slurry concentration at the start of the reaction may be adjusted according to the amount of arsenic contained in the neutralized starch.

Specifically, it is preferable to use a sodium hydroxide solution having a concentration of 1 to 5 mol / l and add the slurry concentration to 10 to 100 g / l. The sodium hydroxide concentration is more preferably about 2 mol / l.
The reaction temperature is suitably around 60 ° C., and if it is lower, the reaction will be slow. On the other hand, even if the temperature is higher than 60 ° C., the reaction is not excessively promoted, and the energy cost is excessive.

When the concentration of sodium hydroxide is lower than 1 mol / l, arsenic cannot be completely removed, and there is a disadvantage that a part remains in the neutralized starch.
In addition, when the concentration of sodium hydroxide is excessively high such as exceeding 5 mol / l, impurities such as antimony and iron other than arsenic are also leached. In this case, although there is a merit that the purity of bismuth remaining in the alkali leaching residue is increased, the amount of sodium hydroxide used increases, so the cost increases, and even a part of bismuth is leached into the alkali leaching solution and lost. There is a problem such as an increase in the number and is not preferable.

  If the slurry concentration is lower than 10 g / l, the equivalent of the neutralized starch to the alkaline solution is too small, and there is a disadvantage that the amount of bismuth dissolved relatively increases and the loss increases, and is higher than 100 g / l. Since there are too many equivalents of neutralized starch with respect to the alkaline solution, arsenic cannot be sufficiently dissolved and removed, and as a result, the effect of removing arsenic is reduced. On the other hand, when the slurry concentration is 10 g / l or more and 100 g / l or less, there is an advantage that arsenic can be efficiently removed while suppressing loss of bismuth.

  In addition, for example, when the neutralized starch contains chloride (Cl) ions derived from the raw material and its processing step, bismuth has high solubility in sulfuric acid such as oxychlorobismuth (BiClO). It exists as a compound and may inhibit the precipitation of bismuth sulfate in the cooling step described later. However, by using the alkaline leaching of the present invention, the quality of chloride ions in the alkaline leaching residue can be suppressed to 0.1% or less, and as a result, the effect of reducing the loss of bismuth in the cooling process described later. There is also.

  If the concentration of arsenic in the alkaline leachate is too high, crystals of sodium dihydrogen arsenate may be generated in the leachate, and the filterability deteriorates with the generation, or the generated crystals are dissolved and removed. It is not preferable that the cleaning load to be performed is increased.

  Arsenic and bismuth in the residue obtained in the alkali leaching step are leached so that the molar ratio (As / Bi) is 0.1 or less. By leaching so as to have this ratio, 90% or more of bismuth can be recovered in a sulfuric acid leaching process described later.

3). Sulfuric acid leaching step Sulfuric acid is added to the alkaline leaching residue obtained in the above alkaline leaching step, and the sulfuric acid leaching solution and the sulfuric acid leaching residue are separated by utilizing the difference in solubility depending on the sulfuric acid concentration.

  In addition, when chloride ions are contained as described above, a washing step (pH adjustment step) for washing the alkaline leaching residue with water is provided between the alkali leaching step and the sulfuric acid leaching step to reduce the residual chloride product level. Further reduction processing may be performed. In the washing step, water is added to the alkali leaching residue to form a slurry, and washing is performed until the pH is 2.5 to 3.5, preferably about 3, so that the dispersibility of the bismuth component in the neutralized starch is increased. It improves and becomes easy to leach into sulfuric acid.

  In the sulfuric acid leaching step, it is preferable to perform a two-stage leaching process by changing the sulfuric acid concentration. That is, firstly, a primary treatment is performed in which low concentration sulfuric acid is contacted to leach the leaching residue and separate into a primary leaching solution and a primary leaching residue, and then high concentration sulfuric acid is applied to the primary leaching residue. It is preferable to perform a secondary treatment in which contact is made to separate the secondary leaching solution and the secondary leaching residue.

  Moreover, it is preferable to supply the above-mentioned secondary leaching solution to the cooling step. By performing such a two-stage leaching process, the solubility of bismuth increases and it becomes easy to concentrate.

  In the present invention, low-concentration sulfuric acid refers to a weakly acidic sulfuric acid solution in which the pH of the solution is in the range of 0 to 3.5, preferably around pH 3, and high-concentration sulfuric acid refers to a pH of less than 0. This is a sulfuric acid solution having a strongly acidic concentration. Specifically, the concentration is 7 mol / l or more, preferably about 10 mol / l. At the time of leaching with the above-described high-concentration sulfuric acid, the temperature of the slurry is preferably in the range of 30 to 90 ° C.

