Dressing and smelting combined process method for treating low-grade high-oxidation-rate copper ore

Abstract

The invention discloses a beneficiation-metallurgy combined process method for treating low-grade high-oxidation-rate copper ore. The beneficiation-metallurgy combined process method comprises the steps that the crushed low-grade high-oxidation-rate copper ore is divided into a part A, a part B and a part C according to the particle size; the part A is subjected to color sorting, and color-sorted concentrate is obtained; carrying out ore grinding and copper sulphide flotation on the color separation concentrate to obtain copper sulphide concentrate and sulfur separation tailings; and the copper sulfide concentrate, the sulfur separation tailings and the part C of ore are further treated to obtain copper-rich leachate. According to the method, coarse particles are partially and coarsely enriched through the color selector, the selection grade of the low-grade copper oxide ore is improved, a large amount of ore grinding loss is omitted, the situation that due to the low grade of raw ore, produced metal is less is avoided, and meanwhile the ore grinding and beneficiation cost is reduced; the beneficiation and smelting process can be flexibly selected according to the selectability of copper oxide in the ore and the content of acid-consuming gangue, acid consumption is reduced, and beneficiation and smelting economic benefits are improved.

Description

Technical Field

[0001] This invention relates to the field of ore beneficiation and smelting, and specifically to a process for processing low-grade, high-oxidation-rate copper ore. Background Technology

[0002] With economic development, the demand for copper is increasing, and easily mined, easily beneficiated, high-quality copper ores are becoming increasingly scarce. A growing number of low-grade ores urgently need to be developed and utilized. It is well known that copper ore bodies generally contain copper oxide, secondary copper sulfide, and primary copper sulfide ores from the surface down to the interior. Secondary and primary copper sulfide ores often have better beneficiation properties, while many copper oxide ores have poorer beneficiation. In the Central African copper-cobalt belt, there are numerous open-pit copper mines, which are mixed sulfur-oxygen copper deposits. Their surface layer is copper oxide, while the underlying layer is mainly secondary copper sulfide. During mining, a significant amount of low-grade, high-oxidation-rate copper ore is produced. However, due to the low grade of the ore, poor beneficiation properties in some areas, low beneficiation recovery rates, high reagent consumption or leaching acid consumption, and relatively high grinding costs, the beneficiation costs are high, severely limiting the development and utilization of low-grade, high-oxidation-rate copper ores. Summary of the Invention

[0003] The technical problem to be solved by the present invention is to overcome the above-mentioned defects of the prior art and provide a combined beneficiation and smelting process for processing low-grade, high-oxidation-rate copper ore that can improve the beneficiation and smelting recovery rate and reduce acid consumption.

[0004] The technical solution adopted by this invention to solve its technical problem is as follows: A combined beneficiation and smelting process for processing low-grade, high-oxidation copper ore, comprising: crushing low-grade, high-oxidation copper ore to a particle size of less than 25 mm, and dividing it into part A, part B, and part C according to particle size; wherein the particle size of part A is greater than 10 mm; the particle size of part B is 0.1 mm to 10 mm; and the particle size of part C is less than 0.1 mm. Part A is subjected to color sorting to obtain color sorted concentrate and color sorted tailings; the color sorting uses the portion with high reflectivity in the 450nm~570nm wavelength band as the color sorted concentrate, with an enrichment ratio of 1~5. The color sorting concentrate is ground to obtain slurry A; the slurry A is subjected to copper sulfide flotation to obtain copper sulfide concentrate and sulfur tailings. The obtained copper sulfide concentrate was roasted and then wet leached to obtain copper-rich leachate A1. Sulfur tailings are processed using one of the following processes: a1, a2, or a3, to obtain copper-rich leachate A2. The ore in section C is processed using either process C1 or process C2 to obtain copper-rich leaching solution C. The a1 process involves sequentially performing desliming flotation, copper oxide flotation, and magnetic separation. The concentrate obtained from desliming flotation is copper oxide slime a1, and the tailings are subjected to copper oxide flotation. The concentrate obtained from copper oxide flotation is copper oxide concentrate, and the tailings are subjected to magnetic separation. The concentrate obtained from magnetic separation is magnetic concentrate, and the tailings are magnetic tailings. The copper oxide slime a1, copper oxide concentrate, and magnetic concentrate are then subjected to wet leaching. The a2 process involves: performing reverse flotation to obtain reverse flotation concentrate a2 and high-copper tailings as tailings; and then wet leaching the obtained high-copper tailings. The a3 process is: direct wet leaching; The C1 process is: direct wet leaching; The C2 process involves: performing reverse flotation to obtain reverse flotation concentrate C2 and copper oxide ore slime C2 as tailings; and then wet leaching the obtained copper oxide ore slime C2. The low-grade, high-oxidation-rate copper ore has an ore oxidation rate of over 70 wt% and a copper grade of less than 2 wt%.

