WO2010084877A1

WO2010084877A1 - Processes for the disposal of arsenic

Info

Publication number: WO2010084877A1
Application number: PCT/JP2010/050622
Authority: WO
Inventors: 三雄鐙屋; 祐輔佐藤; 寛信見上; 良一田口; 尚司久保; 政義松本
Original assignee: Ｄｏｗａメタルマイン株式会社
Priority date: 2009-01-21
Filing date: 2010-01-20
Publication date: 2010-07-29
Also published as: JP2010168237A

Abstract

Provided is a process which is intended to be employed in a refinery where decopperizing electrolysis slime and arsenic sulfide sediment are formed as intermediate products of nonferrous refining with the amount of the former being larger than that of the latter, and by which the disposal of arsenic is enabled without requiring that the mixing ratio between both intermediate products is kept at a specific level. Also provided is a process described above, wherein arsenic is converted into pentavalent arsenic in the leaching step, whereby the ratio of leaching of arsenic is enhanced. Specifically disclosed is a process which comprises: a leaching step of subjecting a mixed slurry of the intermediate products of nonferrous refining to oxidative leaching in an acid region to obtain a leach liquor; a liquor regulation step of adding an oxidizing agent to the leach liquor, thereby oxidizing arsenic into pentavalent arsenic, and thus obtaining a regulated liquor; and a crystallization step of converting the arsenic contained in the regulated liquor into scorodite crystals. The leaching step comprises: the first leaching step of adding elemental sulfur (S⁰) to the mixed slurry at the initiation of the reaction, and then leaching the slurry while adding an oxidizing agent thereto with the temperature raised to 50°C or above and with the pH adjusted to 1.0 to 2.0; the second leaching step of adjusting the pH to 2.0 or above by the addition of an alkali, and then leaching the slurry while adding an oxidizing agent thereto; and the third leaching step of stopping the addition of the oxidizing agent, and then further stirring the slurry.

Description

Arsenic treatment method

The present invention relates to a method for treating arsenic in which arsenic in a smelting intermediate product containing arsenic is extracted out of the system in a stable form.

The following documents exist regarding the stabilization of compounds containing arsenic.
Patent Document 1 describes a method for producing scorodite targeting arsenic contained in smelting ash.

Patent Document 2 describes a method for leaching arsenic sulfide starch by adding alkali while blowing air into a slurry containing arsenic sulfide starch and leaching arsenic while maintaining the pH at 5-8. ing.

Non-Patent Document 1 reports on the solubility product of iron arsenate, calcium arsenate, and magnesium arsenate. According to the literature, calcium arsenate and magnesium arsenate are stable only in the alkaline region, while iron arsenate is stable in the neutral to acidic region, with a minimal solubility of 20 mg / L at pH 3.2. Has been.

Non-Patent Document 2 discloses the solubility of iron arsenate and scorodite. According to this document, the solubility of arsenic from scorodite is shown to be two orders of magnitude lower than that of non-condensed iron arsenate in the weakly acidic region, which discloses that scorodite is a stable arsenic compound.

Non-Patent Document 3 describes a method for generating scorodite targeting arsenic contained in sulfuric acid factory effluent and smelting effluent.

JP 2005-161123 A Japanese Patent Publication No. 61-24329

In recent years, the environment for securing ore raw materials surrounding non-ferrous smelting has been extremely severe worldwide. In particular, in the field of copper smelting, the oligopoly by non-ferrous majors has progressed, and the emerging market has emerged as a new consumer power, and the supply and demand situation has become tight.
Under these circumstances, regulations in the environmental field against pollution have been strengthened and become mandatory in each country. The present inventors considered that mining and smelters that can coexist with the environment will lead the industry in the future.

Here, pollution that is a concern in non-ferrous smelting includes air pollution by SO ₂ gas, soil pollution and drainage pollution by arsenic. Especially for arsenic, arsenic content in copper ore will increase in the future, so more thorough countermeasures are required than ever.
Conventionally, coastal non-ferrous smelters in Japan have been operating without problems by using clean concentrate as a processing raw material. However, since arsenic content in copper ore is expected to increase in the future, we thought that it would be necessary to extract arsenic out of the system as a smelting intermediate and to stabilize and store it in some way.

Overseas, there are many smelters that manage and store arsenic as calcium arsenate, diarsenic trioxide, or arsenic sulfide compounds. However, according to the inventors' consideration, these arsenic compounds are not completely stable in the natural environment.

Here, the present inventors examined the above-mentioned literature. However, both methods have problems in terms of productivity, stability of the generated scorodite, and the like.

On the other hand, the quality of arsenic in copper ore will increase in the future, and in copper smelting, the amount of arsenic sulfide starch generated in the wastewater treatment system will increase, and the load of arsenic on the copper electrolysis plant will also increase. It is thought to go. As a result, it is thought that the amount of decoppered electrolytic slime, which is a smelting intermediate product enriched in arsenic, generated in the copper electrolyte solution purification process also increases. Therefore, it is considered that it is difficult to repeatedly treat these arsenic sulfide starches and intermediate products containing arsenic such as decopperized electrolytic slime in the smelter.

Here, arsenic sulfide starch, which is an intermediate product containing arsenic, and decopperized electrolytic slime will be described.
First, arsenic sulfide starch is a non-ferrous smelting intermediate product containing sulfide-type arsenic. The arsenic sulfide starch is, for example, a residue generated by reacting a sulfiding agent with smelting process water or wastewater containing arsenic. Here, examples of the sulfiding agent include hydrogen sulfide, sodium hydrosulfide, and sodium sulfide.
Next, the copper removal electrolytic slime is a liquid purification process (a process in which impurities such as arsenic accumulated in the copper electrolytic solution are collected and removed by electrowinning) performed in a copper electrolytic refining plant. It is a deposit generated by electrolytic deposition as a metal. The said liquid purification process is the method generally employ | adopted in the copper electrolytic refinery factory. Therefore, the decoppered electrolytic slime is a deposit inevitably generated in order to ensure the quality of electrolytic copper.

Based on the above, a method for simultaneously converting and stabilizing arsenic as scorodite crystals by simultaneously mixing arsenic sulfide starch in which arsenic is in sulfide form and decopperized electrolytic slime in which arsenic or copper is in metal form. Will be very important in the future.
However, in order to be able to treat arsenic sulfide starch and decoppered electrolytic slime at the same time, it is necessary to blend both raw materials at a certain ratio. For example, if the proportion of decopperized electrolytic slime is higher than that of arsenic sulfide starch, a considerable amount of copper ions may remain in the leachate, which may adversely affect scorodite crystal growth in the crystallization process. Is done. Therefore, in a smelter where the amount of decopperized electrolytic slime generated is greater than the amount of arsenic sulfide starch generated, it is not a requirement to keep the blending ratio of these two raw materials at a constant ratio, and a method that enables processing. Is urgently needed.
Furthermore, from the viewpoint of reducing the amount of oxidizing agent used in the liquid adjustment step and reducing the processing cost in the present method, it is desired to provide a method for increasing the rate of leaching arsenic as pentavalent arsenic in the leaching step. .

The present invention has been made under such circumstances, and the problem to be solved is the provision of the above two methods and satisfies the elution standard (according to Environmental Agency Notification No. 13), In addition, the present invention provides a method for easily producing a stable scorodite crystal having excellent filterability without reproducibility and complicated operation.

Here, the present inventors have determined from the X-ray diffraction results of the copper-free electrolytic slime that the copper-free electrolytic slime is composed of copper in the form of metal, arsenic, and copper arsenide in the form of an intermetallic compound. I came up with it. And from the said knowledge, it turned out that it can naturally apply to the copper arsenide thing which generate | occur | produces in a zinc smelter as well as metallic copper instead of the copper removal electrolytic slime in this invention. *

The present inventors have conducted intensive research to solve the above problems. As a result, first, a step of extracting arsenic from the non-ferrous smelting intermediate product containing the arsenic by leaching (leaching step), and then arsenic in the leachate from which the arsenic has been extracted is made pentavalent using an oxidizing agent. Step of oxidizing and removing remaining oxidizing agent (liquid adjustment step), Step of coexisting ferrous ions (Fe ²⁺ ) in the liquid after liquid adjustment, and oxidizing to generate scorodite crystals under acidic conditions The inventors have conceived of performing the three steps of (crystallization step).

Here, the present inventors have made it possible to process from the beginning of the leaching reaction in order to enable processing without requiring that the mixing ratio of both raw materials of arsenic sulfide starch and decopperized electrolytic slime be maintained at a constant ratio. Sulfur (elemental sulfur: S ⁰ ) was added to arrive at a configuration in which dissolved copper ions were fixed as copper sulfide (CuS).
Next, in order to reduce the amount of oxidizing agent used in the liquid adjustment step and reduce the processing cost in this method, the inventors have made an excessive amount of copper ions present during leaching to convert arsenic to pentavalent arsenic. The inventors also conceived of a configuration in which oxidation is promoted, simple sulfur (S ⁰ ) is added at the end of the reaction, and copper ions dissolved in an appropriate pH region are fixed as copper sulfide (CuS).