  Specifically, sulfuric acid is added to the alkali leaching residue to make a slurry adjusted to a pH of 0 to 3.5, and copper and iron are leached. In the sulfuric acid leaching step of pH 0 to 1, for example, among the copper contained in the alkaline leaching residue, the distribution (leaching rate) of copper to the sulfuric acid leaching solution is preferably 50% or more. If the distribution is less than 50%, copper removal is insufficient and the copper quality in the bismuth product is adversely affected.

  The distribution (leaching rate) of the bismuth contained in the alkaline leaching residue into the sulfuric acid leaching solution needs to be 2% or less. If the distribution exceeds 2%, the loss of bismuth in the entire process cannot be ignored.

4). Cooling step The sulfuric acid leaching solution obtained in the sulfuric acid leaching step is cooled to crystallize bismuth sulfate crystals. This cooling step uses a difference in solubility. Generally, the solubility is lowered as the temperature is lowered, so that it cannot be completely dissolved by the liquid. Therefore, bismuth sulfate crystals can be obtained by cooling.

For the cooling method, for example, a jacket is provided outside the reaction tank (cooling tank) filled with the sulfuric acid leachate, or a serpentine tube is installed in the reaction tank. This can be done by flowing a coolant such as water. Note that bismuth sulfate crystals obtained in advance during cooling may be added as seeds to the leachate.
Cooling is preferably performed to a low temperature, but considering the cost and efficiency required for cooling, it is preferable to cool to a room temperature of less than 30 ° C. The time required for cooling is preferably about 1 hour.

5). Bismuth oxidation step An alkali is added to the crystals of bismuth sulfate obtained in the cooling step. When alkali is added, other than bismuth is dissolved, so that bismuth oxide can be obtained.
Specifically, for example, a sodium hydroxide solution having a concentration of about 1 to 2 mol / l is mixed with the above bismuth sulfate crystals so that the slurry concentration is about 25 g / l, and the temperature is maintained at about 60 ° C. When stirred for about 1 hour, bismuth hydroxide (Bi (OH) ₃ ) is obtained, and when dried, bismuth oxide (Bi ₂ O ₃ ) is obtained.

6). Electrolysis step An acid solution is added to and dissolved in the bismuth oxide obtained in the bismuth oxidation step. When an acid solution is added in this manner, bismuth dissolves as ions. However, when the obtained solution is electrolyzed, that is, when an electrode is placed in the solution and energized, the bismuth ions receive electrons and form a single metal bismuth on the cathode. Electrodeposit as

  Hydrochloric acid or the like can be used for the acid solution used for the electrolysis. However, since the solubility of bismuth is sufficiently high and a bismuth concentration favorable for electrolysis can be secured and the separability from coexisting impurities is high, the hydrofluoric acid solution is used. preferable. By using an electrolytic bath using a solution containing 硅 hydrofluoric acid, metal bismuth in which impurities are sufficiently separated from the electrolyte present in the form of bismuth fluorinated fluoride can be obtained.

Specific electrolysis conditions for obtaining metal bismuth include, for example, dissolving bismuth oxide using a solution having a hydrofluoric acid concentration of 300 to 350 g / l to obtain an electrolytic starting solution having a bismuth concentration of 80 to 100 g / l. This electrolytic starting solution is supplied to an electrolytic cell using Hastelloy for the cathode and carbon for the anode, and the cathode current density of 80 to 120 A / m ² is maintained while maintaining the liquid temperature at 40 to 50 ° C., preferably 50 ° C. or less. By energizing at, metal bismuth can be electrodeposited on the cathode. If the current density exceeds 200 A / m ² , the state of the electrodeposition surface becomes rough and precipitates on the grains are likely to be formed, which is undesirable.
When the electrolysis is finished, for example, when the bismuth concentration in the electrolytic solution is reduced to about 20 to 30 g / l, the deterioration of the surface state of the deposited bismuth can be suppressed, and the surface smoothness without influence of the electrolytic solution is suppressed. Bismuth metal can be obtained and is preferable.

  In addition, when bismuth metal is added to the electrolytic starting solution and immersed in a cementation reaction in which silver ions contained in the electrolytic starting solution are deposited on bismuth metal, the solution is subjected to electrolysis. It is preferable because the quality can be reduced. The cementation reaction should be carried out by adding bismuth metal so that the oxidation-reduction potential (ORP) of the electrolytic starting solution is reduced to a value in the range of 400 to 518 mV or less with a silver / silver chloride electrode as a reference electrode. Is good.