[0005] Preferably, the low-grade, high-oxidation-rate copper ore has an ore oxidation rate of 80wt%~100wt% and a copper grade of 0.4wt%~1.5wt%.

[0006] Preferably, the slurry concentration of the slurry A is 26wt%~38wt%; the particle size of the slurry A is: particles with a diameter of less than 0.074mm account for 65wt%~78wt%.

[0007] Preferably, the copper sulfide flotation of the slurry A includes roughing, scavenging and cleaning, wherein the number of cleaning stages is 2 to 5; the middlings obtained during the flotation process are returned to the previous flotation stage.

[0008] Preferably, the reagents used in the copper sulfide flotation of the slurry A include collectors and frothers.

[0009] Preferably, the collector used for copper sulfide flotation of the slurry A includes butyl xanthate and / or pentyl xanthate.

[0010] Preferably, the frother used in the copper sulfide flotation of the slurry A includes pine oil.

[0011] Preferably, the collector used in the copper sulfide flotation of the slurry A is 30g / t ore to 200g / t ore.

[0012] Preferably, the amount of frother used in the copper sulfide flotation of the slurry A is 5g / t ore to 80g / t ore.

[0013] Preferably, the desliming flotation includes one or more stages, the concentrate obtained from each stage is copper oxide slime a1, the tailings obtained from the last stage are the tailings from the desliming flotation, and the tailings obtained from each stage except the last stage enter the next stage of flotation operation.

[0014] Preferably, the reagents used in the desliming flotation include pine oil, with a dosage of 3g / t ore to 30g / t ore.

[0015] Preferably, the copper oxide flotation includes one or more stages, the concentrate obtained from each stage is copper oxide concentrate, the tailings obtained from the last stage are tailings from copper oxide flotation, and the tailings obtained from each stage other than the last stage enter the next stage of flotation operation.

[0016] Preferably, the reagents used in copper oxide flotation include sulfiding agents and collectors.

[0017] Preferably, the sulfiding agent used in copper oxide flotation includes sodium hydrosulfide and / or sodium sulfide.

[0018] Preferably, the collector used in copper oxide flotation includes butyl xanthate and / or pentyl xanthate.

[0019] Preferably, the amount of sulfiding agent used in copper oxide flotation is 0.8 kg / t ore to 5.0 kg / t ore.

[0020] Preferably, the amount of collector used in copper oxide flotation is 50g / t ore to 500g / t ore.

[0021] Preferably, the magnetic separation includes roughing and cleaning. The concentrate obtained from roughing enters the cleaning process, the tailings obtained from roughing are magnetic tailings, the tailings obtained from cleaning are returned to roughing, and the concentrate obtained from cleaning is magnetic concentrate.

[0022] Preferably, the magnetic field strength of the magnetic separation is 0.8T~1.5T.

[0023] Preferably, the reverse flotation includes one or more stages, the concentrate obtained from each stage is the reverse flotation concentrate, the tailings obtained from the last stage are the reverse flotation tailings, and the tailings obtained from each stage other than the last stage enter the next stage of flotation operation.

[0024] Preferably, the collector used in reverse flotation is a fatty acid collector.

[0025] Preferably, the amount of collector used in reverse flotation is 0.5 kg / t ore to 3 kg / t ore.

[0026] Preferably, the ore in part B is granulated with binder and solvent to form solidified pellets with a particle size of 5mm to 30mm, which are then subjected to bio-heap leaching together with the color sorting tailings to obtain copper-rich leaching solution B.

[0027] Preferably, the bioleaching process uses *Thiobacillus ferrooxidans*; the pH value of the leaching pile is 1.6~2.0.

[0028] Preferably, the solvent used for granulation is water, and the amount of water used is 10wt% to 25wt% of the amount of ore in part B.

[0029] Preferably, the amount of binder used in granulation is 1wt% to 7wt% of the amount of ore in part B.

[0030] Preferably, the binder used in granulation includes carboxymethyl cellulose and sulfate-resistant cement.

[0031] Preferably, the binder contains 50 wt% to 70 wt% carboxymethyl cellulose.

[0032] Preferably, the sulfate-resistant cement in the binder accounts for 30wt% to 50wt%.

[0033] Preferably, the height of the bioleaching heap is 2m to 4m.

[0034] Preferably, the leaching cycle of bio-heap leaching is 2 to 12 months.

[0035] Preferably, dilute sulfuric acid is sprayed during the bioleaching process, with a concentration of 0.1 mol / L to 1 mol / L and a spraying intensity of 0.1 L / min. -1 ·m -2 ~1L·min -1 ·m -2 .