And the present inventors added elemental sulfur (S ⁰ ) from the beginning of the leaching reaction described above, and fixed the dissolved copper ions as copper sulfide (CuS), or caused an excessive amount of copper ions to exist during leaching. By adopting a configuration that promotes oxidation of arsenic to pentavalent arsenic, adds elemental sulfur (S ⁰ ) at the end of the reaction, and fixes copper ions dissolved in an appropriate pH range as copper sulfide (CuS) It has been conceived that the copper ions in the leachate can be removed to a concentration or less that does not hinder the crystallization process. By removing copper ions in the leachate to a concentration that does not interfere with the crystallization process, the scorodite crystals that satisfy the elution standards and that are excellent in filterability and stable can be operated with good reproducibility. I came up with the idea that it can be generated easily without any problems. As a result, the present invention was completed by obtaining completely new knowledge that arsenic contained in the initial non-ferrous smelting intermediate product can be recovered as a stable scorodite having excellent filterability.

That is, the first invention for solving the above-described problem is
A leaching step of oxidizing and leaching a mixed slurry of a non-ferrous smelting intermediate product containing sulfide form arsenic and a non-ferrous smelting intermediate product containing arsenic and metal form copper in an acidic region;
A liquid adjustment step of adding an oxidizing agent to the leachate to oxidize arsenic to pentavalent arsenic to obtain an adjusted liquid;
A crystallization step of converting the arsenic in the adjusted liquid into scorodite crystals,
In the leaching step, single sulfur (S ^{0 at the} beginning of the reaction) is mixed into a mixed slurry of the non-ferrous smelting intermediate product containing arsenic in the sulfide form and the non-ferrous smelting intermediate product containing arsenic and copper in the metal form. ), Leaching first step of leaching at a temperature of 50 ° C. or higher and a pH of 1.0 or more and 2.0 or less while adding an oxidizing agent, and then after the pH is set to 2.0 or more The leaching second step of leaching while adding the oxidant to the mixed slurry, and then the leaching third step of stopping the addition of the oxidant and further stirring the mixed slurry, It is a processing method.

The second invention is
Wherein the amount of elemental sulfur (S ⁰⁾ is the single body sulfur (S ⁰⁾ 1 times mole or more of the total number of moles of copper remaining as ions leaching solution during when leached without the addition of The method for treating arsenic according to the first invention.

The third invention is
A leaching step of oxidizing and leaching a mixed slurry of a non-ferrous smelting intermediate product containing sulfide form arsenic and a non-ferrous smelting intermediate product containing arsenic and metal form copper in an acidic region;
A liquid adjustment step of adding an oxidizing agent to the leachate to oxidize arsenic to pentavalent arsenic to obtain an adjusted liquid;
A crystallization step of converting the arsenic in the adjusted liquid into scorodite crystals,
In the leaching step, the temperature of the non-ferrous smelting intermediate product containing the sulfide form of arsenic and the non-ferrous smelting intermediate product containing the arsenic and metal form of copper is increased while adding an oxidizing agent to the mixed slurry. First leaching step in which leaching is performed at a temperature of not less than 0 ° C. and a pH of 1.0 or more and 2.0 or less, and then leaching is performed by adding oxidant to the mixed slurry after the pH is set to 2.0 or more. Arsenic, characterized in that it has two steps and a third step of leaching after stopping addition of oxidant and adding elemental sulfur (S ⁰ ) to bring the pH to 2 or less and further stirring It is a processing method.

The fourth invention is:
Wherein the amount of elemental sulfur (S ⁰⁾ is the single body sulfur (S ⁰⁾ 2-fold mole or more of the total number of moles of copper remaining as ions leaching solution during when leached without the addition of The method for treating arsenic according to the third aspect of the present invention.

The fifth invention is:
A leaching step of oxidizing and leaching a mixed slurry of a non-ferrous smelting intermediate product containing sulfide form arsenic and a non-ferrous smelting intermediate product containing arsenic and metal form copper in an acidic region;
A liquid adjustment step of adding an oxidizing agent to the leachate to oxidize arsenic to pentavalent arsenic to obtain an adjusted liquid;
A crystallization step of converting the arsenic in the adjusted liquid into scorodite crystals,
In the leaching step, single sulfur (S ^{0 at the} beginning of the reaction) is mixed into a mixed slurry of the non-ferrous smelting intermediate product containing arsenic in the sulfide form and the non-ferrous smelting intermediate product containing arsenic and copper in the metal form. ), Leaching first step in which leaching is performed while adding the oxidizing agent and the temperature is set to 50 ° C. or more, and the pH is set to 1.0 or more and 2.0 or less, and then the pH is set to 2.0 or more, The second step of leaching in which oxidant is added to the mixed slurry and then leaching is stopped, and then the addition of the oxidant is stopped and single sulfur (S ⁰ ) is added to bring the pH to 2 or less, followed by further stirring And a third step of leaching.

The sixth invention is:
The non-ferrous smelting intermediate product containing arsenic and metallic copper is decopperized electrolytic slime and / or copper arsenide, according to any one of the first to fifth inventions, This is a method for treating arsenic.

The seventh invention
In the leaching step, after the leaching first step, the pH is set to 2.0 or more, and then the leaching second step is performed while adding the oxidant to the mixed slurry while maintaining the pH unretained. The arsenic processing method according to any one of the first, third, and fifth inventions.

The eighth invention
The arsenic treatment method according to any one of the first, third, fifth, and seventh inventions, wherein air and / or oxygen gas blowing is used as the oxidizing agent added to the mixed slurry. .

The ninth invention
In the liquid adjustment step, hydrogen peroxide is added as an oxidant at 40 ° C. or more, and after arsenic is oxidized to pentavalent arsenic to obtain an adjusted liquid, the post-reaction liquid and metal copper are brought into contact with each other to remain. Any one of the first to eighth inventions is characterized in that the hydrogen peroxide to be removed is removed, or the post-reaction liquid is further maintained by stirring to remove hydrogen peroxide remaining in the post-adjustment liquid. The arsenic treatment method described in 1.

The tenth invention is
The first to ninth inventions, wherein the crystallization step is a crystallization step in which ferrous ions coexist in the adjusted solution, and the ferrous ions are oxidized with pentavalent arsenic. The arsenic treatment method according to any one of the above.

The eleventh invention is
The arsenic treatment method according to the tenth invention, wherein the oxidation reaction is carried out at a pH of 1 or less.

The twelfth invention
The arsenic treatment method according to the tenth invention, wherein the oxidation reaction is performed at a temperature of 50 ° C. or higher.

According to the invention described in any one of the first to twelfth inventions, a stable scorodite crystal having excellent filterability and reproducibility could be easily produced without complicated operations. Further, the generated scorodite crystals were able to greatly satisfy the elution standard value (according to Environmental Agency Notification No. 13).

It is a process flow figure showing the processing method of arsenic concerning the present invention.

As described above, the embodiment of the arsenic treatment method according to the present invention leaches arsenic in a weakly acidic region from the non-ferrous smelting intermediate product (1) containing arsenic as described in the process flow shown in FIG. First to third leaching steps (2) to (4), a liquid adjusting step (6) for adding oxidant to the leaching solution (5) to oxidize arsenic to pentavalent arsenic, and arsenic in the adjusted solution And a crystallization step (7) for converting to scorodite (8). The leaching residue (9) produced in the leaching first to third steps (2) to (4) is returned to the copper smelting (10), and the filtrate (11) produced in the crystallization step (7) is drained. Processing is performed in the processing step (12).

Hereinafter, embodiments according to the present invention will be described. 1. Non-ferrous smelting intermediate product containing arsenic (1) 2. First to third leaching steps (2) to (4); 3. Liquid adjustment step (6), It demonstrates in order of a crystallization process (7).

1. Non-ferrous intermediates containing arsenic (1)
Non-ferrous smelting intermediate product (1) leaching pulp containing arsenic, which is a raw material, is suitable for smelters that produce a large amount of decoppered electrolytic slime. If the (later-described (equation 4), compared to the arsenic sulfide _(as 2 _{S 3)} is decoppered electrolytic slime (Cu ^0), a case of less than quantitatively reactive equivalent, "Cu ⁰ rich or less When the amount of de-coppered electrolytic slime in the smelter where a large amount of arsenic sulfide starch is generated is smaller than that of arsenic sulfide starch (in the following (Formula 4), the amount of arsenic sulfide) (As ₂ S ₃ ) is a case where there is a reaction equivalent or more compared to the amount of copper removal electrolysis slime (Cu ⁰ ), and is described below as “when As ₂ S ₃ is abundant”. There is.

2. Leaching first to third steps (2) to (4)
In the leaching first to third steps (2) to (4) according to the embodiment of the present invention, the starting stage of the leaching first step (2) (in the starting stage, the raw material mixing for performing the leaching first step) second embodiment the addition of the first embodiment of adding elemental sulfur (S ⁰⁾ in step are also included.), elemental sulfur at the end of the leaching third step (4) the (S ⁰⁾ and, A part of elemental sulfur (S ⁰ ) is added to the beginning of the first leaching step (2) (including the raw material mixing stage for the first leaching step), and the third leaching step There is a third embodiment in which the remainder is added at the end of (4).
On the other hand, as described above, in the blending of the leached pulp of the non-ferrous smelting intermediate product (1) containing arsenic as the raw material, “when Cu ⁰ is abundant” and “when As ₂ S ₃ is abundant” There are two cases.