  After the electrolysis is finished, the cathode is pulled up, the electrodeposited bismuth is peeled off, washed with water, then placed in a furnace, and the temperature is about 300 ° C., slightly higher than the melting point of bismuth (271 ° C.) in an inert atmosphere. By melting with, impurities and oxides can be removed and bismuth metal having a shape such as an ingot can be obtained.

Example 1
An anode obtained by casting copper concentrate in a furnace and melting crude copper separated from impurities by high temperature immersion is immersed in an electrolytic cell filled with a sulfuric acid solution, and at the same time, the copper or A copper electrolytic slime containing a noble metal such as gold or silver is obtained by using a known copper electrolytic purification method in which a current is passed between a cathode made of stainless steel and electrolytic copper is electrodeposited on the cathode surface. An acidic solution containing a noble metal leached from the copper electrolytic slime was prepared by allowing an oxidizing agent such as chlorine gas to act on the electrolytic slime using a known method.

  Next, sodium hydroxide was added to this acidic solution at room temperature to obtain a slurry adjusted to pH 2.6. Next, this slurry was subjected to solid-liquid separation into a neutralized starch and a neutralized filtrate using 5C filter paper using a Nutsche and a filter bottle (neutralization treatment step). When the proportion of each component of bismuth, iron, lead, and arsenic contained in the original solution was distributed to the neutralized starch, bismuth; 90%, iron; 40%, lead; 40%, arsenic; 40%, More than half of the components other than bismuth could be separated.

(Example 2)
Using an acidic solution obtained by leaching a noble metal from a copper electrolytic slime containing the same noble metal as in Example 1 above, adding sodium hydroxide solution to adjust the pH to 2.6, and neutralizing in the same manner as in Example 1 A starch and a neutralized filtrate were obtained (neutralization treatment step).

Next, sodium hydroxide having a concentration of 2 mol / l was added to the neutralized starch and leached to obtain an alkali leaching residue (alkali leaching step). A lower concentration of sulfuric acid was added to the obtained alkali leaching residue to adjust the slurry concentration to 100 g / l and stirred for 1 hour to obtain a sulfuric acid leaching solution (sulfuric acid leaching step). The pH of the slurry after addition of sulfuric acid was adjusted to 0.8.
The leaching rate of copper in the sulfuric acid leaching solution was 53%. On the other hand, the leaching of bismuth was suppressed to 0.7%, and the target was achieved.

To the obtained residue, 10 mol / L sulfuric acid was added to form a slurry, and the temperature was maintained at 60 ° C. to leach Bi in the residue.
After separating the residue, the leachate was cooled to room temperature to obtain bismuth sulfate crystals (cooling step). The obtained crystals were added to a caustic soda solution having a pH of 14 and stirred to obtain bismuth oxide crystals. The obtained crystals are dissolved in a hydrofluoric acid solution having a concentration of 336 g / l to adjust the bismuth concentration to 100 g / l, and separately prepared bismuth metal is immersed in this solution to dissolve by a cementation reaction. A solution obtained by desilvering the silver concentration of the solution from 13 mg / l to less than 5 mg / l, which is the lower limit of analysis, was used as an electrolytic starting solution (bismuth oxidation step).

Next, this electrolytic starting solution was put in an electrolytic cell, and the solution temperature was maintained at 45 to 50 ° C. In the electrolytic cell, a Hastelloy cathode and a carbon anode were arranged so that the distance between the surfaces was 50 mm. Next, current was supplied at a cathode current density of 100 A / m ² while circulating the electrolytic solution discharged from the electrolytic cell by supplying the electrolytic solution again to the electrolytic cell using a pump (electrolytic process). The bismuth concentration of the electrolyte discharged from the electrolytic cell was analyzed, and when the bismuth concentration dropped to 25 g / l or less, the energization was stopped.
Next, the cathode was lifted, and the electrodeposited bismuth metal was peeled off from the cathode, and the bismuth metal was washed with water and dried.
The current efficiency obtained by dividing the amount of the obtained bismuth metal by the theoretical electrodeposition amount calculated from the amount of energized current was 99.6%.

  Next, the obtained bismuth metal was analyzed using GDMS (glow discharge mass spectrometer). As a result, silver, the main impurity, is about 70 ppm, which can be significantly reduced compared to 1300 ppm when the cementite reaction is not performed, and a high-purity bismuth metal having a bismuth quality of 99.993% is obtained. It was.

