EQUIPMENT AND METHOD FOR LEACHING COPPER, AND METHOD FOR PRODUCING ELECTROLYTIC COPPER USING SAID EQUIPMENT AND METHOD

Abstract

Provided is a method for efficiently promoting a leaching reaction of copper. Equipment for leaching copper includes a reactor for leaching reaction and a controller for oxidation-reduction potential. The reactor is configured to be provided with a leaching solution containing iodine and iron. The reactor is configured to be capable of being tightly sealed during the leaching reaction. The controller for oxidation-reduction potential is configured so that, during the leaching reaction, the oxidation-reduction potential of the leaching solution can be maintained at 500 mV (based on Ag/AgCl reference) or higher.

Claims

1-6. (canceled)

7. Equipment for leaching copper, the equipment comprising a reactor for leaching reaction and a controller for oxidation-reduction potential, the reactor being configured to be provided with a leaching solution containing iodine and iron and being configured to be capable of being tightly sealed during the leaching reaction, the controller for oxidation-reduction potential being configured so that, during the leaching reaction, the oxidation-reduction potential of the leaching solution can be maintained at 500 mV (based on Ag/AgCl reference) or higher.

8. The equipment of claim 7, the equipment further comprising a pH controller, the pH controller being configured so that pH of the leaching solution can be controlled within a range from 1.0 to 2.0.

9. The equipment of claim 7, the reactor comprising a lid that is made from PTFE.

10. The equipment of claim 8, the reactor comprising a lid that is made from PTFE.

11. The method for leaching copper with use of the equipment of claim 7, the method comprising: introducing a substance containing copper and a leaching solution into the reactor; and proceeding the leaching reaction wherein the proceeding the leaching reaction includes proceeding the leaching reaction while the reactor is tightly sealed, and wherein the proceeding the leaching reaction includes maintaining oxidation-reduction potential of the leaching solution at 500 mV (based on Ag/AgCl reference) or higher.

12. The method of claim 11, wherein the proceeding the leaching reaction includes proceeding the leaching reaction under conditions of pH within a range from 1.0 to 2.0.

13. The method of producing electrolytic copper, the method comprising performing the method of claim 11.

14. The method of producing electrolytic copper, the method comprising performing the method of claim 12.

15. The method for leaching copper with use of the equipment of claim 8, the method comprising: introducing a substance containing copper and a leaching solution into the reactor; and proceeding the leaching reaction wherein the proceeding the leaching reaction includes proceeding the leaching reaction while the reactor is tightly sealed, and wherein the proceeding the leaching reaction includes maintaining oxidation-reduction potential of the leaching solution at 500 mV (based on Ag/AgCl reference) or higher.

16. The method for leaching copper with use of the equipment of claim 9, the method comprising: introducing a substance containing copper and a leaching solution into the reactor; and proceeding the leaching reaction wherein the proceeding the leaching reaction includes proceeding the leaching reaction while the reactor is tightly sealed, and wherein the proceeding the leaching reaction includes maintaining oxidation-reduction potential of the leaching solution at 500 mV (based on Ag/AgCl reference) or higher.

17. The method for leaching copper with use of the equipment of claim 10, the method comprising: introducing a substance containing copper and a leaching solution into the reactor; and proceeding the leaching reaction wherein the proceeding the leaching reaction includes proceeding the leaching reaction while the reactor is tightly sealed, and wherein the proceeding the leaching reaction includes maintaining oxidation-reduction potential of the leaching solution at 500 mV (based on Ag/AgCl reference) or higher.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0017] FIG. 1 shows equipment for leaching copper according to one embodiment of the present invention.

[0018] FIG. 2 shows the relation between oxidation-reduction potential and the rate of Cu extraction in one embodiment of the present invention. The vertical axis indicates the rate of Cu extraction, and the horizontal axis indicates days of leaching reaction.

[0019] FIG. 3 shows the relation between oxidation-reduction potential and the rate of Cu extraction in the case without iodine as a comparative example. The vertical axis indicates the rate of Cu extraction, and the horizontal axis indicates days of leaching reaction.

[0020] FIG. 4 shows the relation between the concentration of iodine and the rate of Cu extraction in one embodiment of the present invention. The vertical axis indicates the rate of Cu extraction, and the horizontal axis indicates days of leaching reaction.