Therefore, first, [the basic structure of the reaction common in the leaching first to third steps (2) to (4) according to the first to third embodiments] will be described, and then [“Cu ⁰ Explaining the leaching first to third steps (2) to (4) according to the first to third embodiments ”
Further, the leaching first to third steps (2) to (4) according to the first to third embodiments in “when As ₂ S ₃ is abundant” will be described.

[Basic structure of reaction common in leaching first to third steps (2) to (4) according to first to third embodiments]
First, an oxidizing agent is added to the mixed pulp of the non-ferrous smelting intermediate product (arsenic sulfide starch and decopperized electrolytic slime) (1) containing arsenic (for example, air and / or oxygen gas is preferably blown). Then, the first step (2) of leaching is carried out, in which the pH is set between 1 and 2 under heating, and in particular, the leaching of the decoppered electrolytic slime in the metal form is advanced. Next, after adding an alkali (for example, sodium hydroxide) to bring the pH to 2 or more, the pH control of the leaching solution is not maintained, and leaching mainly leaching unreacted arsenic sulfide starch while maintaining the change in pH. A 2nd process (3) is performed. Further, the third step of leaching, in which the addition of the oxidizing agent is stopped at the end of leaching, and copper ions dissolved in the leaching solution are sulfided with elemental sulfur (S ⁰ ) contained in the leaching residue and removed as copper sulfide (CuS). Perform 4).

Hereinafter, the leaching first to third steps will be specifically described based on the chemical reaction formula. Since copper and arsenic in the copper removal electrolytic slime are in a metal form, they are expressed as Cu ⁰ and As ⁰ for convenience.

The first leaching step (2) is considered to consist of elementary reactions of the following (formula 1), (formula 2) and (formula 3).
Cu ⁰ + 2H ⁺ + 1 / 2O ₂ = Cu ²⁺ + H ₂ O (Formula 1)
As ⁰ + 3 / 4O ₂ + 1 / 2H ₂ O = HAsO ₂ (Formula 2)
^{_{_{_{Cu 2+ + 1 / 3As 2 S}}}} 3 + 4 / 3H 2 O = CuS + 2 / 3HAsO 2 + 2H + ··· ( Equation 3)
That is, the reaction of copper (Cu ⁰ ) and arsenic sulfide (As ₂ S ₃ ) in the decopperized electrolytic slime is expressed by (Expression 4) below from (Expression 1) + (Expression 3).
Cu ⁰ +1/3 As ₂ S ₃ + 1 / 2O ₂ + 1 / 3H ₂ O = 2/3 HAsO ₂ + CuS (Formula 4)

In the said leaching 1st process (2), in order to mainly advance the leaching of the copper removal electrolytic slime in a metal form, the pH of raw material mixing pulp is adjusted to the acidic side. General-purpose sulfuric acid is suitable as the acid for adjusting the pH.
Here, it is generally considered that the lower the pH is, the better, in order to oxidize and leach copper-type electrolytic copper slime in metal form. However, according to studies by the present inventors, it has been found that the pH value is preferably 1-2. This is presumably because the primary particles of the decoppered electrolytic slime are very fine, 10-30 μm, and are inherently rich in reactivity. In addition, the pH at the start of the reaction in the crystallization process, which is a subsequent process, is set to 1. From the viewpoint of reducing the amount of alkali used in the second leaching process, the pH 1-2 setting in the leaching first process (2) is Convenient.

Moreover, what is necessary is just to perform the leaching time in the said leaching 1st process (2) for 30 minutes or more. This is because the reactivity is good as described above.
Leaching proceeds by setting the temperature during leaching to 50 ° C. or higher. However, the temperature during leaching is preferably determined according to the balance between the amount of copper removal electrolytic slime and the amount of arsenic sulfide starch.

In the leaching second step (3), at the end of the leaching first step (2), after adding alkali (for example, sodium hydroxide) to pH 2 or higher, the pH control of the leachate is not retained, and the pH change is determined. This is a process of leaching while proceeding.
This step is considered to consist of the elementary reactions of the following (formula 5) (formula 6) (formula 7) and the above-described (formula 3).
As ₂ S ₃ + 3 / 2O ₂ + H ₂ O = 2HAsO ₂ + 3S ⁰ (formula 5)
HAsO ₂ + 1 / 2O ₂ + H ₂ O = H ₂ AsO ₄ ⁻ + H ⁺ (formula 6)
Cu ²⁺ + S ⁰ → CuS (formula 7)
Arsenic sulfide starch is more likely to dissolve on the neutral side than on the acidic side, and it is considered that unleached arsenic sulfide is dissolved by (Equation 5) in the first leaching step (2). At the same time, hydrogen ions (H ⁺ ) are released in (Expression 6), (Expression 7), and (Expression 3), and the pH is naturally lowered. This is considered convenient because the pH at the start of crystallization is 1, and the acid side is shifted to without adding an acid.
The amount of sodium hydroxide to be added is such that the Na concentration in the leachate is 20 g / l or less, preferably 10 g / l or less. This is because if the Na concentration is 20 g / l or less, the viscosity of the reaction pulp in the crystallization step is preferably kept low.

Like the leaching first step (2), the temperature of the mixed slurry in the leaching second step (3) is 50 ° C. or more, and leaching proceeds. However, the temperature during leaching is preferably determined according to the balance between the amount of copper removal electrolytic slime and the amount of arsenic sulfide starch. However, for the purpose of positively leaching unreacted arsenic sulfide starch, it is preferably set higher than the first leaching step (2).
Further, the reaction time of the second leaching step (3) is preferably 30 minutes or more, preferably 45 minutes or more from the viewpoint of sufficiently ensuring the progress of the reaction.

In the leaching third step (4), the addition of the oxidizing agent (for example, air and / or oxygen gas blowing is preferable) is stopped, and the copper ions dissolved in the leaching liquid are contained in elemental sulfur ( This is a step of removing as copper sulfide (CuS) by S ⁰ ).
The reaction in this step is mainly based on (Expression 7) described above. Accordingly, the higher the leaching temperature is, the higher the reaction, but it is preferable that the leaching temperature is actually determined by the equipment material.
Strictly speaking, (Equation 7) is a reaction accompanied by the release of hydrogen ions (H ⁺ ), so the pH value slightly shifts to the acidic side.
The purpose of this step is mainly to remove copper, but according to the study by the present inventors, elements other than copper that easily form sulfides (for example, Pb, Hg, Bi, Sb, etc.) ), It was found that the same effect can be expected by the dissolved concentration.

[Leaching First to Third Steps (2) to (4) according to First to Third Embodiments in “Abundant Cu ⁰ ”]
Here, “the case where Cu ⁰ is abundant” is a case where the arsenic sulfide starch is less than the reaction equivalent in terms of quantity as compared with the copper removal electrolytic slime (Cu ⁰ ) in the above-described (Formula 4).
In this case, since As ₂ S ₃ sufficient to sulfidize the blended Cu ⁰ is insufficient, excess Cu is contained in the leachate (5) at the end of the first to third steps (2) to (4). ⁰ remains as copper ions (Cu ²⁺ ) and is brought to the crystallization step (7).
Since the copper ions dissolved in the crystallization liquid in the crystallization step (7) act as an oxidation catalyst in the scorodite (8) crystallization, in order to make the oxidation conditions in the crystallization step (7) constant, It is necessary to suppress and standardize the copper concentration. From this point of view, when the copper concentration in the leachate (5) is 1 g / l or less, preferably 500 mg / l or less, variation in the oxidization conditions of the crystallization conditions can be suppressed, and the stability of the crystallization step (7) can be suppressed. This is preferable because it leads to Moreover, not leaving copper ions in the leachate (5) leads to avoidance of copper loss, which is preferable from the viewpoint of active recovery of resources.

Hereinafter, specific operation methods according to the first to third embodiments will be described.
<< Leaching first to third steps (2) to (4) according to the first embodiment in "when Cu ⁰ is abundant">>
In the first embodiment, elemental sulfur (S ⁰ ) is added in the leaching first step (2), and excess Cu ⁰ in the leaching solution (5) is finally converted to copper sulfide (CuS), thereby leaching residue. (9).
Regarding the timing of addition of elemental sulfur (S ⁰ ) in the first leaching step (2), it is preferable to start the addition of an oxidizing agent (for example, air and / or oxygen gas is preferably blown). However, in consideration of handling properties, it is better to prepare and repulse simple sulfur (S ⁰ ), arsenic sulfide starch, and decopperized electrolytic slime at the same time when preparing the raw material.

Here, the amount of elemental sulfur (S ⁰ ) added is the total amount of copper remaining as ions in the leachate when leached without adding elemental sulfur (S ⁰ ), as described in Example 1 described later. If the number of moles is 1.0 times or more, the copper in the leachate (5) can be removed to 1 g / l or less. Similarly, if the total number of moles of copper remaining as ions in the leachate (5) is 1.3 times or more, the copper in the leachate (5) can be removed to 500 mg / l or less.

