System for efficiently producing cathode copper through combination of copper sulfide concentrate and copper oxide concentrate

Abstract

The invention discloses a system for efficiently producing cathode copper through combination of copper sulfide concentrate and copper oxide concentrate. The system comprises a copper sulfide concentrate system (1), a copper oxide concentrate system and a copper sulfide concentrate system (2). The copper sulfide concentrate system (1) is roasting, electrodeposition mixed liquid leaching and electrodeposition; the copper oxide concentrate system is subjected to raffinate leaching-extraction-electrodeposition; and the leaching mode of the copper sulfide concentrate system (2) can be flexibly adjusted, an electrodeposition mixed solution in the copper sulfide concentrate system (1) or a raffinate in the copper oxide concentrate system is selectively adopted for leaching, and ore pulp obtained after leaching is merged into the copper sulfide concentrate system (1) or the copper oxide concentrate system. By flexibly adjusting the leaching mode of the copper sulfide concentrate system (2), the treatment amount of the copper sulfide concentrate and the copper oxide concentrate and the supply and demand balance of electrodeposition production of cathode copper are achieved, meanwhile, stable and efficient production of the leaching-electrodeposition system and the extraction-electrodeposition system is achieved, and the system does not have the problem of water expansion.

Description

Technical Field

[0001] The present invention relates to the technical field of hydrometallurgy of copper-cobalt ore, and in particular, to a system for jointly and efficiently producing cathode copper from copper sulfide concentrate and copper oxide concentrate. Background Art

[0002] The rich copper-cobalt mineral resources in the Democratic Republic of the Congo (DRC) have attracted a large number of mining enterprises at home and abroad to carry out resource development. The hydrometallurgy technology, with its advantages of being able to efficiently recover copper and cobalt metal resources simultaneously and having a low dependence on the stable supply of the power system, is widely used in mining enterprises in the DRC.

[0003] With the increasing intensity of ore mining and the increasing mining depth in recent years, copper-cobalt ores have gradually transitioned from oxidized ores to sulfur-oxygen mixed ores. Sulfur-oxygen mixed ores can produce products such as copper sulfide concentrate and copper oxide concentrate through the beneficiation flotation process. Copper oxide concentrate can be directly used in the classical leaching-extraction-electrowinning process to produce cathode copper, and the in-situ smelting treatment process of copper sulfide concentrate needs to be further optimized.

[0004] The hydrometallurgical treatment process of copper sulfide concentrate includes oxygen pressure leaching, bioleaching, roasting leaching, etc. Chinese Patent CN 111225988A uses the oxygen pressure leaching method for copper sulfide concentrate, which has high requirements for reaction temperature, reaction equipment, etc. At the same time, the iron leaching rate in the solution increases, and the leaching solution needs to be de-ironed. The system generates acid swelling and requires additional acid neutralization, resulting in high production costs and poor economic benefits. Chinese Patent CN 105969695 B introduces a method for preparing a composite ore-leaching bacterium for copper sulfide ore to improve the reaction rate and leaching rate. Although it can successfully leach copper from copper sulfide ore, for large-scale industrial production enterprises, its leaching rate is still difficult to guarantee. Secondly, bioleaching will produce some complex waste, which needs to be treated in time to reduce the impact on the environment. Roasting leaching is widely used in the Democratic Republic of the Congo due to its high copper and cobalt recovery rates and its suitability for large-scale industrial production. The traditional roasting-leaching-electrowinning process has not been widely promoted due to its disadvantages such as impurity enrichment in the system, inability to guarantee the quality of cathode copper products when the leaching solution directly enters the electrowinning production, etc. At present, the main production process of copper sulfide concentrate in most enterprises in the Democratic Republic of the Congo is roasting-leaching-extraction-electrowinning, but this process also has disadvantages such as a long process flow and unremarkable economic benefits. In the method for co-smelting copper sulfide concentrate and copper oxide concentrate to produce cathode copper, the advantages of the short process flow and good economic benefits of the roasting-leaching-electrowinning process of copper sulfide concentrate are fully utilized. A production system is formed by combining copper sulfide concentrate and copper oxide concentrate, which successfully solves most of the problems in the production of high-quality cathode copper products by the traditional copper sulfide concentrate using the roasting-leaching-electrowinning process. However, the roasting-leaching-electrowinning system of copper sulfide concentrate continuously opens the circuit to the solution of the leaching-extraction-electrowinning system of copper oxide concentrate, greatly increasing the water treatment pressure of the extraction-electrowinning system. Especially during the period of heavy rainfall, it is extremely easy to cause water swelling problems, affecting the normal and stable production of the system. Summary of the Invention

[0005] The present invention provides a system for jointly and efficiently producing cathode copper from copper sulfide concentrate and copper oxide concentrate to solve the technical problem that the solution in the copper sulfide concentrate production system is opened to the extraction-electrowinning system of copper oxide concentrate, which is prone to cause water swelling. At the same time, the present invention enables the treatment amounts of copper sulfide concentrate and copper oxide concentrate to be flexibly adjusted and cooperate with each other to achieve the supply-demand balance between the treatment amounts of copper sulfide concentrate and copper oxide concentrate and the production of cathode copper by multiple electrowinning systems, and at the same time realizes the stable and efficient production of the leaching-electrowinning system and the extraction-electrowinning system.