  Moreover, when the leaching solution and the washing solution obtained in the alkali leaching step were boiled to a temperature of 90 ° C., crystals of sodium dihydrogen arsenate were obtained, and arsenic was separated and recovered as a solid by filtration.

(Example 3)
Using the same acidic solution as in Examples 1 and 2 above, sodium hydroxide was added to this acidic solution at room temperature to obtain a slurry adjusted to pH 2.6, and then the same method as in Examples 1 and 2 was used. The solid was separated into a neutralized starch and a neutralized filtrate (neutralization treatment step). The bismuth grade contained in the neutralized starch was 19% by weight, and the grade of chloride ions was 11% by weight.

  Next, a sodium hydroxide solution having a concentration of 2 mol / l was added to the neutralized starch to make the slurry concentration 100 g / l, and the slurry was stirred for 1 hour while maintaining the temperature of the slurry at 60 ° C. (alkali leaching step). Next, the slurry after the completion of stirring was subjected to solid-liquid separation, the obtained alkaline leaching residue was washed with water, and the washed alkaline leaching residue obtained by solid-liquid separation again was analyzed. As a result, the bismuth grade was 28.1% by weight, and the chloride ion grade was 0.01% by weight, which significantly reduced chloride.

  Next, the alkaline leaching residue after washing was treated in the same manner as in Example 2 above, and leached with sulfuric acid having a concentration of 10 mol / l to obtain a leachate having a bismuth concentration of 3.7 g / l. After cooling to room temperature (25 ° C.) and solid-liquid separation, a filtrate having a bismuth concentration of 1.0 g / l was obtained, and 73% of the bismuth contained in the leachate could be recovered.

Example 4
An alkaline leaching residue was obtained by the same method as in Example 3 above, and a leaching solution in which bismuth was leached by adding sulfuric acid having a concentration of 8 mol / l to the alkaline leaching residue was obtained. Next, when the obtained leachate was cooled by the same method as in Example 3, 80% of the bismuth contained in the leachate could be recovered.

(Example 5)
An alkali leaching residue was obtained in the same manner as in Example 2 above, and sulfuric acid and water were added to the alkali leaching residue so that the slurry concentration was 100 g / l to adjust the pH to 3.0, and stirring was continued for 1 hour. did. After solid-liquid separation, sulfuric acid and water having a concentration of 10 mol / l were added to the obtained residue to form a slurry, which was leached for 2 hours while maintaining at 60 ° C. It was confirmed that the obtained leaching solution was sufficiently leached with a bismuth concentration of 3.0 g / l.

(Comparative Example 1)
Except for adjusting the pH to 3.8, the same apparatus and the same acidic solution as in Example 1 were used to neutralize in the same manner. The proportion of bismuth distributed to the neutralized starch was as good as 95%, but iron: 80%, lead: 60%, arsenic 40%, and a bismuth grade of only about 52% was obtained.

(Comparative Example 2)
When the neutralized starch prepared in the same manner as in Example 2 was subjected to sulfuric acid leaching under the same conditions as in Example 1 without leaching with alkali, the bismuth leaching rate was 60%. The bismuth concentration in the leachate was 4.0 g / l. However, the leaching residue was again leached with sulfuric acid under the same conditions, but bismuth hardly leached. Further, even when the leachate was cooled, bismuth sulfate crystals could hardly be obtained.

(Comparative Example 3)
Except that the neutralized starch prepared in the same manner as in Example 2 was adjusted to pH 3.5 with sodium hydroxide and alkali leached, and the sulfuric acid solution was added to adjust the pH to 1.2. Treated in the same manner as Example 2. The distribution of bismuth into the liquid was a sufficient range of 1.5%, but the distribution (leaching rate) of copper was insufficient at 45%.

(Comparative Example 4)
The neutralized starch prepared in the same manner as in Example 2 above was adjusted to 3.5 with sodium hydroxide, and alkaline leaching was performed, except that high-concentration sulfuric acid with a pH of less than 0 was used. Treated in the same manner as Example 2. As a result, the dissolution of copper into the solution was satisfactory at 55%, but 3% of bismuth was leached, and the target bismuth leaching rate could not be suppressed.

(Reference Example 1)
An alkali leaching residue was obtained by the same method as in Example 4 above, and a leaching solution was obtained in which bismuth was leached by adding sulfuric acid having a concentration of 6 mol / l to the alkali leaching residue. Subsequently, when the obtained leachate was cooled by the same method as in Example 4, only 45% of the bismuth contained in the leachate could be recovered.