Here, the specific addition amount of elemental sulfur (S ⁰ ) can be obtained by the following calculation.
・ Assuming that all arsenic in the arsenic sulfide starch is in the As ₂ S ₃ form, the amount is obtained.
In Equation 4, the amount of Cu ⁰ that reacts with the amount of As ₂ S ₃ calculated in 1) above is obtained.
・ Assuming that all copper in the copper removal electrolytic slime is in metal form, the amount of copper is determined.
The amount of copper dissolved as copper ions in the leachate (5) is determined from the difference between the amount of copper in 3) and the amount of Cu ⁰ in 2).
The amount of elemental sulfur (S ⁰ ) added is 1.0 mol or more of the total molar amount of copper dissolved in the leachate (5) obtained from 4) above.

In the leaching first step (2), it is desirable to dissolve copper ions (Cu ²⁺ ) as an arsenic oxidation catalyst, and (Formula 1) is given priority while suppressing (Formula 3) and (Formula 7). From the viewpoint, a lower leaching temperature is more effective. The presence of this copper ion exhibits its effect particularly in the second leaching step (3). Although leaching itself proceeds at a leaching temperature of 50 ° C. or higher, a leaching temperature of 60 to 80 ° C. is preferable in consideration of shortening of the leaching time. As described above, the leaching time is sufficient if it is 30 minutes or longer.

In the subsequent leaching second step (3), the pH of the mixed slurry is set to 2.0 or more, and the pH is increased to promote the oxidation of trivalent arsenic to pentavalent arsenic, while unreacted arsenic sulfide. The starch can be actively leached. In order to ensure these two purposes, the leaching temperature is preferably 70 to 80 ° C., which is slightly higher than the leaching first step (2), and the leaching time is preferably 30 minutes or more, preferably 45 minutes or more. .

Further, in the final leaching third step (4), addition of the oxidizing agent is stopped at the end of leaching (for example, blowing of air and / or oxygen gas is stopped). Since the third leaching step (4) is a step of completing the reaction between copper ions remaining until the end of leaching and elemental sulfur (S ⁰ ) added at the beginning of leaching, the higher the leaching temperature, the better. C. or higher is preferable. However, in actual operation, even if the material on the actual equipment is taken into consideration, it is possible even at around 80 ° C. The leaching time is preferably 30 minutes or longer.

<< Leaching first to third steps (2) to (4) according to the second embodiment in "when Cu ⁰ is abundant">>
In a second embodiment where Cu ⁰ is abundant, the addition of oxidant is stopped at the end of leaching (eg, blowing off air and / or oxygen gas), elemental sulfur (S ⁰ ) is added, and excess Cu is added. ⁰ is finally converted into copper sulfide (CuS) to form a leaching residue (9). The leaching first step (2) and the leaching second step (3) in the second embodiment are basically the same as those in the first embodiment described above. However, copper ions are sufficiently dissolved up to the end of leaching when elemental sulfur (S ⁰ ) is added, and basically conditions for easily oxidizing trivalent arsenic to pentavalent arsenic are prepared. Accordingly, the leaching temperature may not be as strict as in the first embodiment. That is, from the viewpoint of actively promoting arsenic oxidation, the leaching temperature can be performed at a high temperature in both the leaching first step (2) and the leaching second step (3). However, considering the material on the actual equipment in actual operation, about 80 ° C. is preferable.

In the final leaching third step (4), the addition of the oxidant is stopped (for example, the blowing of air and / or oxygen gas is stopped), then the sulfur (S ⁰ ) is added, mixed into the leached pulp, and the above-mentioned The copper removal reaction based on (Formula 7) is performed.
The addition amount of elemental sulfur (S ⁰⁾ is when leached without the addition of elemental sulfur (S ^0), there in leachate (5) 2.0 moles or more of the total number of moles of copper remaining as ions in For example, the copper in the leachate (5) can be removed to 1 g / l or less. Similarly, if the total number of moles of copper remaining as ions in the leachate (5) is 2.5 times or more, the copper in the leachate (5) can be removed to 500 mg / l or less.

Furthermore, as a result of intensive studies by the present inventors regarding the pH of the leaching reaction, it has been found that the reactivity between elemental sulfur (S ⁰ ) and copper ions remarkably depends on the pH. Specifically, as described in Example 2 and Comparative Example 2, when the reaction pH of elemental sulfur (S ⁰ ) is 2 or more, the reaction shown in (Equation 7) becomes very slow and Copper capacity is incomplete. On the other hand, if the pH is 2 or less, the reaction shown in (Formula 7) proceeds rapidly.
Although the clear reason for this phenomenon is unknown, the present inventors have found that a considerable amount of arsenic in the leachate has been oxidized to pentavalent arsenic, and these pentavalent arsenic forms copper arsenate when the pH is 2 or more. It is presumed that this will hinder the progression of (Equation 7). Therefore, if the pH of the leached pulp is not lowered to 2 or less, the pH is adjusted to 2 or less by adding sulfuric acid or the like after the addition of elemental sulfur (S ⁰ ).
The leaching time may be the same as in the case of the first embodiment in the above “in the case where Cu ⁰ is abundant”.

<< Leaching first to third steps (2) to (4) according to the third embodiment in "when Cu ⁰ is abundant">>
At the beginning of leaching, a part of elemental sulfur (S ⁰ ) is added, and after leaching first step (2) and leaching second step (3), leaching last step leaching third step (4) Stop adding the oxidizer (for example, stop blowing air and / or oxygen gas), add the remainder of the elemental sulfur (S ⁰ ) to the leached mixed slurry, and finally add excess Cu ⁰ to copper sulfide (CuS) As leaching residue (9). The third embodiment is a leaching method using the advantages of the first and second embodiments described above.

That is, the first embodiment has an advantage that copper can be removed to a low concentration with a small amount of elemental sulfur (S ⁰ ) added, and the second embodiment has an arsenic oxidation rate. Has the advantage of extremely high.

Here, a method for adding elemental sulfur (S ⁰ ) capable of utilizing the advantages of the first and second embodiments will be described.
The addition method is a method in which elemental sulfur (S ⁰ ) is added at the beginning and the latter stage of the leaching first to third steps (2) to (4).
First, the addition amount at the beginning of leaching is 1.0 times the total number of moles of copper remaining as ions in the leaching solution when leaching without adding elemental sulfur (S ⁰ ). By adding 1.0 times the total number of moles of the remaining copper, the copper ion concentration in the leached pulp during leaching can be guaranteed at least 1 g / l. Then, the first leaching step (2) and the second leaching step (3) are performed, and the amount of elemental sulfur (S ⁰ ) added in the leaching third step (4) at the end of leaching is 1 g of the residual copper concentration. Assuming / l, 20 times mole or more of the total number of moles of copper is added. As a result, the remaining copper can be reduced to 500 mg / l or less.
The leaching time and the leaching temperature may be the same as those in the first embodiment in the above-mentioned “in the case where Cu ⁰ is abundant” in order to promote the arsenic oxidation by dissolving copper ions as much as possible during the leaching.
It should be noted that the amount of elemental sulfur (S ⁰ ) added separately in the leaching start stage and leaching end stage can be variously changed, and is not necessarily limited to the above-described conditions.

<< Leaching first to third steps (2) to (4) according to the first embodiment in "when As ₂ S ₃ is abundant">>
In the above (Formula 4), the compounding amount of arsenic sulfide (As ₂ S ₃ ) in the arsenic sulfide starch is 1.0 to 1.1 times equivalent of the reaction to the copper (Cu ⁰ ) of the copper removal electrolytic slime. In the range, practically, copper ions may remain in the final leachate from several hundred mg / l to about 1 g / l. As a cause of this, the reaction can be easily completed if the blending amount of arsenic sulfide (As ₂ S ₃ ) is, for example, 2 times equivalent, but it may be difficult to complete the reaction if it is 1.0 to 1.1 times equivalent. Moreover, the difference in activity for each raw material can be considered.
From the generation ratio of both raw materials, the first embodiment in “when As ₂ S ₃ is abundant” can be applied to the processing at the smelter that is forced to perform such raw material blending processing.

In this example, the amount of elemental sulfur (S ⁰ ) added at the beginning of the leaching is assumed to be a residual copper concentration of 1 g / l. It can always be 100 mg / l or less.
The leaching time and leaching temperature may be the same as those in the first embodiment described above in the case of “rich Cu ⁰ ” from the viewpoint of accelerating arsenic oxidation by dissolving copper ions as much as possible during leaching.

<< Leaching first to third steps (2) to (4) according to the second embodiment in "when As ₂ S ₃ is abundant">>
In the present embodiment as well, as in the first embodiment described above, “when As ₂ S ₃ is abundant”, the copper (Cu ⁰ ) of the decopperized electrolytic slime is compared with arsenic sulfide in the arsenic sulfide starch. This is applicable when the blending amount of F (As ₂ S ₃ ) is 1.0 to 1.1 times the equivalent of the reaction.