[0006] According to one aspect of the present invention, there is provided a system for jointly and efficiently producing cathode copper from copper sulfide concentrate and copper oxide concentrate, including copper sulfide concentrate system ①, copper sulfide concentrate system ② and copper oxide concentrate system;

[0007] The copper sulfide concentrate system ① includes a roasting - leaching - electrowinning process. The copper sulfide concentrate is roasted to form calcine, which is leached using the electrowinning mixed solution. After leaching, solid - liquid separation is carried out to obtain thickened underflow ① and thickened overflow ①. The thickened overflow ① enters the electrowinning rich - liquid pool and is used to produce cathode copper by electrowinning, and then is converted into electrowinning lean liquid. The electrowinning rich liquid and the electrowinning lean liquid are mixed to obtain the electrowinning mixed solution, which is returned to the leaching process of the copper sulfide concentrate system ①. The thickened underflow ① is then stacked after pressure filtration and washing;

[0008] The copper oxide concentrate system includes a leaching - extraction - electrowinning process. The copper oxide concentrate is leached using the raffinate. After leaching, solid - liquid separation is carried out to obtain thickened underflow ② and thickened overflow ②. The thickened overflow ② is used for the extraction - electrowinning production of cathode copper. Part of the raffinate is returned to the leaching process, and part enters the cobalt recovery system. The thickened underflow ② is then stacked after pressure filtration and washing;

[0009] The copper sulfide concentrate system ② can be incorporated into the copper sulfide concentrate system ① or the copper oxide concentrate system by flexibly selecting the leaching method. When incorporated into the copper sulfide concentrate system ①, after the copper sulfide concentrate is roasted, it is leached using the electrowinning mixed solution, and the leaching pulp is directly incorporated into the thickening and clarification process of the copper sulfide concentrate system ①. When incorporated into the copper oxide concentrate system, after the copper sulfide concentrate is roasted, it is leached using the raffinate, and the leaching pulp is incorporated into the leaching process of the copper oxide concentrate.

[0010] Furthermore, a valve ① is provided on the pipeline through which the electrowinning mixed solution enters the leaching process of the copper sulfide concentrate system ①, and a valve ② is provided on the pipeline through which the electrowinning mixed solution enters the leaching process of the copper sulfide concentrate system ②; a valve ③ is provided on the pipeline through which the pulp after leaching in the copper sulfide concentrate system ② enters the thickening and clarification process of the copper sulfide concentrate system ①, and a valve ④ is provided on the pipeline through which the pulp after leaching in the copper sulfide concentrate system ② enters the leaching process of the copper oxide concentrate system; a valve ⑤ is provided on the pipeline through which the raffinate in the copper oxide concentrate system enters the leaching process of the copper sulfide concentrate system ②;

[0011] When the copper sulfide concentrate system ① is leached using the electrowinning mixed solution, valve ① is in the open state;

[0012] When the copper sulfide concentrate system ② is leached using the electrowinning mixed solution, valve ② is opened and valve ⑤ is closed. The electrowinning mixed solution enters the leaching process of the copper sulfide concentrate system ②. After the reaction is completed, valve ③ is opened, and at the same time valve ④ is closed. The pulp after leaching is incorporated into the copper sulfide concentrate system ①.

[0013] Furthermore, when the copper sulfide concentrate system ② is leached using the raffinate in the copper oxide concentrate system, valve ② is closed and valve ⑤ is opened. The raffinate enters the leaching process of the copper sulfide concentrate system ②. After the reaction is completed, valve ③ is closed, and at the same time valve ④ is opened. The pulp after leaching is incorporated into the leaching process of the copper oxide concentrate system.

[0014] Further, the thick underflow ① undergoes a pressure filtration and washing process to obtain filtrate ① and roasted ore leaching residue, and the filtrate ① flows into the leaching process in the copper oxide concentrate system.

[0015] Further, the thick underflow ② undergoes a pressure filtration and washing process to obtain filter cake and filtrate ②, and the filtrate ② flows into the leaching process in the copper oxide concentrate system.

[0016] Further, the copper concentration in the electrowinning mixed solution is 40 - 75 g / L, and the copper acid concentration and

[0017] Where:

[0018] ——Copper ion concentration;

[0019] ——Relative molecular mass of sulfuric acid;

[0020] Mr (Cu) ——Relative atomic mass of Cu;

[0021] ——Sulfuric acid concentration.

[0022] Further, sulfuric acid and neutral water are also added in the leaching process of the copper sulfide concentrate system ① to maintain the copper acid concentration and

[0023] Further, the concentration of the leaching pulp in the copper sulfide concentrate system ① is 4% - 8%, the reaction temperature is 40°C - 80°C, the reaction time is 5 - 9 h, and the copper concentration at the reaction end point is 60 g / L - 110 g / L.

[0024] Further, when leaching the roasted ore in the copper sulfide concentrate system ② with the electrowinning mixed solution, the leaching conditions are the same as those in the copper sulfide concentrate system ①; when using the raffinate for leaching, the concentration of the leaching pulp is 4% - 8%, the reaction temperature is 25 - 80°C, and the reaction time is 5 - 9 h.

[0025] The copper sulfide concentrate system ② uses the raffinate for leaching. After the leached pulp is incorporated into the leaching process of the copper oxide concentrate system, the raffinate and sulfuric acid are replenished simultaneously to make the reaction liquid - solid ratio 4 - 10, and the pH value at the reaction end point is 1.2 - 1.8.