[0036] Preferably, the inoculum amount of *Thiobacillus ferricyanide* is 10 wt% to 20 wt%; the viable bacteria concentration in the *Thiobacillus ferricyanide* inoculum is 10 wt%. 6 ~10 9 per mL.

[0037] The present invention has the following beneficial effects: (1) The method of the present invention crushes and classifies the ore, and coarse particles are coarsely enriched by color sorter to improve the feed grade of low-grade oxidized copper ore; the useful minerals in low-grade high-oxidation copper ore are mainly malachite, chrysocolla, azurite, etc.; these useful mineral particles are rich in malachite (bright green, emerald green), chrysocolla (blue green, greenish blue), azurite (indigo blue, sky blue), and their copper grade is significantly improved by appropriate color sorting separation; the tailings are particles that are judged as invalid by the color sorter and discarded. This part is mainly gangue minerals (quartz, feldspar, mica, etc.), which are separated because their colors (colorless, white, light yellow, etc.) are significantly different from the target minerals; a large amount of grinding loss is saved, and the low grade of the raw ore results in less metal output, while the high cost of grinding and beneficiation leads to poor beneficiation and smelting economic benefits or even losses; (2) This method separates copper sulfide concentrate with extremely low acid consumption by sorting by particle size, color sorting, and copper sulfide flotation, avoiding excessive acid-consuming gangue from entering the leaching process; and provides a variety of feasible treatment options for the obtained sulfur tailings and ores with a particle size of less than 0.1 mm; the beneficiation process can be flexibly selected according to the beneficiation of copper oxide and the content of acid-consuming gangue in the ore, reducing acid consumption and improving the economic benefits of beneficiation.

[0038] In addition to the objectives, features, and advantages described above, the present invention has other objectives, features, and advantages. The invention will now be described in further detail with reference to the accompanying drawings. Attached Figure Description

[0039] The accompanying drawings, which form part of this application, are used to provide a further understanding of the invention. The illustrative embodiments of the invention and their descriptions are used to explain the invention and do not constitute an undue limitation of the invention. In the drawings: Figure 1 This is a process flow diagram of the combined beneficiation and smelting process for processing low-grade, high-oxidation copper ore according to Embodiment 1 of the present invention. Figure 2 This is process flow diagram a1 in the combined beneficiation and smelting process for processing low-grade, high-oxidation copper ore according to an embodiment of the present invention. Figure 3 This is process flow diagram a2 in the combined beneficiation and smelting process for processing low-grade, high-oxidation copper ore according to an embodiment of the present invention. Figure 4 This is a flow chart of process C2 in the combined beneficiation and smelting process for processing low-grade, high-oxidation-rate copper ore according to an embodiment of the present invention. Detailed Implementation

[0040] To make the objectives, solutions, and beneficial technologies of this invention clearer, the invention will be further described in detail below with reference to embodiments and accompanying drawings. It should be noted that the embodiments described in this specification are merely illustrative of the invention and are not intended to limit the invention.

[0041] For simplicity, this paper only explicitly discloses some numerical ranges. However, any lower limit can be combined with any upper limit to form an undefined range; and any lower limit can be combined with other lower limits to form an undefined range, just as any upper limit can be combined with any other upper limit to form an undefined range. Furthermore, although not explicitly stated, every point or individual value between the endpoints of a range is included within that range. Therefore, each point or individual value can serve as its own lower or upper limit and be combined with any other point or individual value, or with other lower or upper limits, to form an undefined range.

[0042] In this description, it should be noted that, unless otherwise stated, "above" and "below" include the stated number, "multiple" in "one or more" means two or more, and "more than" in "one or more" means two or more.

[0043] The notation “-0.074mm”, “-200 mesh”, and “+10mm” is common in the mineral processing industry. The negative sign indicates that the particle size is below the value, such as -0.074mm, which means that the particle size is below 0.074mm. The positive sign indicates that the particle size is above the value, such as +10mm, which means that the particle size is above 10mm.

[0044] The *Thiobacillus ferrooxidans* used in the embodiments of this invention were purchased from the China General Microbiological Culture Collection Center (CGMCC).