In this example, the amount of elemental sulfur (S ⁰ ) added at the end of leaching is assumed to be a residual copper concentration of 1 g / l. It can always be 100 mg / l or less.
The leaching time and leaching temperature may be the same as those in the first embodiment described above in the case of “rich Cu ⁰ ” from the viewpoint of accelerating arsenic oxidation by dissolving copper ions as much as possible during leaching.

<< Leaching first to third steps (2) to (4) according to the third embodiment in "when As ₂ S ₃ is abundant">>
In the present embodiment, similarly to the first and second embodiments in the above-mentioned “when As ₂ S ₃ is abundant”, arsenic sulfide in the arsenic sulfide starch (Cu ⁰ ) in the copper removal electrolytic slime ( This can be applied when the amount of As ₂ S ₃ ) is 1.0 to 1.1 times the equivalent of the reaction.

In this example, the amount of elemental sulfur (S ⁰ ) added at the beginning of leaching is the same as the amount of addition described in the first embodiment in the above-mentioned “when As ₂ S ₃ is abundant”. The amount of elemental sulfur (S ⁰ ) added at the end is also the same as the amount added in the second embodiment in the above “when As ₂ S ₃ is abundant”. Then, the copper ions in the leachate can be removed almost completely to a level of several m / l.
The leaching time and the leaching temperature in the present embodiment may be the same as those in the first embodiment in the above-described “in the case where Cu ⁰ is abundant” based on the same idea.

As described above, the present invention discloses the effect of addition of elemental sulfur (S ⁰ ) in wet processing of non-ferrous smelting intermediate products containing arsenic. In addition, it is known that coexistence of sulfite gas (SO ₂ gas) and sulfite ion (SO ₃ ²⁻ ) acts as a catalyst for promoting the reaction during the sulfurization reaction using addition of elemental sulfur (S ⁰ ). Of course, it is possible to use them together in the present invention.

In addition, many heavy metals other than copper (for example, Pb, Hg, Bi, Sb, etc.) also have the ability to form sulfides with a strong affinity for sulfur. Therefore, the method for adding elemental sulfur (S ⁰ ) disclosed in the present invention allows the copper in the leachate (5) to be removed without any problems by setting the above-described blend in (Formula 4) to 1.1 times equivalent or more. Even in the case where the amount of heavy metals other than copper is taken into consideration, the optimum amount of elemental sulfur (S ⁰ ) is added and leaching is performed in accordance with each embodiment described above. is there.

Furthermore, the category of the present invention is not limited to the removal of copper in the leachate (5), but can be applied to the control of the elution of many contained heavy metals.

There are other methods for leaching the mixed pulp of arsenic sulfide starch and decoppered electrolytic slime.
While adding an oxidizing agent (for example, air and / or oxygen gas is preferably blown) to the mixed slurry of arsenic sulfide starch and decopperized electrolytic slime, by adding alkali (for example, sodium hydroxide) under heating. While maintaining the pH at 4.0 or more and 6.5 or less, the first step of leaching that promotes leaching of arsenic sulfide particularly in the form of sulfide, and then the pH control of the leachate is not retained, The leaching second step of leaching the decoppered electrolytic slime and unreacted arsenic sulfide starch in the course of change, and the addition of the oxidizing agent was stopped at the end of leaching, and the copper ions dissolved in the leaching solution were dissolved in the leaching residue. And leaching third step for removing copper sulfide (CuS) with elemental sulfur (S ⁰ ) contained in the leaching method.
This leaching method is also applied to the same raw material system as in the present invention, and is leaching in a weakly acidic region, and a leachate having the same liquid quality is obtained. Therefore, for the crystallization process of generating scorodite by adding the elemental sulfur (S ⁰ ) according to the present invention at the beginning of leaching, adding at the end of leaching, or adding twice at the beginning and end of leaching. Naturally, the configuration for securing an optimal leaching solution can also be applied to the leaching method.

3. Liquid adjustment process (6)
In the liquid adjustment step (6), an oxidant is added to the leachate (5) obtained in “1. Leaching first to third steps” to oxidize arsenic dissolved as trivalent to pentavalent arsenic. In this step, an adjusted solution is obtained, and then the oxidant remaining in the adjusted solution is removed.

First, the oxidizing agent used in the liquid adjustment step (6) will be described.
In general, oxidation of trivalent arsenic to pentavalent arsenic is easier in the neutral region than in the acidic region, and in the alkaline region than in the neutral region. However, the leachate according to the present invention is acidic. Therefore, it is conceivable to add alkenyl (for example, sodium hydroxide) to the acidic leachate to make the liquid alkaline, and then oxidize arsenic. However, according to the study by the present inventors, a large amount of alkali is required for the liquid alkalinization, which is disadvantageous in terms of cost. In addition, the salt concentration in the liquid is increased, and the scorodite in the subsequent process is increased. (8) It came up with an adverse effect on generation. Note that trivalent arsenic and pentavalent arsenic mean that the ion valence is +3 valent arsenic (plus trivalent) or +5 valent arsenic (plus 5 valent).

First, the present inventors examined oxidation of trivalent arsenic using oxygen in a neutral region (pH 6 to 7). However, it has been found that oxidation of trivalent arsenic remains insufficient. Therefore, the use of a copper-based catalyst (in this study, copper arsenate was examined) was also examined, but it did not reach the complete oxidation of trivalent arsenic to pentavalent arsenic.

Here, the present inventors have conceived that hydrogen peroxide (H ₂ O ₂ ) is used as an oxidizing agent. Then, when the oxidation of arsenic was examined in the acidic region using the hydrogen peroxide, it was confirmed that the oxidation proceeded sufficiently.
However, after the arsenic oxidation reaction, the hydrogen peroxide remaining in the adjusted liquid oxidizes some of the ferrous ions that coexist in the subsequent crystallization step (7). Therefore, in order to accurately manage the ferrous ion concentration, it is desirable to remove the remaining hydrogen peroxide, although it depends on the residual amount of hydrogen peroxide.

This will be specifically described below.
First, the hydrogen peroxide used may be a general-purpose product having a concentration of 30 to 35%.
It is considered that oxidation of trivalent arsenic to pentavalent arsenic under an acidic region proceeds according to the following (formula 8) and (formula 9).
HAsO ₂ + H ₂ O ₂ = H ₃ AsO ₄ (Equation 8)
HAsO ₂ + H ₂ O ₂ = H ₂ AsO ₄ ⁻ + H ⁺ ... (Formula 9)

The addition amount of hydrogen peroxide is preferably 1 to 1.2 times the reaction equivalent based on the trivalent arsenic concentration and (Equation 8) (Equation 9). However, when the concentration of trivalent arsenic is unknown, it may be taken as a guide that the oxidation-reduction potential of the liquid at a liquid temperature of 80 ° C. has reached 500 mV (Vs; Ag / AgCl) or more after the addition of the hydrogen peroxide.

The addition time of hydrogen peroxide depends on the concentration of trivalent arsenic to be oxidized. For example, when oxidizing trivalent arsenic with a concentration of 20 g / L, the addition time is preferably 5 minutes or more. This is because, by taking sufficient addition time, it is possible to avoid that hydrogen peroxide is partly decomposed rapidly, bubbles are generated, and the addition efficiency is deteriorated. More preferably, the addition time is 10 minutes to 15 minutes.

Oxidation of trivalent arsenic to pentavalent arsenic by addition of hydrogen peroxide is very fast, and a decrease in pH and an increase in liquid temperature due to reaction heat are observed. However, the reaction time is preferably 60 minutes or more from the viewpoint of complete oxidation, and is preferably terminated when the oxidation-reduction potential of the liquid becomes 450 mV (Vs; Ag / AgCl) or less.

Here, a method for treating hydrogen peroxide remaining in the solution after adjustment will be described.
There are the following two methods for treating the residual hydrogen peroxide.
1) Method of removing residual hydrogen peroxide by contacting it with metallic copper 2) Method of spontaneously decomposing residual hydrogen peroxide by maintaining stirring of the adjusted liquid at high temperature

1) Method for removing residual hydrogen peroxide by contact with metallic copper by consumption:
After the arsenic oxidation reaction, the hydrogen peroxide remaining in the adjusted solution can be removed by contacting with metallic copper.
Specifically, a method is generally used in which copper powder is added to the adjusted solution and stirred to react. However, in an actual plant operation, the object can be achieved by passing through a column filled with copper plate or copper scrap for the purpose of simplification.
The liquid temperature of the liquid after adjustment is preferably 40 ° C. or higher in order to complete the reaction.
The removal reaction is considered to proceed as shown below (Formula 10).
Cu ⁰ + H ₂ O ₂ + H ₂ SO ₄ = CuSO ₄ + 2H ₂ O (formula 10)
As a result, since the removal reaction is accompanied by an increase in pH, it can be determined that the removal is complete when the pH shows a constant value.