[0026] The present invention has the following beneficial effects:

[0027] (1) The copper supply amounts of the upstream copper sulfide concentrate and copper oxide concentrate in the present invention can be flexibly adjusted according to the copper demand amounts of the downstream leaching - electrowinning system and extraction - electrowinning system process requirements, maintaining the efficient and stable production of the entire system:

[0028] When the grade or throughput of the copper sulfide concentrate system ① decreases and the copper supply from the copper sulfide concentrate system ① is difficult to meet the production demand of the leaching-electrowinning system, the copper sulfide concentrate system ② can selectively use the electrowinning mixed solution for leaching to ensure the copper supply of the system and maintain stable and efficient electrowinning production. When the grade or throughput of the copper oxide concentrate decreases and the copper supply from the copper oxide concentrate is difficult to meet the production demand of the extraction-electrowinning system, the copper sulfide concentrate system ② can selectively use the raffinate for leaching to ensure the copper supply of the system and maintain stable and efficient electrowinning production.

[0029] When the copper sulfide concentrate system ② is incorporated into the copper sulfide concentrate system ①, the copper concentration in the solution pool of the leaching-electrowinning system increases, which can increase the copper inventory in the solution of the leaching-electrowinning system. The dependence of the downstream electrowinning production of the leaching-electrowinning system on the copper leached from the upstream ore treatment weakens, and the fluctuations in the upstream ore will not affect the operation of the electrowinning production. The anti-interference ability of the system is enhanced, ensuring stable production of the leaching-electrowinning process.

[0030] When the copper sulfide concentrate system ② is incorporated into the copper oxide concentrate system, the copper concentration in the pre-extraction solution of the copper oxide concentrate system increases, which can increase the copper inventory in the solution of the extraction-electrowinning system. The dependence of the downstream electrowinning production of the extraction-electrowinning system on the copper leached from the upstream ore treatment weakens, and the fluctuations in the upstream ore will not affect the operation of the electrowinning production. The anti-interference ability of the system is enhanced, ensuring stable production of the extraction-electrowinning system.

[0031] (2) By flexibly adjusting the leaching method of the copper sulfide concentrate system ②, the present invention can achieve the effect that the downstream electrowinning workshop can still produce cathode copper products efficiently under the conditions of changes in the throughput or grade of the upstream copper sulfide concentrate and copper oxide concentrate. At the same time, in this system, the open-circuit volume of the solution and the externally added fresh water volume are small, and problems such as water swelling will not occur, and the economic benefits are good.

[0032] In addition to the purposes, features and advantages described above, the present invention has other purposes, features and advantages. The present invention will be further described in detail below with reference to the drawings. BRIEF DESCRIPTION OF THE DRAWINGS

[0033] The drawings forming a part of this application are used to provide a further understanding of the present invention. The schematic embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation of the present invention. In the drawings:

[0034] Figure 1 is a schematic process flow diagram of the system of the present invention.

[0035] Figure 2 is a schematic process flow diagram in Comparative Example 1 of the present invention. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0036] The embodiments of the present invention will be described in detail below in conjunction with the accompanying drawings. However, the present invention can be implemented in many different ways defined and covered by the following.

[0037] Referring to Figure 1 , an embodiment of the first aspect of the present invention provides a system for the combined and efficient production of cathode copper from copper sulfide concentrate and copper oxide concentrate, including a copper sulfide concentrate system ①, a copper oxide concentrate system, and a copper sulfide concentrate system ②;

[0038] The copper sulfide concentrate system ① includes a roasting - leaching - electrowinning process. The copper sulfide concentrate is roasted to form roasted ore, which is leached with an electrowinning mixed solution. After leaching, solid - liquid separation is carried out to obtain thickened underflow ① and thickened overflow ①. The thickened overflow ① enters the electrowinning rich liquid pool and is used for electrowinning to produce cathode copper and is converted into electrowinning lean liquid. The electrowinning rich liquid and the electrowinning lean liquid are mixed to obtain an electrowinning mixed solution, which is returned to the leaching process of the copper sulfide concentrate system ①. The thickened underflow ① is then filtered and washed and stacked;

[0039] The copper oxide concentrate system includes a leaching - extraction - electrowinning process. The copper oxide concentrate is leached with the raffinate. After leaching, solid - liquid separation is carried out to obtain thickened underflow ② and thickened overflow ②. The thickened overflow ② is used for extraction - electrowinning to produce cathode copper. Part of the raffinate is returned to the leaching process, and part enters the cobalt recovery system. The thickened underflow ② is then filtered and washed and stacked;

[0040] The copper sulfide concentrate system ② can be incorporated into the copper sulfide concentrate system ① or the copper oxide concentrate system by flexibly selecting the leaching method. When incorporated into the copper sulfide concentrate system ①, after the copper sulfide concentrate is roasted, it is leached with the electrowinning mixed solution, and the leaching pulp is directly incorporated into the thickening and clarification process of the copper sulfide concentrate system ①. When incorporated into the copper oxide concentrate system, after the copper sulfide concentrate is roasted, it is leached with the raffinate, and the leaching pulp is incorporated into the leaching process of the copper oxide concentrate.

[0041] This application is applicable to a hydrometallurgical system for simultaneously treating copper sulfide concentrate and copper oxide concentrate, which at least includes two independent copper sulfide concentrate roasting systems. The roasting process can be one or more of oxidation roasting, semi - oxidation roasting, and sulfation roasting, converting the copper in the copper sulfide concentrate into metal oxides or sulfates that are easily acid - leached.