[0021] FIG. 5 shows the relation between the temperature and the rate of Cu extraction in one embodiment of the present invention. The vertical axis indicates the rate of Cu extraction, and the horizontal axis indicates days of leaching reaction.

[0022] FIG. 6 shows the relation between pH and potential, in particular, the relation between pH (horizontal axis) and oxidation-reduction potential (vertical axis) and status of iodine. In the figure, the values for the resultant pH and ORP in the reactor that have been examined in Example 1 are plotted to be shown.

DETAILED DESCRIPTION OF THE INVENTION

[0023] More specified embodiments to practice the present invention are described hereinafter, which are not intended to limit the scope of the present invention, but are for the purpose of enhancing the understanding of the present invention.

1. Leaching Reaction that the Present Invention can be Applied to

[0024] In one embodiment, the present invention relates to equipment and method for leaching copper. Copper can be leached from ore containing copper. The term “ore” as used herein includes not only ore as raw materials, but also includes concentrate. Concentrate can be obtained by grinding stones as raw materials and/or by ore dressing (e.g., froth flotation).

[0025] Ore containing copper includes oxide ore, secondary copper sulfide ore, primary copper sulfide ore, etc. Examples of primary copper sulfide ore include, for example, bornite, chalcopyrite, etc. Equipment and method for leaching copper according to one embodiment of the present invention are preferable for chalcopyrite.

[0026] A leaching solution for leaching copper contains iodine (e.g., iodide ions) and iron (e.g., Fe ions (III)). These chemical elements react with a copper compound in ore to ionize copper and to cause leaching into the solution (a detail for reaction is described hereinafter).

[0027] The source of iron may be compounds such as iron sulfate n-hydrate (Fe.sub.2(SO.sub.4).sub.3.Math.nH.sub.2O). Alternatively, a solution of divalent iron ions (e.g., Iron (II) sulfide) may be supplied and then it may be converted to trivalent iron ions by Iron-oxidizing bacteria, etc.

[0028] The source of iodine may be an arbitrary form. For example, it may be supplemented in the form of elemental iodine molecule (which can be solubilized and converted into iodide ions), iodide (e.g., potassium iodide), etc.

[0029] Although the concentration of iodine in a leaching solution (i.e., the total concentration of iodine which includes any forms of iodine such as molecular iodine (I.sub.2), iodide ion (I.sup.−), triiodide ion (I.sub.3.sup.−), and the like) is not particularly limited, it may be at least 50 mg/L or more, preferably 100 mg/L or more, more preferably 150 mg/L or more. Although the upper limit is not particularly limited, it may be typically 300 mg/L or less.

[0030] Although the concentration of iron in a leaching solution (i.e., the total concentration of iron which includes any forms of iodine such as Fe ions (II), Fe ions (III), and the like) is not particularly limited, it may be at least 1 g/L or more, preferably 2 g/L or more, more preferably 5 g/L or more. Although the upper limit is not particularly limited, it may be typically 10 g/L or less.

[0031] A leaching solution may contain any ingredients other than iodine and iron. For example, as a result of adjusting oxidation-reduction potential described hereinafter, a leaching solution may contain oxidizing agent and/or reducing agents, and furthermore, it may contain a resultant substance caused from their reaction. In another example, as a result of adjusting pH described hereinafter, a leaching solution may contain H.sup.+ ions, OH.sup.− ions, and/or their counterions.

[0032] In equipment and methods according to one embodiment of the present invention, there is no need to add, to a leaching solution, nitric acid ions and nitrous acid ions as shown in Patent Literature 2, etc.

[0033] Hereinafter, referring to chalcopyrite as an example, equipment and methods for leaching copper are described.

2. Equipment for Leaching Copper from Copper Ore

[0034] FIG. 1 shows conceptual equipment for leaching copper. Equipment includes at least a reactor 90 for leaching reaction and a controller 10 for oxidation-reduction potential (ORP).