2) Method for spontaneous decomposition of residual hydrogen peroxide by maintaining stirring of the adjusted solution at high temperature:
Here, the high temperature means a temperature of 70 to 100 ° C.
As an example, at 80 ° C. considering actual equipment materials, etc., stirring of the adjusted liquid is maintained until the liquid potential of the adjusted liquid (potential at 80 ° C., Ag / AgCl electrode standard) reaches a predetermined value. The residual hydrogen peroxide will be described. The amount of residual hydrogen peroxide in the solution after adjustment cannot be directly quantified. Therefore, the amount of residual hydrogen peroxide was compared according to the concentration of copper eluted by reacting the adjusted solution with copper powder.
As a result, 420 mV → eluting copper concentration = 144 mg / l
410 mV → eluted copper concentration = 107 mg / l
400 mV → eluted copper concentration = 66 mg / l
390 mV → eluting copper concentration = 36 mg / l.

From the above results, by maintaining the stirring at 80 ° C. until the liquid potential of the adjusted liquid becomes 390 mV or less, the residual hydrogen peroxide amount is reduced to the residual hydrogen peroxide amount corresponding to 50 mg / l or less as the eluting copper concentration. It was confirmed that it can be removed. The potential of 390 mV is a potential that can be reached by stirring for 1 hour at 80 ° C. after the end of oxidation (60 minutes after addition of a predetermined amount of hydrogen peroxide). And it was thought that there was almost no influence of residual hydrogen peroxide considering the eluted copper concentration (36 mg / l).

As described above, there are two possible methods for removing residual hydrogen peroxide from the adjusted solution. Here, the method of consuming residual hydrogen peroxide using metallic copper can be removed in a short time, but the operation is somewhat complicated. On the other hand, the natural decomposition method by maintaining stirring of the adjusted liquid at high temperature is easy to operate, but the reaction time is longer than the method of consuming residual hydrogen peroxide using metallic copper, The operating rate will be reduced. Therefore, a method suitable for the process should be determined in consideration of both characteristics.

According to the liquid adjustment step (6) according to the present invention, trivalent arsenic can be oxidized to pentavalent arsenic without complicated operation even if the leachate (5) is in the acidic region, and arsenic scorodite (8 High conversion rate to) can be maintained.

4). Crystallization process (7)
The crystallization step (7) is a step of crystallizing the pentavalent arsenic in the adjusted liquid obtained in the “2. Liquid adjustment step (6)” to scorodite (8).
The arsenic concentration of the adjusted liquid obtained after finishing the liquid adjusting step (6) is preferably a concentrated liquid of 20 g / L or more, preferably 30 g / L or more, considering the productivity of scorodite.
First, ferrous ions (Fe ²⁺ ) are allowed to coexist with the adjusted solution, and then sulfuric acid (H ₂ SO ₄ ) is added to adjust the pH to 1 at room temperature.
Here, in order to allow ferrous ions (Fe ²⁺ ) to coexist in the adjusted solution, ferrous salt, ferrous hydroxide (Fe (OH) ₂ ) or the like is added to the adjusted solution and dissolved. And a method of mixing a concentrated liquid of ferrous ions (Fe ²⁺ ). In the present invention, any method is possible, but from the viewpoint of easy pH adjustment and securing a high arsenic concentration, a method of adding and dissolving a ferrous salt is preferable. Although there are various ferrous salt compounds, ferrous sulfate is preferred from the viewpoint of the corrosion resistance of the equipment and the availability.
The addition amount of the ferrous salt is not less than 1 equivalent, preferably 1.5 equivalents of the total molar amount of arsenic to be treated as the pure Fe amount.

After the pH adjustment is completed after adding and dissolving the ferrous salt, the adjusted solution is heated to a predetermined reaction temperature.
Here, when the reaction temperature is 50 ° C. or higher, scorodite (8) can be precipitated. However, from the viewpoint of increasing the particle size of scorodite, the higher the reaction temperature, the better. However, from the viewpoint of enabling the reaction in an air atmosphere, the reaction temperature is desirably 90 to 100 ° C.

When the adjusted liquid reaches a predetermined reaction temperature, addition of an oxidant (for example, air and / or oxygen gas blowing is preferable) is started, and strong mixing is performed to create a gas-liquid mixed state. The high-temperature oxidation reaction proceeds while maintaining the reaction temperature.
The high temperature oxidation reaction is considered to proceed as in the following (formula 11) to (formula 16).
(First half of the reaction)
2FeSO ₄ + 1 / 2O ₂ + H ₂ SO ₄ = Fe ₂ (SO ₄ ) ₃ + H ₂ O (formula 11)
2H ₃ AsO ₄ + Fe ₂ (SO ₄ ) ₃ + 4H ₂ O = 2FeAsO ₄ .2H ₂ O + 3H ₂ SO ₄ ... (Formula 12)
(All reaction formulas (Formula 11 + Formula 12) are shown in the following (Formula 13).)
2H ₃ AsO ₄ + 2FeSO ₄ + 1 / 2O ₂ + 3H ₂ O = 2FeAsO ₄ .2H ₂ O + 2H ₂ SO ₄ ... (Formula 13)
(Second half of reaction when arsenic concentration decreased)
2FeSO ₄ + 1 / 2O ₂ + H ₂ SO ₄ = Fe ₂ (SO ₄ ) ₃ + H ₂ O (formula 14)
2 / 3H ₃ AsO ₄ + 1 / 3Fe ₂ (SO ₄ ) ₃ + 4 / 3H ₂ O = 2 / 3FeAsO ₄ .2H ₂ O + H ₂ SO ₄ ... (Formula 15)
(The entire reaction formula (Formula 14 + Formula 15) is shown in the following (Formula 16).)
2 / 3H ₃ AsO ₄ + 2FeSO ₄ + 1 / 2O ₂ + 4 / 3H ₂ O = 2 / 3FeAsO ₄ .2H ₂ O + 2 / 3Fe ₂ (SO ₄ ) ₃ ... (Formula 16)

Depending on the oxidation method, the pH, arsenic concentration, and Fe concentration drop rapidly in 2 to 3 hours after the start of the high temperature oxidation reaction. In this stage, the oxidation-reduction potential of the liquid is 400 mV or higher (Vs; Ag / AgCl) at 95 ° C. And 90% or more of the contained arsenic becomes scorodite (8) crystals. After 3 hours from the start of the high-temperature oxidation reaction, the arsenic remaining in the liquid is reduced by a small amount, and the pH and liquid potential are hardly changed. In order to complete the high temperature oxidation reaction in a completely equilibrium state, it is preferably continued for 5 to 7 hours.

According to the crystallization step (7) according to the present invention described above, the reaction operation is simple, and there is no need for pH adjustment during the process, so that the contained arsenic can be reliably converted into scorodite (8) crystals. What is necessary is just to process the filtrate (11) to produce | generate at a waste_water | drain process process (12). The obtained scorodite (8) crystals are excellent in sedimentation and filterability, have low adhesion moisture of about 10% after filtration, and have an arsenic grade of 30%, so that volume reduction is achieved and Excellent elution and stable. Therefore, arsenic can be removed and stored in a stable form from the smelting process.

Example 1
In Example 1, elemental sulfur (S ⁰ ) was added at the beginning of the reaction in the first leaching step, and the effect of the addition was confirmed.

The raw material quality used in the examples will be described.
Table 1 shows the grade of the arsenic sulfide starch used in the examples, Table 2 shows the grade of the decoppered electrolytic slime, and Table 3 shows the blending ratio of the arsenic sulfide starch and the decoppered electrolytic slime.

In the formulation shown in Table 3 above, as described in (Equation 4), the amount of arsenic sulfide (As ₂ S ₃ ) in the arsenic sulfide starch sulfidizes copper (Cu ⁰ ) in the copper removal electrolytic slime. The equivalent of 0.5 times equivalent to the above. That is, it is a composition corresponding to the above-mentioned “when Cu ⁰ is abundant”.
(Cu ⁰ ) + 1 / 3As ₂ S ₃ + 1 / 2O ₂ + 1 / 3H ₂ O = 2 / 3HAsO ₂ + CuS (Formula 4)

That is, since the formulation and (Equation 4), of copper (Cu ⁰⁾ contained in the decoppered electrolytic slime, copper (Cu ⁰⁾ amount not sulfided is calculated to be 51.2 g. The unsulfurized copper will remain as copper ions at the end of leaching.

The amount of elemental sulfur (S ⁰ ) added is twice the total number of moles of remaining copper ions.
Double mole amount of elemental sulfur (S ⁰ ) = 51.2 ÷ M _Cu × M _S × 2 = 52 g
Here, the _{M Cu} is atomic weight 63.54 of copper, and _{M S} is the atomic weight 32.06 of S.

Arsenic sulfide starch, decoppered electrolytic slime and 52 g of reagent simple sulfur (S ⁰ ) shown in Tables 1 to 3 were measured in a 2 liter beaker, and predetermined pure water was added and repulped to prepare pulp. . In this preparation, if the amount of water contained in the raw material is taken into account, the amount of water in the pulp is 1,550 ml. The reaction was carried out at 800 rpm with a 2 liter beaker, 4 baffles, and 2 stage turbine blades.
And the said pulp was heated, stirring weakly, and the temperature was 80 degreeC. At this point, the pH was 1.62.