[0042] The roasted ore produced by the copper sulfide concentrate system ① is only leached with the electrowinning mixed solution. The leached solution enters the electrowinning rich liquid pool and is used for electrowinning to produce cathode copper products. The roasted ore produced by the copper sulfide concentrate system ② can be selectively leached with the electrowinning mixed solution, and the obtained leaching pulp is incorporated into the thickening and clarification process of the copper sulfide concentrate system ①; or leached with the raffinate, and the obtained leaching pulp is incorporated into the leaching - extraction - electrowinning production process of the copper oxide concentrate to produce cathode copper.

[0043] The copper supply of copper sulfide concentrate and copper oxide concentrate upstream of the present invention can be flexibly adjusted according to the copper demand of the downstream leaching-electrowinning system and solvent extraction-electrowinning system processes, so as to maintain the efficient and stable production of the whole system:

[0044] When the grade or throughput of the copper sulfide concentrate system ① decreases, and the copper supply of the copper sulfide concentrate system ① is difficult to meet the production demand of the leaching-electrowinning system, the copper sulfide concentrate system ② can selectively adopt electrowinning mixed solution leaching to ensure the copper supply of the system and maintain the stable and efficient production of electrowinning; when the grade or throughput of the copper oxide concentrate decreases, and the copper supply of the copper oxide concentrate is difficult to meet the production demand of the solvent extraction-electrowinning system, the copper sulfide concentrate system ② can selectively adopt raffinate leaching to ensure the copper supply of the system and maintain the stable and efficient production of electrowinning.

[0045] When the copper sulfide concentrate system ② is incorporated into the copper sulfide concentrate system ①, the copper concentration in the solution pool of the leaching-electrowinning system increases, which can increase the copper storage amount in the solution of the leaching-electrowinning system. The dependence of the downstream electrowinning production of the leaching-electrowinning system on the leached copper from the upstream ore treatment weakens, and the fluctuation of the upstream ore will not affect the operation of electrowinning production, the anti-interference ability of the system is enhanced, and the stable production of the leaching-electrowinning process is ensured;

[0046] When the copper sulfide concentrate system ② is incorporated into the copper oxide concentrate system, the copper concentration in the pre-extraction solution of the copper oxide concentrate system increases, which can increase the copper storage amount in the solution of the solvent extraction-electrowinning system. The dependence of the downstream electrowinning production of the solvent extraction-electrowinning system on the leached copper from the upstream ore treatment weakens, and the fluctuation of the upstream ore will not affect the operation of electrowinning production, the anti-interference ability of the system is enhanced, and the stable production of the solvent extraction-electrowinning system is ensured.

[0047] The present invention realizes the effect that the downstream electrowinning workshop can still efficiently produce cathode copper products under the conditions of changes in the throughput or grade of the upstream copper sulfide concentrate and copper oxide concentrate by flexibly adjusting the leaching method of the copper sulfide concentrate system ②. At the same time, in this system, if the copper demand of the copper oxide concentrate system increases, the copper sulfide concentrate ② can be converted into raffinate leaching, and the directly leached copper amount of the ore increases, without the need for solution open circuit; if the open-circuit solution amount from the leaching-electrowinning system to the solvent extraction-electrowinning system is small, the amount of supplementary neutral water and sulfuric acid is also small, and the solution is relatively stable. Therefore, the open-circuit solution amount and the externally added new water amount are small, and problems such as water swelling will not occur, and the economic benefit is good.

[0048] In an embodiment of the present invention, a valve ① is provided on the pipeline of the leaching process of the electrowinning mixed solution entering the copper sulfide concentrate system ①, and a valve ② is provided on the pipeline of the leaching process of the electrowinning mixed solution entering the copper sulfide concentrate system ②; a valve ③ is provided on the pipeline of the thickening and clarification process of the copper sulfide concentrate system ① into which the pulp after leaching in the copper sulfide concentrate system ② enters, and a valve ④ is provided on the pipeline of the leaching process of the copper oxide concentrate system into which the pulp after leaching in the copper sulfide concentrate system ② enters; a valve ⑤ is provided on the pipeline of the leaching process of the raffinate in the copper oxide concentrate system entering the copper sulfide concentrate system ②;

[0049] The copper sulfide concentrate system ① is leached with the electrowinning mixed solution, and the valve ① is in the open state;

[0050] When the copper sulfide concentrate system ② is leached with the electrowinning mixed solution, the valve ② is opened and the valve ⑤ is closed. The electrowinning mixed solution enters the leaching process of the copper sulfide concentrate system ②. After the reaction is completed, the valve ③ is opened and at the same time the valve ④ is closed, and the pulp after leaching is incorporated into the copper sulfide concentrate system ①.

[0051] When the copper sulfide concentrate system ② is leached with the raffinate, the valve ② is closed and the valve ⑤ is opened. The raffinate enters the leaching process of the copper sulfide concentrate system ②. After the reaction is completed, the valve ③ is closed and at the same time the valve ④ is opened, and the pulp after leaching is incorporated into the leaching process of the copper oxide concentrate system.

[0052] In an embodiment of the present invention, the thickened underflow ① undergoes a pressure filtration and washing process to obtain a pressure filtrate ① and a roasted ore leaching residue, and the pressure filtrate ① flows into the leaching process in the copper oxide concentrate system.

[0053] In an embodiment of the present invention, the thickened underflow ② in the copper oxide concentrate system undergoes a pressure filtration and washing process to obtain a pressure filter cake and a pressure filtrate ②, and the pressure filtrate ② flows into the leaching process in the copper oxide concentrate system.

[0054] The above-mentioned pressure filtrate is either a leaching solution or a washing solution. The main function of pressure filtration is to more thoroughly separate the leaching liquid from the leaching residue. The liquid returns to the system, and the leaching residue is discharged from the system.