[0035] (2-1. Reactor for Leaching Reaction)

[0036] A reactor for leaching reaction is a place where copper leaching reaction occurs. As shown in an example according to FIG. 1, the reactor 90 may include a jacket. Furthermore, the reactor 90 may have a sealable structure to prevent gas from flowing into and out of the reactor 90 during leaching reaction. Thereby, loss of iodine due to volatilization of iodine may be prevented. In addition, a material for the reactor 90 is preferably glass, or a material of glass lining (which is covered by glass material), or PTFE (Poly Tetra Fluoro Ethylene) in view of sealability and reactivity with iodine. The reactor 90 may include the lid 70 in its upper side to achieve sealability. As similar to a material for the reactor 90, a material for the lid 70 is preferably glass, or a material of glass lining (which is covered by glass material), or PTFE, and especially a material for parts of lid 70 that contact with the reactor 90 is preferably PTFE.

[0037] The reactor 90 is configured to be supplied with a leaching solution containing iodine and iron. Iodine and iron may be converted into an arbitrary form due to leaching reaction described hereinafter, etc. For example, iodine may be converted into the forms of iodine molecules (I.sub.2), iodide ions (I.sup.−), triiodide ions (I.sub.3.sup.−), etc. Iron may be converted into the forms of Fe ions (II), Fe ions (III), etc.

[0038] Although not shown in Figures, equipment may include a member of supplying a leaching solution to provide a leaching solution to the reactor 90. Although specified structure for the member of supplying a leaching solution is not particularly limited, it may include, for example, a pipe and a tank to provide a leaching solution, and optionally, a controller for control of supplying a leaching solution.

[0039] In order to agitate a leaching solution inside the reactor 90, equipment may include agitating equipment 50. A material for impeller parts in the agitating equipment 50 is preferably PTFE. In addition to this, in order to adjust an amount of liquid, etc., equipment may include a water bath 100 and a pump 110 for supplying liquid.

[0040] (2-2. Controller for Oxidation-Reduction Potential)

[0041] The controller 10 for oxidation-reduction potential (ORP) adjusts oxidation-reduction potential in a leaching solution during leaching reaction. For the purpose of this, equipment may have the ORP electrode 60 and the tank for oxidizing agent 20. The controller for oxidation-reduction potential may control an amount of oxidizing agent supplied from the tank 20 for oxidizing agent on the basis of oxidation-reduction potential of a leaching solution that has been determined by the ORP electrode. Although the controller 10 for oxidation-reduction potential (ORP) may control oxidation-reduction potential to an arbitrary value, in order to promote a good copper leaching reaction, the value of oxidation-reduction potential is maintained to 500 mV (based on Ag/AgCl reference) or higher. The value of oxidation-reduction potential is preferably 520 mV or higher, and more preferably 540 mV or higher. The upper limit may be, though not particularly limited, typically 700 mV or less.

[0042] (2-3. Controller for pH)

[0043] In addition to the reactor 90 for leaching reaction, and the controller 10 for oxidation-reduction potential, etc., equipment may further include a controller 10 for pH. The controller 10 for pH adjusts pH in a leaching solution during leaching reaction. For the purpose of this, equipment may include the pH electrode 40 and the tank 30 for pH adjuster. The controller 10 of pH may control an amount of pH adjuster supplied from the tank 30 for pH adjuster on the basis of pH of a leaching solution that has been determined by the pH electrode 40. Preferably, the tank 30 for pH adjuster may accommodate an acidic pH adjuster and a basic pH adjuster. Although the controller 10 for pH may control pH to an arbitrary value, in order to promote a good copper leaching reaction, the value of pH is preferably controlled within a range from 1.0 to 2.0, more preferably, from 1.3 to 1.7. The controller 10 for pH may exist separately from the above-stated controller for the oxidation-reduction potential, alternatively, the controller 10 for pH may be integrated with the above-stated controller for oxidation-reduction potential as shown in FIG. 1.

3. Method for Leaching Copper from Copper Ore

[0044] Utilizing the above-stated equipment, copper can be leached. More specifically, the method for leaching copper includes the following steps. [0045] introducing a substance containing copper and a leaching solution into a reactor; and [0046] proceeding leaching reaction.

[0047] A detail for each of the steps is described hereinafter.

[0048] (3-1. Step of Introducing a Substance Containing Copper and a Leaching Solution into a Reactor)

[0049] As stated above, equipment includes the reactor 90 for leaching reaction. A substance containing copper and a leaching solution are introduced into the reactor 90. The substance containing copper may be ore containing copper as stated above. The leaching solution contains iodine and iron as stated above.