Next, blowing of oxygen gas at 430 cc / min was started from the bottom of the beaker using a glass tube, and stirring was performed at 800 rpm to start the reaction.
When 30 minutes had elapsed (80 ° C., pH 1.55), 26 ml of a 500 g / l sodium hydroxide solution was added over 5 minutes to 80 ° C. and pH 4.86. Thereafter, the reaction was continued, and after 120 minutes had elapsed (80 ° C., pH 1.85), the oxygen gas blowing was stopped, and stirring was further maintained for 30 minutes, and then leaching was completed (80 ° C., pH 1.72).

Table 4 shows the quality of the collected leachate. In Table 4, total-As indicates the total amount of arsenic, and pentavalent-As indicates the amount of pentavalent arsenic. The pentavalent-As ratio indicates the ratio of the pentavalent arsenic amount in the total amount of arsenic, and Cu indicates the copper concentration of the recovered leachate.

The recovered leaching residue was 501 wet · g (water content 50.2%), and the arsenic quality was 2.0%. From this, the leaching rate of arsenic was estimated to be about 93.5%, and the leaching rate was very high. Copper removal was also good.

Furthermore, the addition effect of elemental sulfur (S ⁰ ) was confirmed under the same conditions and procedures except that 2.5 moles of elemental sulfur (S ⁰ ) was added at the beginning of the reaction.
2.5 mole mol of elemental sulfur (S ⁰ ) = 51.2 ÷ M _Cu × M _S × 2.5 = 65 g
Arsenic sulfide starch, decopperized electrolytic slime and 65 g of reagent simple sulfur (S ⁰ ) shown in Tables 1 to 3 were measured in a 2 liter beaker and repulped with pure water to prepare a pulp.

First, the pulp was heated with weak stirring to a temperature of 80 ° C. At this point, the pH was 1.64.
Next, using a glass tube from the bottom of the beaker, oxygen gas was started to be blown at 430 cc / min, and the reaction was started with stirring at 800 rpm.
When 30 minutes had passed (80 ° C., pH 1.57), 26 ml of a 500 g / l sodium hydroxide solution was added over 5 minutes to 80 ° C. and pH 5.67. Thereafter, the reaction was continued, and after 120 minutes had elapsed (80 ° C., pH 1.93), the oxygen gas blowing was stopped, and stirring was continued for another 30 minutes, after which leaching was completed (80 ° C., pH 1.82).

Table 5 shows the quality of the collected leachate (leaching end point). In addition, the notation of a table | surface is the same as that of Table 4 mentioned above.

The collected leach residue was 520 wet · g (water content 48.9%), and the arsenic quality was 2.0%. From this, the leaching rate of arsenic was estimated to be about 93.2%, and the leaching rate was very high. Copper removal was also good.

Thereafter, in the same operation procedure, 0.4 times mole, 1.0 times mole and 1.3 times mole of elemental sulfur (S ⁰ ) are added at the beginning of the reaction with respect to the amount of remaining copper (Cu ⁰ ) Except for the above, the effect of adding elemental sulfur (S ⁰ ) was confirmed under the same conditions and procedures.
Table 6 shows the results of residual copper concentration when elemental sulfur was added at the beginning of the reaction under the above conditions.

From the above results, in order to reduce the residual copper concentration to 1 g / l or less, elemental sulfur (S ⁰ ) in an amount of 1.0 times mol or more, preferably 1.3 times mol or more of the total number of moles of remaining copper. Is understood to be added from the beginning of the reaction in the first leaching step.

(Example 2)
In Example 2, elemental sulfur (S ⁰ ) was added at the end of the reaction, which was the third step of leaching, and the effect of the addition was confirmed.

The arsenic sulfide starch and the decoppered electrolytic slime shown in the raw material preparation tables shown in Tables 1 to 3 of Example 1 were measured in a 2 liter beaker, and predetermined pulp was added to repulp to prepare a pulp. . The pulp was heated with weak agitation to bring the temperature to 80 ° C. At this point, the pH was 1.67.

Next, using a glass tube, 430 cc / min of oxygen gas was started from the bottom of the beaker, and the reaction was started with stirring at 800 rpm.
When 30 minutes had passed (80 ° C., pH 1.89), 26 ml of a 500 g / l sodium hydroxide solution was added over 5 minutes to 80 ° C. and pH 3.89. Thereafter, the reaction was continued, and oxygen blowing was stopped when 120 minutes had passed (80 ° C., pH 2.15).

As a result of a small amount of sampling, the amount of remaining copper was 3,750 mg / l. Therefore, after adding 65 g of simple sulfur (S ⁰ ) and stirring and mixing with the pulp for 10 minutes (80 ° C., pH 2.14), 95% sulfuric acid was added to lower the pH to 1.85 (80 ° C.). After stirring for 30 minutes, leaching was completed (80 ° C., pH 1.52).
Table 7 shows the quality of the collected leachate (leaching end point). In addition, the notation of a table | surface is the same as that of Table 4 mentioned above.

The recovered leaching residue was 552 wet · g (water content 48.6%), the arsenic quality was 2.7%, and the arsenic leaching rate was estimated to be about 90.2%. Although the leaching rate was lower than the method of adding elemental sulfur (S ⁰ ) from the beginning of leaching, the arsenic oxidation efficiency was remarkably improved. Specifically, Example 1 is a case where 65 g of simple sulfur (S ⁰ ) of the same amount as in this example was added at the beginning of the reaction in the first leaching process, but the ratio of pentavalent arsenic was 41.3%. there were. In comparison with this, in this example, the ratio of pentavalent arsenic was 83.3%, indicating an oxidation efficiency more than doubled.

Copper removal was also good. However, compared to the method of adding elemental sulfur (S ⁰ ) from the beginning of leaching shown in Example 1, Example 1 had higher copper removal capability.
Therefore, in order to make the residual copper concentration 1 g / l or less, it is preferable to add elemental sulfur (S ⁰ ) in an amount of 2.0 times or more the total number of moles of remaining copper.
However, by adding elemental sulfur (S ⁰ ) at the end of the reaction, which is the third step of leaching, an excess amount of copper ions can coexist in the leached pulp during the leaching step, so that the arsenic oxidation efficiency is increased. There is.

1,000 ml of the leachate prepared in Example 2 was placed in a 1 (L) beaker and hydrogen peroxide was added. The amount of hydrogen peroxide added is 1.05 times equivalent to the amount required to oxidize the trivalent arsenic. Specifically, 12.6 g of 30% H ₂ O ₂ water was added at the time when the temperature of the solution being raised reached 70 ° C., and the addition was completed in 10 minutes. The liquid potential at this time was 521 mV at 81 ° C. (in this example, the liquid potential is the Ag / AgCl electrode reference potential).

The oxidation reaction started from the end of the addition of hydrogen peroxide.
The oxidation reaction itself was completed in 60 minutes from the end of hydrogen peroxide addition. However, at this time, stirring was maintained for another 60 minutes so that the temperature did not fall below 80 ° C., and stirring was terminated after a total of 120 minutes had elapsed.
In addition, the said stirring was made into the intensity | strength of the grade which does not involve air. The liquid potential at the end of stirring was 378 mV at 81 ° C.

After completion of the reaction, the water was slightly evaporated and the amount of the liquid was reduced, so pure water was added to make 1000 ml before the reaction, and this was the final solution. The solution after adjusting the oxidizing solution was prepared by the above operation.

The amount of hydrogen peroxide remaining in the solution after the oxidation adjustment was examined. Specifically, 300 mg of copper powder was added to 50 ml of the post-oxidation-adjusted solution, and the mixture was allowed to react for 4 minutes at 40 ° C. with weak stirring that did not involve air, followed by filtration. A stirrer was used for stirring.
The copper concentration of the obtained filtrate was 281 mg / l, and an increase in concentration of about 22 mg / l was confirmed. From this result, it was confirmed that most of the residual hydrogen peroxide was decomposed and removed in the solution after oxidation adjustment.

The crystallization of arsenic contained in the post-oxidation adjusted solution will be described.
1) The solution after oxidation adjustment was diluted with pure water to adjust the arsenic concentration to 45 g / l.
2) 800 cc of the solution after oxidation adjustment with adjusted arsenic concentration was transferred to a 2 L beaker, and 95% sulfuric acid was added to adjust to pH 1.15.
3) 1.5 times the molar amount of ferrous iron (Fe ²⁺ ) contained in the oxidation-adjusted solution was added to the oxidation-adjusted solution. Specifically, 200 g of reagent grade ferrous sulfate (FeSO ₄ · 7H ₂ O) was weighed and dissolved in the adjusted solution, and 95% sulfuric acid was added to adjust the pH to 1.0 at 30 ° C. did.
4) Heat the solution of 3) above to 95 ° C., then start blowing oxygen gas at 400 cc / min from the bottom of the beaker using a glass tube, and in a gas-liquid mixed state for 7 hours under strong stirring High temperature oxidation reaction. The analysis results of the adjusted solution after the high temperature oxidation reaction are shown in Table 8 below.