[0055] In an embodiment of the present invention, the electrowinning mixed solution in the copper sulfide concentrate system ① is a mixture of the electrowinning rich liquid and the electrowinning lean liquid in the roasting - leaching - electrowinning process flow. The copper concentration of the electrowinning mixed solution is 40 - 75 g / L, and the copper acid concentration and

[0056] Wherein:

[0057] ——Copper ion concentration;

[0058] ——Relative molecular mass of sulfuric acid;

[0059] Mr (Cu) ——Relative atomic mass of Cu;

[0060] ——Concentration of sulfuric acid.

[0061] This control step is as follows: In the electrowinning workshop, the copper concentration of the lean electrowinning solution is controlled at 40 g / L. Under the production condition that the copper leaching amount in the upstream process < the copper electrowinning amount in the downstream process, the system consumes the copper in the solution, the copper concentration in the solution slowly decreases, and the delivery volume of the rich electrowinning solution directly supplied to the electrowinning workshop gradually increases to maintain the normal copper supply in the electrowinning workshop. Then, the amount of the rich electrowinning solution directly transferred to the electrowinning mixed solution pool gradually decreases. Among its liquid sources, the proportion of the lean electrowinning solution gradually increases, and the copper concentration gradually approaches that of the lean electrowinning solution. Under the production condition that the copper leaching amount in the upstream process > the copper electrowinning amount in the downstream process, the copper stored in the system solution increases, the copper concentration in the solution slowly rises, and the delivery volume of the rich electrowinning solution directly supplied to the electrowinning workshop gradually decreases. To maintain the solution balance between the rich electrowinning solution pool and the electrowinning mixed solution pool, the solution in the rich electrowinning solution pool bypasses the electrowinning workshop and directly enters the electrowinning mixed solution pool. The copper concentration in the solution in the electrowinning mixed solution pool gradually rises, realizing an increase in the copper storage amount in the solution and enhancing the anti-interference ability of the system. When the copper concentration in the rich electrowinning solution increases to 110 g / L, in the solution source of the electrowinning mixed solution pool, the proportions of the lean electrowinning solution and the rich electrowinning solution are each 50%, and the copper concentration in the electrowinning mixed solution pool increases to 75 g / L.

[0062] In the present invention, the copper concentration in the solution system is controlled below 110 g / L. Excessively high copper concentration will greatly increase the risk of pipeline crystallization during actual application, affecting the safe and stable operation of the system.

[0063] In the embodiment of the present invention, sulfuric acid and neutral water are also added in the leaching process of the copper sulfide concentrate system ① to maintain the copper acid concentration and increase the ionic concentration of the solution, improve the conductivity of the solution, and maintain a good process parameter range for the downstream electrowinning process;

[0064] In the copper sulfide concentrate system ①, the leaching pulp concentration is 4% - 8%, the reaction temperature is 40°C - 80°C, the reaction time is 5 - 9 h, and the copper concentration at the reaction end point is 60 g / L - 110 g / L.

[0065] In this control step, good reaction conditions are mainly created for the copper electrowinning process, and the involved reaction equations are as follows:

[0066] Cathode reaction: Cu 2+ + 2e = Cu↓, E = 0.34V

[0067] Anode reaction:

[0068] Total chemical reaction equation:

[0069]

[0070] The products of the copper electrowinning process are cathode copper, anode oxygen, and regenerated sulfuric acid in the solution. During the copper electrowinning process, the concentrations of Cu 2+ and H2SO4 in the solution will change, but the overall copper-acid concentration and remain unchanged. Controlling the appropriate copper-acid concentration and can not only ensure the smooth progress of the electrowinning process but also avoid situations such as a large amount of impurities leaching during the roasting ore leaching process when the acid concentration in the electrowinning mixed solution is too high or the solid-liquid cannot be effectively separated during the thickening and settling process after the roasting ore leaching when the acidity is too low.

[0071] In the embodiment of the present invention, when the roasted ore in the copper sulfide concentrate system ② is leached with the electrowinning mixed solution, the leaching conditions are the same as those in the copper sulfide concentrate system ①; when leached with the raffinate, the leaching pulp concentration is 4% - 8%, the reaction temperature is 25 - 80 °C, and the reaction time is 5 - 9 h.

[0072] The copper sulfide concentrate system ② is leached with the raffinate. After the leached pulp is incorporated into the leaching process of the copper oxide concentrate system, the raffinate and sulfuric acid are supplemented simultaneously to make the reaction liquid-solid ratio 4 - 10, and the pH value at the end of the reaction is 1.2 - 1.8.

[0073] The treatment amounts of the copper sulfide concentrate and the copper oxide concentrate, as well as the leaching method of the copper sulfide concentrate system ②, can be flexibly adjusted and cooperate with each other to achieve the supply-demand balance between the treatment of the copper sulfide concentrate and the copper oxide concentrate and the production of cathode copper by electrowinning, and at the same time achieve the stable and efficient production of the leaching-electrowinning system and the extraction-electrowinning system.

[0074] The following embodiments more specifically describe the content disclosed in the present application, and these embodiments are only for illustrative purposes.