[0050] (3-2. Step of Proceeding Leaching Reaction)

Although the following description is not intended to limit the scope of the present invention, leaching proceeds for example, according to a series of the catalytic reaction by iodine as shown in the following Formula I and Formula II.

2I.sup.−+2Fe.sup.3+.fwdarw.I.sub.2+2Fe.sup.2+  (Formula I)

CuFeS.sub.2+I.sub.2+2Fe.sup.3+.fwdarw.Cu.sup.2++3Fe.sup.2++2S+2I.sup.−  (Formula II)

[0051] Furthermore, in the reaction of Formula II, copper sulfide ore is oxidized by Fe (III) ions and by iodine (I.sub.2) which is generated via the reaction of Formula I to generate copper ions (Cu.sup.2+). In addition, the above triiodide ions (I.sub.3.sup.−) also contribute to the reaction of Formula II as a catalyst as similar to iodine (I.sub.2).

[0052] The step of proceeding leaching reaction includes sealing the reactor 90 for proceeding leaching reaction. For example, after introducing the substance containing copper and the leaching solution, the lid 70 may be mounted on the reactor 90 to seal the reactor 90.

[0053] The step of proceeding leaching reaction includes maintaining oxidation-reduction potential of the leaching solution at 500 mV (based on Ag/AgCl reference) or higher. By maintaining oxidation-reduction potential of the leaching solution at 500 mV (based on Ag/AgCl reference) or higher, triiodide ion (I.sub.3.sup.−), which contributes as a catalyst during leaching, can stably exist, and as a result, an amount of leaching increases. The value of oxidation-reduction potential is preferably 520 mV or higher, and more preferably 540 mV or higher. The upper limit may be, though not particularly limited, typically 700 mV or less.

[0054] When maintaining oxidation-reduction potential, oxidizing agent can be used. Although not particularly limited, oxidizing agent to be used may be, for example, potassium permanganate, etc.

[0055] The step of proceeding leaching reaction may include proceeding leaching reaction at pH within a range from 1.0 to 2.0. By maintaining the range, leaching reaction can proceed preferably and an amount of triiodide ion (I.sub.3.sup.−), which contributes as a catalyst during leaching, increases. A range of pH is more preferably from 1.3 to 1.7.

[0056] A type of pH adjuster is not particularly limited and a typical type of pH adjuster in the art may be used. For example, an acidic pH adjuster may include sulfuric acid (H.sub.2SO.sub.4), chloric acid (HCl), etc. For example, a basic pH adjuster may include sodium hydroxide (NaOH), potassium hydroxide (KOH), etc.

[0057] Temperature for proceeding leaching reaction is also not particularly limited and may be ambient temperature or more (e.g., 25 degrees C. or more), 30 degrees C. or more, or 35 degrees C. or more. In general, reaction proceeds better at the higher temperature. Although the upper limit is not particularly limited, it is typically 60 degrees C. or less because reaction in proportion to high temperature reaches a plateau.

[0058] Time for leaching reaction is also not particularly limited and may be 168 hours or more, or 336 hours or more. Although the upper limit is not particularly limited, it is typically 514 hours or less because reaction for a too long time reaches a plateau.

[0059] An important point for proceeding leaching reaction preferably is that while the reactor 90 is sealed, oxidation-reduction potential in a leaching solution is maintained to a certain value or more. As stated above, an increase of oxidation-reduction potential in a leaching solution theoretically leads to preferable proceed of a leaching reaction, but in practice, iodine volatilizes and its amount decreases with time. With a decrease of the amount of iodine, the rate of leaching reaction decreases. However, sealing the reactor 90 prevents iodine from volatilizing. Thus, a decrease of the rate of leaching reaction due to iodine volatilization can be prevented.

4. Method of Producing Electrolytic Copper

[0060] In one embodiment, the present invention relates to a method of producing electrolytic copper. The method may include at least performing the above-stated steps. Via these steps, a post-leaching solution of copper can be obtained. From the obtained post-leaching solution, copper ions can be selectively recovered and concentrated by Solvent Extraction (SX). Then, from the concentrated copper solution, electrolytic copper can be produced by Electrowinning (EW).

EXAMPLES

[0061] Hereinafter, via the following working examples, the above-described embodiments of the present invention are described more specifically, although the scope of the present invention is not limited to the following working examples.