The arsenic precipitation rate was 97.2%.
The arsenic precipitation rate is the conversion rate of arsenic in the solution to scorodite, and the elution method for obtaining the elution value was based on the Environmental Agency Notification No. 13 method. The liquid after the elution treatment was filtered through a filter made by MCE (Mixed Cellulose Ester) having a pore size of 0.2 μm.

(Comparative Example 1)
In this comparative example, arsenic leaching was measured when no elemental sulfur (S ⁰ ) was added in the leaching step.

The arsenic sulfide starch and the decoppered electrolytic slime shown in the raw material preparation tables shown in Tables 1 to 3 of Example 1 were measured in a 2 liter beaker, and predetermined pure water was added and repulped to prepare pulp. .
The pulp was heated with weak agitation to bring the temperature to 80 ° C. At this point, the pH was 1.71.

Using a glass tube, oxygen gas was started to be blown from the bottom of the beaker at 430 cc / min, and the reaction was started with stirring at 800 rpm. When 30 minutes have elapsed (80 ° C., pH 1.95), 26 ml of a 500 g / l sodium hydroxide solution (an amount corresponding to a Na concentration in the liquid corresponding to 4.8 g / l) is added over 5 minutes. The temperature was set to 80 ° C. and pH 3.70. Here, after sampling a small amount, the reaction was continued and oxygen blowing was stopped when 120 minutes had passed (80 ° C., pH 2.11). From here, stirring was further maintained for 30 minutes, and then leaching was completed (80 ° C., pH 2.07). Table 9 shows the quality of the recovered leachate immediately after the addition of the sodium hydroxide solution, and Table 10 shows the quality at the end of the leaching. In addition, the notation of a table | surface is the same as that of Table 4 mentioned above.

The recovered leaching residue was 529 wet · g (moisture 51.7%), and the arsenic quality was 14.9%. From this, the leaching rate of arsenic was estimated to be about 50.7%, and the leaching rate was very low.

In the comparative example 1, the inventors consider the following reasons for the very low arsenic leaching rate.
That is, in the formulation according to Comparative Example 1, an excessive amount of copper is present in the leachate, and arsenic oxidation is promoted. For this reason, it is considered that pentavalent arsenic and copper ions react to form copper arsenate during the leaching and remain as a residue. That is, it is considered that leaching to obtain an arsenic solution with a high leaching rate and a high concentration is impossible when the amount of copper is excessive as in Comparative Example 1.

(Comparative Example 2)
This comparative example is similar to Example 2, an example in which the pH of the reaction elemental sulfur (S ⁰⁾ after the addition was carried out in 2 or more.

The raw material blending / operation procedure was the same as in Example 2. Specifically, the same pulp as in Example 2 was similarly heated with weak stirring, and the temperature was set to 80 ° C. At this point, the pH was 1.61.
Next, blowing of 430 cc / min of oxygen gas was started from the bottom of the beaker using a glass tube, and the reaction was started with stirring at 800 rpm. When 30 minutes had passed (80 ° C., pH 1.85), 26 ml of a sodium hydroxide solution having a concentration of 500 g / l was added over 5 minutes to 80 ° C. and pH 3.80. Subsequently, the reaction was advanced and oxygen blowing was stopped when 120 minutes had passed (80 ° C., pH 2.12). After sampling a small amount (result: residual copper 3,849 mg / l), 65 g of elemental sulfur (S ⁰ ) was added, and after stirring and mixing with the pulp for 10 minutes (80 ° C., pH 2.11), stirring was further performed for 30 minutes. Maintained. Here (80 ° C., pH 2.09) a small amount of sampling (result: residual copper 3,566 mg / l), and further stirring was continued and after 30 minutes (80 ° C., pH 2.08), a small amount of sampling (result: residual) The leaching was completed with copper (429 mg / l).

From the above results, the pH is higher than that of Example 2 (pH is 2 or more), and in the region according to Comparative Example 2, the reactivity between elemental sulfur (S ⁰ ) and copper ions is very slow. There was found. Therefore, it was also found that copper removal was insufficient in the region according to Comparative Example 2.

Claims

A leaching step of oxidizing and leaching a mixed slurry of a non-ferrous smelting intermediate product containing sulfide form arsenic and a non-ferrous smelting intermediate product containing arsenic and metal form copper in an acidic region;
A liquid adjustment step of adding an oxidizing agent to the leachate to oxidize arsenic to pentavalent arsenic to obtain an adjusted liquid;
A crystallization step of converting the arsenic in the adjusted liquid into scorodite crystals,
In the leaching step, single sulfur (S 0 at the beginning of the reaction) is mixed into a mixed slurry of the non-ferrous smelting intermediate product containing arsenic in the sulfide form and the non-ferrous smelting intermediate product containing arsenic and copper in the metal form. ), Leaching first step of leaching at a temperature of 50 ° C. or higher and a pH of 1.0 or more and 2.0 or less while adding an oxidizing agent, and then after the pH is set to 2.0 or more The leaching second step of leaching while adding the oxidant to the mixed slurry, and then the leaching third step of stopping the addition of the oxidant and further stirring the mixed slurry, Processing method.
Wherein the amount of elemental sulfur (S 0) is the single body sulfur (S 0) 1 times mole or more of the total number of moles of copper remaining as ions leaching solution during when leached without the addition of The method for treating arsenic according to claim 1.
A leaching step of oxidizing and leaching a mixed slurry of a non-ferrous smelting intermediate product containing sulfide form arsenic and a non-ferrous smelting intermediate product containing arsenic and metal form copper in an acidic region;
A liquid adjustment step of adding an oxidizing agent to the leachate to oxidize arsenic to pentavalent arsenic to obtain an adjusted liquid;
A crystallization step of converting the arsenic in the adjusted liquid into scorodite crystals,
In the leaching step, the temperature of the non-ferrous smelting intermediate product containing the sulfide form of arsenic and the non-ferrous smelting intermediate product containing the arsenic and metal form of copper is increased while adding an oxidizing agent to the mixed slurry. First leaching step in which leaching is performed at a temperature of not less than 0 ° C. and a pH of 1.0 or more and 2.0 or less, and then leaching is performed by adding oxidant to the mixed slurry after the pH is set to 2.0 or more. Arsenic, characterized in that it has two steps and a third step of leaching after stopping addition of oxidant and adding elemental sulfur (S 0 ) to bring the pH to 2 or less and further stirring Processing method.
Wherein the amount of elemental sulfur (S 0) is the single body sulfur (S 0) 2-fold mole or more of the total number of moles of copper remaining as ions leaching solution during when leached without the addition of The method for treating arsenic according to claim 3.
A leaching step of oxidizing and leaching a mixed slurry of a non-ferrous smelting intermediate product containing sulfide form arsenic and a non-ferrous smelting intermediate product containing arsenic and metal form copper in an acidic region;
A liquid adjustment step of adding an oxidizing agent to the leachate to oxidize arsenic to pentavalent arsenic to obtain an adjusted liquid;
A crystallization step of converting the arsenic in the adjusted liquid into scorodite crystals,
In the leaching step, single sulfur (S 0 at the beginning of the reaction) is mixed into a mixed slurry of the non-ferrous smelting intermediate product containing arsenic in the sulfide form and the non-ferrous smelting intermediate product containing arsenic and copper in the metal form. ), Leaching first step in which leaching is performed while adding the oxidizing agent and the temperature is set to 50 ° C. or more, and the pH is set to 1.0 or more and 2.0 or less, and then the pH is set to 2.0 or more, The second step of leaching in which oxidant is added to the mixed slurry and then leaching is stopped, and then the addition of the oxidant is stopped and single sulfur (S 0 ) is added to bring the pH to 2 or less, followed by further stirring And a third step of leaching.
The non-ferrous smelting intermediate product containing arsenic and copper in a metal form is a decopperized electrolytic slime and / or a copper arsenide deposit, according to any one of claims 1 to 5, Processing method.
In the leaching step, after the leaching first step, the pH is set to 2.0 or more, and then the leaching second step is performed while adding the oxidant to the mixed slurry while maintaining the pH unretained. The method for treating arsenic according to claim 1. *
The method for treating arsenic according to any one of claims 1, 3, 5, and 7, wherein air and / or oxygen gas blowing is used as an oxidant added to the mixed slurry. *
In the liquid adjustment step, hydrogen peroxide is added as an oxidant at 40 ° C. or more, and after arsenic is oxidized to pentavalent arsenic to obtain an adjusted liquid, the post-reaction liquid and metal copper are brought into contact with each other to remain. The hydrogen peroxide remaining is removed, or the post-reaction liquid is further maintained by stirring to remove hydrogen peroxide remaining in the post-adjustment liquid. Arsenic treatment method. *
10. The crystallization process according to claim 1, wherein the crystallization process is a crystallization process in which ferrous ions coexist in the adjusted solution, and the ferrous ions are oxidized with pentavalent arsenic. A method for treating arsenic according to claim 1.
11. The arsenic treatment method according to claim 10, wherein the oxidation reaction is performed at a pH of 1 or less.
The arsenic treatment method according to claim 10, wherein the oxidation reaction is performed at a temperature of 50 ° C. or higher.