[0075] Example 1

[0076] This example adopts the production practice of efficiently producing cathode copper from copper oxide concentrate and copper sulfide concentrate of a certain copper-cobalt hydrometallurgical enterprise in the Democratic Republic of the Congo under the condition of flexibly adjusting the roasting ore leaching method. The process flow diagram is shown in Figure 1 , and the main element analysis and detection results of the copper sulfide concentrate and copper oxide concentrate used are shown in Table 1:

[0077] Table 1 Main element analysis and detection results of copper oxide concentrate and copper sulfide concentrate (%)

[0078]

[0079] In this embodiment, there are two sets of independent copper sulfide concentrate roasting systems, both using oxidative roasting at a roasting temperature of 700 - 780 °C. In the initial stage, the roasted ores produced by copper sulfide concentrate system ① and copper sulfide concentrate system ② are all leached with the electrowinning mixed solution. The initial electrowinning mixed solution all comes from the spent electrowinning solution in the electrowinning workshop, without the incorporation of rich electrowinning solution. Its initial copper concentration is 40 g / L, and the copper acid concentration and In the leaching process, the pulp concentration during the reaction process is 4%, the reaction temperature is 60 °C, and the reaction time is 5 h. After the leaching reaction is completed, the terminal acid concentration in the initial thickened overflow liquid is 82 g / L, the copper concentration is 70 g / L, and the copper acid concentration and

[0080] In this embodiment, the two sets of independent copper sulfide concentrate roasting systems process 380 t / d of copper sulfide concentrate, and the leaching rate of the roasted ore is 97%. The total amount of copper leached from the roasted ores produced by the two roasting systems is 464 t / d. The copper oxide concentrate treatment system processes 1000 t / d of ore, the leaching rate of copper oxide concentrate is 80%, and the leached copper amount is 128 t / d. There are two downstream electrowinning workshops, corresponding to the leaching - electrowinning system and the extraction - electrowinning system respectively, and the cathode copper production amount in both electrowinning productions is 295 t / d.

[0081] In the initial production stage, both electrowinning workshops are operating at full capacity. The copper content in the solution in the solution tank of the leaching - electrowinning process in copper sulfide concentrate system ① increases by 169 t / d, and the copper concentration shows an upward trend. The copper content in the solution in the solution tank of the extraction - electrowinning process in the copper oxide concentrate system decreases by 167 t / d, and the copper concentration in the solution shows a downward trend.

[0082] After one week of production, the solution in the leaching - electrowinning system in copper sulfide concentrate system ① contains 1183 t of enriched copper, the copper concentration in the rich electrowinning solution reaches 110 g / L, the copper concentration in the electrowinning mixed solution reaches 75 g / L, and the copper inventory in the solution system reaches a high value. At the same time, the copper content in the solution in the extraction - electrowinning system in the copper oxide concentrate system decreases by 1169 t. Copper sulfide concentrate system ② is converted from leaching with the electrowinning mixed solution to leaching with the raffinate. When copper sulfide concentrate system ② conducts raffinate leaching, the pulp concentration is 4%, the reaction temperature is about 40 °C, the reaction time is 5 - 9 h, and the pH at the end of leaching is 1.8; the pulp after raffinate leaching is incorporated into the copper oxide concentrate leaching process, and at the same time, raffinate and sulfuric acid are supplemented. The reaction liquid - solid ratio is 4, and the pH at the reaction end is 1.8. Under these production conditions, the copper content in the solution in the solution tank of the leaching - electrowinning system in copper sulfide concentrate system ① decreases by an average of 62 t / d, and the copper concentration shows a downward trend. The copper content in the solution in the solution tank of the extraction - electrowinning system increases by an average of 65 t / d, and the copper concentration in the solution shows an upward trend.

[0083] In this embodiment, by flexibly adjusting the water quenching method of copper sulfide concentrate system ②, the copper supply and production in the leaching - electrowinning system and the extraction - electrowinning system are ensured to be stable, realizing long - term stable operation.

[0084] Example 2

[0085] This example adopts the production practice of efficiently producing cathode copper from copper oxide concentrate and copper sulfide concentrate of a certain copper-cobalt hydrometallurgy enterprise in the Democratic Republic of the Congo under the condition of flexibly adjusting the roasting leaching method. The main element analysis and detection results of the copper sulfide concentrate and copper oxide concentrate used are shown in Table 2:

[0086] Table 2 Main element analysis and detection results of copper oxide concentrate and copper sulfide concentrate (%)

[0087]

[0088] In this example, two independent copper sulfide concentrate roasting systems are included, both using oxidation roasting with a roasting temperature of 700 - 780 °C. In the initial stage, all the roasted ores produced by copper sulfide concentrate system ① and copper sulfide concentrate system ② are leached with the electrowinning mixed solution. The initial copper concentration of the electrowinning mixed solution is 50 g / L, the sulfuric acid concentration is 90 g / L, and the copper acid concentration and In the leaching process, the pulp concentration during the reaction is 8%, the reaction temperature is 80 °C, and the reaction time is 7 h. After the leaching reaction is completed, the final copper concentration in the initial thickening overflow liquid is 79 g / L, and the copper acid concentration and

[0089] In this example, the two independent copper sulfide concentrate roasting systems process 380 t / d of copper sulfide concentrate, and the roasting ore leaching rate is 97%. The total amount of copper leached from the roasted ores produced by the two roasting systems is 479 t / d. The copper oxide concentrate treatment system processes 1000 t / d of ore, and the leaching rate of copper oxide concentrate is 81%, with the leached copper amount being 146 t / d. There are two downstream electrowinning workshops, corresponding to the leaching-electrowinning system and the extraction-electrowinning system respectively, and the daily cathode copper production amount by electrowinning in both is 295 t / d.