5. Example 1 (Oxidation-Reduction Potential)

[0062] Next, the relation between oxidation-reduction potential and the rate of Cu extraction was examined. One liter of an aqua acidic solution of sulfuric acid and 2 grams of copper concentrate which primarily contains chalcopyrite were introduced into a reactor. The concentration of iron in the aqua acidic solution of sulfuric acid was 5 g/L. The source of iron was iron(II) sulfate (Fe(II)) and iron(III) sulfate (Fe(III)). Incidentally, the amounts of these sources of iron to be added were set as shown in Table 1 for the purpose of setting desired oxidation-reduction potential.

TABLE-US-00001 TABLE 1 oxidation-reduction potential Fe.sup.3+ Fe.sup.2+ (mV vs Ag/AgCl) (g/L) (g/L) 570 4.900 0.100 545 4.750 0.250 526 4.500 0.500 515 4.286 0.714 505 4.000 1.000 470 2.500 2.500

[0063] The concentration of iodine in the aqua acidic solution of sulfuric acid was 150 mg/L. The pH of the solution was controlled to 1.5 with use of sulfuric acid. The temperature was maintained at 25 degrees C. Samples were taken with an amount of about 3 mL from the reactor and were subjected to a filter with a 0.2-micrometer pore size, and the concentration of copper in the solution was analyzed by ICP-OES (SPS7700, SEIKO inc). Potassium permanganate was used for controlling oxidation-reduction potential (ORP).

[0064] The change of the rate of Cu extraction with the change of controlled ORP from 470 mV to 570 mV was determined. The result is shown in FIG. 2. When oxidation-reduction potential was controlled to 470 mV, the rate of Cu extraction was 20%. However, when oxidation-reduction potential was controlled to 500 mV or more, the rate of Cu extraction was above 50%. Further, when oxidation-reduction potential was controlled to 526 mV or more, the rate of Cu extraction was above 90%.

6. Comparative Example

[0065] Iodine was not added and ORP to be controlled was set to two values (470 mV and 570 mV). The other conditions were the same as those of Example 2. The result is shown in FIG. 3. In any oxidation-reduction potential, the rate of Cu extraction was 10%.

7. Example 2 (the Concentration of Iodine)

[0066] The concentration of iodine was changed in a range from 0 to 200 mg/L. ORP was controlled to 570 mV. The other conditions were the same as those of Example 1. The result is shown in FIG. 4. At the concentration of 100 mg/L or more, the rate of Cu extraction was nearly 100%.

8. Example 3 (Temperature)

[0067] The concentration of iodine was set to 150 mg/L. ORP to be controlled was set to two values (470 mV and 570 mV). The temperature was changed within a range from 25 degrees C. to 45 degrees C. The other conditions were the same as those of Example 1. The result is shown in FIG. 5. In the case where ORP was 570 mV, the higher temperature promoted better Cu leaching. In the case where ORP was 470 mV, even if the temperature was set to 45 degrees C., the rate of Cu extraction was only 40%.

9. Supplementary Example (Oxidation-Reduction Potential and Ionic Forms of Iodine)

[0068] FIG. 6 shows the status of iodine in a solution when oxidation-reduction potential and pH change. In this figure, the values for potential and pH in the reactor determined in Example 2 were plotted.

[0069] Approximately at pH 1.5, when oxidation-reduction potential was above 500 mV, the form of ions was triiodide ion (I.sub.3.sup.−), from which the reaction according to the above-stated Formula II was assumed to be promoted under co-existence with chalcopyrite.

[0070] The detailed embodiments of the present invention have been described. The above embodiments are merely an example of the present invention, and the present invention is not limited to the above embodiments. For example, a technical feature disclosed in one embodiment may be applied to another embodiment. Furthermore, regarding a method or process, the order of some steps may be switched from other steps unless otherwise noted. Also, a further step may be inserted among certain two steps. The scope of the present invention is defined by the appended claim.

DESCRIPTION OF REFERENCE NUMERALS

[0071] 10 Controller for pH and ORP [0072] 20 Tank for oxidizing agent [0073] 30 Tank for pH adjuster [0074] 40 pH electrode [0075] 50 agitating equipment and mixing impeller [0076] 60 ORP electrode [0077] 70 Lid [0078] 80 Metering pump [0079] 90 Reactor [0080] 100 Water bath [0081] 110 Pump for supplying liquid