(Reference Example 2)
An alkali leaching residue was obtained in the same manner as in Example 5 above, and sulfuric acid and water having a concentration of 10 mol / l were added to the alkali leaching residue without adjusting the pH to form a slurry, which was leached for 2 hours while maintaining at 60 ° C. The obtained leaching solution had a bismuth concentration of 1.2 g / l, which was insufficient leaching.

(Reference Example 3)
An alkali leaching residue was obtained in the same manner as in Example 5, and sulfuric acid and water were added to the alkali leaching residue so that the slurry concentration was 100 g / l to adjust the pH to 5 and stirring was continued for 1 hour. After solid-liquid separation, sulfuric acid and water having a concentration of 10 mol / l were added to the obtained residue to form a slurry, which was leached for 2 hours while maintaining at 60 ° C. The obtained leaching solution had a bismuth concentration of 2.5 g / l, which was insufficient.

(Reference Example 4)
An alkali leaching residue was obtained in the same manner as in Example 5, and sulfuric acid and water were added to the alkali leaching residue so that the slurry concentration would be 100 g / l to adjust to pH 0, and stirring was continued for 1 hour. After solid-liquid separation, sulfuric acid and water having a concentration of 10 mol / l were added to the obtained residue to form a slurry, which was leached for 2 hours while maintaining at 60 ° C. The obtained leaching solution had a bismuth concentration of 2.5 g / l, which was insufficient.

DESCRIPTION OF SYMBOLS 1 Neutralization process 2 Alkali leaching process 3 Sulfuric acid leaching process 4 Cooling process 5 Bismuth oxidation process 6 Electrolytic process

Claims (7)

Crude copper obtained by smelting a mineral containing copper, noble metal, bismuth and impurities is subjected to electrolytic purification to recover copper, and then the noble metal is obtained from the electrolytic slime produced by electrolytic purification by a wet method. A method for purifying bismuth, characterized in that, in the step of recovering, an acidic solution produced after recovering the precious metal is subjected to the following step.
1) Neutralization step of adding an alkali to the acidic solution to adjust the pH to a range of 2.0 to 3.0, and then solid-liquid separation to obtain a neutralized filtrate and a neutralized starch 2) Alkaline leaching step of adding alkali to neutralized starch to separate into alkali leaching solution and alkali leaching residue 3) Sulfuric acid leaching step of adding sulfuric acid to said alkali leaching residue to separate into sulfuric acid leaching solution and sulfuric acid leaching residue 4) Cooling step of cooling the sulfuric acid leachate to obtain bismuth sulfate crystals 5) Bismuth oxidation step of adding alkali to the bismuth sulfate crystals to obtain bismuth oxide 6) Obtaining and dissolving the acid solution in the bismuth oxide Electrolytic process to obtain metal bismuth by electrolyzing the solution 2. The method for purifying bismuth according to claim 1, wherein the impurity is one or more of copper, iron, lead, arsenic, and tellurium. The method for purifying bismuth according to claim 1, further comprising a boiling step of heating the alkali leaching solution obtained in the alkali leaching step to 90 ° C or higher and then cooling to obtain crystals containing arsenic. In the sulfuric acid leaching step, low concentration sulfuric acid is first contacted to leached the leaching residue to separate the primary leaching solution and the primary leaching residue, and then the primary leaching residue is contacted with high concentration sulfuric acid. 2. The method for purifying bismuth according to claim 1, wherein the secondary leaching liquid is separated into a secondary leaching liquid and a secondary leaching residue, and the obtained secondary leaching liquid is supplied to the cooling step. The method for purifying bismuth according to claim 1, wherein the acid solution used in the electrolysis step is a solution containing hydrofluoric acid. In the alkali leaching step, the alkali added to the neutralized starch is a sodium hydroxide solution having a concentration of 1 mol / l or more and 5 mol / l mol or less, and the slurry concentration is 10 g / l or more using the sodium hydroxide solution. 2. The method for purifying bismuth according to claim 1, wherein the alkali leaching solution and the alkali leaching residue are obtained by mixing and dissolving in a range of 100 g / l or less. 2. The sulfuric acid leaching step and the sulfuric acid leaching residue are obtained by adjusting the pH of the slurry after adding sulfuric acid to a range of 0 to 1 and solid-liquid separation in the sulfuric acid leaching step. Bismuth purification method.

Images