[0090] In the initial production stage, both electrowinning workshops are operating at full capacity. The daily copper content increase in the solution pool of the leaching-electrowinning process of copper sulfide concentrate system ① is 184 t / d, and the copper concentration shows an upward trend. The daily copper content decrease in the solution pool of the copper oxide concentrate system is 56 t / d, and the solution copper concentration shows a downward trend.

[0091] After six days of production, the enriched solution in copper sulfide concentrate system ① contains 1104 t of copper. The copper concentration in the electrowinning rich solution of the leaching-electrowinning system reaches 106 g / L, and the copper concentration of the electrowinning mixed solution reaches 70 g / L. The copper inventory in the solution system is close to the high value. At the same time, the solution in the copper oxide concentrate system reduces the copper content by 720 t.

[0092] The copper sulfide concentrate system ② was converted from leaching with electrowinning mixed solution to leaching with raffinate. At the same time, maintenance work was carried out on the copper oxide concentrate production line, and the processing volume decreased to 0 t / d. In the raffinate leaching process of the copper sulfide concentrate system ②, the pulp concentration during the reaction was 8%, the reaction temperature was about 80 °C, the reaction time was 9 h, the pH at the end of leaching was 1.2, and the pulp after raffinate leaching entered the copper oxide concentrate leaching process. Under these production conditions, the average daily reduction in copper content in the solution in the solution tanks of both the copper sulfide concentrate system ① and the copper oxide concentrate system was 56 t / d, and the copper concentration showed a downward trend. After the maintenance (one week) was completed, the copper oxide concentrate production line resumed normal production, and the copper concentration increased accordingly.

[0093] In this embodiment, the leaching method of the copper sulfide concentrate system ② was flexibly adjusted. First, copper was stored in the solution of the copper sulfide concentrate system ① by quenching with electrowinning mixed solution. Subsequently, during the maintenance period of the copper oxide concentrate production line, it was converted to raffinate leaching to make up for the insufficient copper leaching amount of the copper oxide concentrate, so as to maintain normal production in the downstream electrowinning process during the maintenance period of the copper oxide concentrate production line.

[0094] Comparative Example 1

[0095] This embodiment adopted the production practice of copper oxide concentrate and copper sulfide concentrate from a copper-cobalt hydrometallurgical enterprise in the Democratic Republic of the Congo. Its system included a copper oxide concentrate processing system and a copper sulfide concentrate roasting and processing system, and the process flow was as Figure 2 shown. The main element analysis and detection results of the copper sulfide concentrate and copper oxide concentrate used in its process are as follows:

[0096] Table 1 Main element analysis and detection results of copper oxide concentrate and copper sulfide concentrate (%)

[0097]

[0098] In this comparative example, the copper sulfide concentrate roasting system adopted oxidative roasting, with a roasting temperature of 700 - 780 °C. The roasted ore produced by the roasting system could only be leached with raffinate. The pulp concentration during the leaching reaction was 6%, the reaction temperature was room temperature 70 °C, the reaction time was 7 h, the pH at the end of leaching was 1.5. The pulp after raffinate leaching was incorporated into the copper oxide concentrate leaching process, and at the same time, raffinate and sulfuric acid were supplemented, with a reaction liquid-solid ratio of 5 and a reaction end pH of 1.5.

[0099] In this comparative example, the copper sulfide roasting system processed 380 t / d of copper sulfide concentrate, with a roasted ore leaching rate of 97%. The total amount of copper leached from the roasted ore produced by the roasting system was 221 t / d. The copper oxide concentrate processing volume was 660 t / d, with a leaching rate of 80% and a leaching copper amount of 74 t / d, supplying a downstream electrowinning workshop to produce cathode copper products, with a daily electrowinning cathode copper amount of 295 t / d.

[0100] In this comparative example, the whole process of copper sulfide concentrate treatment is roasting - leaching - extraction - electrowinning. Compared with the roasting - leaching - electrowinning process, the extraction process is added, resulting in large production investment and high operating costs. In addition, the anti - interference ability of this system is weak. During the maintenance period of the upstream roasting process or the copper oxide concentrate process, the downstream electrowinning process must reduce the copper electrowinning output or enter the maintenance process synchronously in the short term to achieve the system supply - demand balance. Similarly, during the maintenance period of the downstream electrowinning process, the upstream roasting process or the copper oxide concentrate treatment process must reduce the ore treatment volume or enter the maintenance synchronously in the short term to achieve the system supply - demand balance.

[0101] The above are only the preferred embodiments of the present invention and are not intended to limit the present invention. For those skilled in the art, the present invention can have various changes and modifications. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included within the protection scope of the present invention.

Claims

1. A system for jointly and efficiently producing cathode copper from copper sulfide concentrate and copper oxide concentrate, characterized in that, It includes copper sulfide concentrate system ①, copper oxide concentrate system, and copper sulfide concentrate system ②; The copper sulfide concentrate system ① includes a roasting - leaching - electrowinning process. The copper sulfide concentrate is roasted to form calcine, which is leached using an electrowinning mixed solution. After leaching, solid - liquid separation is carried out to obtain thickened underflow ① and thickened overflow ①. The thickened overflow ① enters the electrowinning rich - liquid tank and is used for electrowinning to produce cathode copper and is converted into electrowinning lean liquid. The electrowinning rich liquid and the electrowinning lean liquid are mixed to obtain the electrowinning mixed solution, which is returned to the leaching process of the copper sulfide concentrate system ①. The thickened underflow ① is stored after pressure filtration and washing; The copper oxide concentrate system includes a leaching - extraction - electrowinning process. The copper oxide concentrate is leached using the raffinate. After leaching, solid - liquid separation is carried out to obtain thickened underflow ② and thickened overflow ②. The thickened overflow ② is used for extraction - electrowinning to produce cathode copper. Part of the raffinate is returned to the leaching process, and part enters the cobalt recovery system. The thickened underflow ② is stored after pressure filtration and washing; The copper sulfide concentrate system ② can be incorporated into the copper sulfide concentrate system ① or the copper oxide concentrate system by flexibly selecting the leaching method. When incorporated into the copper sulfide concentrate system ①, the copper sulfide concentrate in the copper sulfide concentrate system ② is roasted and then leached using the electrowinning mixed solution, and the leaching pulp is directly incorporated into the thickening and clarification process of the copper sulfide concentrate system ①. When incorporated into the copper oxide concentrate system, the copper sulfide concentrate in the copper sulfide concentrate system ② is roasted and then leached using the raffinate, and the leaching pulp is incorporated into the leaching process of the copper oxide concentrate system.

2. The system for jointly and efficiently producing cathode copper from copper sulfide concentrate and copper oxide concentrate according to claim 1, wherein A valve ① is provided on the pipeline where the electrowinning mixed solution enters the leaching process of the copper sulfide concentrate system ①, and a valve ② is provided on the pipeline where the electrowinning mixed solution enters the leaching process of the copper sulfide concentrate system ②; A valve ③ is provided on the pipeline where the leached pulp of the copper sulfide concentrate system ② enters the thickening and clarification process of the copper sulfide concentrate system ①, and a valve ④ is provided on the pipeline where the leached pulp of the copper sulfide concentrate system ② enters the leaching process of the copper oxide concentrate system; A valve ⑤ is provided on the pipeline where the raffinate of the copper oxide concentrate system enters the leaching process of the copper sulfide concentrate system ②; When the copper sulfide concentrate system ① is leached using the electrowinning mixed solution, valve ① is in the open state; When the copper sulfide concentrate system ② is leached using the electrowinning mixed solution, valve ② is opened and valve ⑤ is closed. The electrowinning mixed solution enters the leaching process of the copper sulfide concentrate system ②. After the reaction is completed, valve ③ is opened and at the same time valve ④ is closed, and the leached pulp is incorporated into the copper sulfide concentrate system ①.

3. The system for jointly and efficiently producing cathode copper from copper sulfide concentrate and copper oxide concentrate according to claim 2, wherein When the copper sulfide concentrate system ② is leached using the raffinate in the copper oxide concentrate system, valve ② is closed and valve ⑤ is opened. The raffinate enters the leaching process of the copper sulfide concentrate system ②. After the reaction is completed, valve ③ is closed and at the same time valve ④ is opened, and the leached pulp is incorporated into the leaching process of the copper oxide concentrate system.

4. The system for jointly and efficiently producing cathode copper from copper sulfide concentrate and copper oxide concentrate according to claim 1, characterized in that, The thickened underflow ① undergoes a pressure filtration and washing process to obtain filtrate ① and roasted ore leaching residue, and the filtrate ① flows into the leaching process in the copper oxide concentrate system.

5. The system for jointly and efficiently producing cathode copper from copper sulfide concentrate and copper oxide concentrate according to claim 1, wherein The thickened underflow ② in the copper oxide concentrate system undergoes pressure filtration and washing to obtain filter residue and filtrate ②, and the filtrate ② flows into the leaching process in the copper oxide concentrate system.

6. The system for jointly and efficiently producing cathode copper from copper sulfide concentrate and copper oxide concentrate according to claim 1, wherein The copper concentration in the electrowinning mixed solution is 40 - 75 g / L, and the copper acid concentration is 160 - 210 g / L; Wherein: —— Copper ion concentration; —— relative molecular mass of sulfuric acid; Mr (Cu) —— Relative atomic mass of Cu; —— Sulfuric acid concentration.

7. The system for jointly and efficiently producing cathode copper from copper sulfide concentrate and copper oxide concentrate according to claim 1, wherein In the leaching process of the copper sulfide concentrate system ①, sulfuric acid and neutral water are also added to maintain the copper acid concentration and 160 - 210 g / L.

8. The system for jointly and efficiently producing cathode copper from copper sulfide concentrate and copper oxide concentrate according to claim 1, characterized in that, In the copper sulfide concentrate system ①, the concentration of the leaching pulp is 4% - 8%, the reaction temperature is 40°C - 80°C, the reaction time is 5 - 9 h, and the copper concentration at the reaction end point is 60 g / L - 110 g / L.

9. The system for jointly and efficiently producing cathode copper from copper sulfide concentrate and copper oxide concentrate according to claim 1, wherein When the roasted ore in the copper sulfide concentrate system ② is leached with the electrowinning mixed solution, the leaching conditions are the same as those in the copper sulfide concentrate system ①; when leached with the raffinate, the concentration of the leaching pulp after leaching is 4% - 8%, the reaction temperature is 25 - 80°C, and the reaction time is 5 - 9 h.

10. The system for the combined and efficient production of cathode copper from copper sulfide concentrate and copper oxide concentrate according to claim 1, wherein, The copper sulfide concentrate system ② adopts leaching with the raffinate. After leaching, the pulp is incorporated into the leaching process of the copper oxide concentrate system, and at the same time, the raffinate and sulfuric acid are supplemented to make the reaction liquid-solid ratio 4 - 10, and the pH value at the reaction end point is 1.2 - 1.8.

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