[0045] The present invention provides a combined beneficiation and smelting process for processing low-grade, high-oxidation copper ore, comprising: crushing the low-grade, high-oxidation copper ore to a particle size of less than 25 mm, and dividing it into part A, part B, and part C according to particle size; wherein the particle size of part A is greater than 10 mm; the particle size of part B is 0.1 mm to 10 mm; and the particle size of part C is less than 0.1 mm. Part A is subjected to color sorting to obtain color sorted concentrate and color sorted tailings; the color sorting uses the portion with high reflectivity in the 450nm~570nm wavelength band as the color sorted concentrate, with an enrichment ratio of 1~5. The color sorting concentrate is ground to obtain slurry A; the slurry A is subjected to copper sulfide flotation to obtain copper sulfide concentrate and sulfur tailings. The obtained copper sulfide concentrate was roasted and then wet leached to obtain copper-rich leachate A1. Sulfur tailings are processed using one of the following processes: a1, a2, or a3, to obtain copper-rich leachate A2. The ore in section C is processed using either process C1 or process C2 to obtain copper-rich leaching solution C. The a1 process involves sequentially performing desliming flotation, copper oxide flotation, and magnetic separation. The concentrate obtained from desliming flotation is copper oxide slime a1, and the tailings are subjected to copper oxide flotation. The concentrate obtained from copper oxide flotation is copper oxide concentrate, and the tailings are subjected to magnetic separation. The concentrate obtained from magnetic separation is magnetic concentrate, and the tailings are magnetic tailings. The copper oxide slime a1, copper oxide concentrate, and magnetic concentrate are then subjected to wet leaching. The a2 process involves: performing reverse flotation to obtain reverse flotation concentrate a2 and high-copper tailings as tailings; and then wet leaching the obtained high-copper tailings. The a3 process is: direct wet leaching; The C1 process is: direct wet leaching; The C2 process involves: performing reverse flotation to obtain reverse flotation concentrate C2 and copper oxide ore slime C2 as tailings; and then wet leaching the obtained copper oxide ore slime C2. The low-grade, high-oxidation-rate copper ore has an ore oxidation rate of over 70 wt% and a copper grade of less than 2 wt%.

[0046] From an economic perspective, among the A1, A2, and A3 processes available for treating sulfur tailings, A1 is suitable when the copper oxide minerals in the slurry are relatively easy to remove; A2 is suitable when the slurry contains a large amount of acid-consuming gangue and the leaching acid consumption is high; reverse flotation can remove the acid-consuming gangue from the sulfur tailings to obtain high-copper tailings; and A3 is suitable when the copper oxide minerals in the slurry are poorly removeable and there are not many acid-consuming gangues. Technical personnel with expertise in this field can freely choose the appropriate solution based on the specific circumstances.

[0047] From an economic perspective, among the two processes that can be used to process C-section ore, C1 is suitable for situations where there is less acid-consuming gangue and lower leaching acid consumption; while C2 is suitable for situations where there is more acid-consuming gangue and higher leaching acid consumption. Technical personnel with expertise in this field can freely choose the appropriate solution based on the circumstances.

[0048] In some embodiments of the present invention, the color sorting concentrate is ground using a ball mill to achieve a grinding concentration of 65wt%-85wt%.

[0049] In some embodiments of the present invention, when the raw ore is divided into parts A, B, and C, a washing machine is used for washing, and a vibrating screen is used for grading. Washing also removes the sludge and dust adhering to the surface of the ore, revealing the ore's natural color, which is beneficial for color sorting.

[0050] The resulting copper-rich leachates can be used in an extraction-electrowinning process to produce cathode copper.

[0051] The degree of crushing of low-grade, high-oxidation copper ore should be moderate. If the crushed size is too large, it will lead to a poorer enrichment ratio in color sorting; if the crushed size is too small, the crushing energy consumption will increase and it will be detrimental to flotation.

[0052] The valuable minerals in low-grade, high-oxidation copper ore are mainly malachite, chrysocolla, and azurite. These valuable mineral particles are rich in malachite (bright green, emerald green), chrysocolla (blue-green, greenish-blue), and azurite (indigo, sky blue). Through color sorting, their copper content is significantly enriched. Tailings are particles discarded by the color sorter as invalid. This part mainly consists of gangue minerals (quartz, feldspar, mica, etc.), which are separated because their colors (colorless, white, light yellow, etc.) are significantly different from the target minerals. Malachite has high reflectivity mainly in the green (G) band (approximately 495-570nm); chrysocolla has high reflectivity in the green (G) to blue (B) band (approximately 450-570nm); azurite has high reflectivity mainly in the blue (B) band (approximately 450-495nm); gangue minerals generally have high reflectivity in the red (R) band, while their reflectivity is relatively low in the blue and green bands.

[0053] In an embodiment of the present invention, the low-grade, high-oxidation-rate copper ore has an ore oxidation rate of 80wt%~100wt% and a copper grade of 0.4wt%~1.5wt%.

[0054] In an embodiment of the present invention, the slurry concentration of the slurry A is 26wt%~38wt%; the particle size of the slurry A is: particles with a diameter of less than 0.074mm account for 65wt%~78wt%.

[0055] In an embodiment of the present invention, the copper sulfide flotation of the slurry A includes roughing, scavenging and cleaning, wherein the number of cleaning stages is 2 to 5; the middlings obtained during the flotation process are returned to the previous flotation stage.

[0056] In an embodiment of the present invention, the reagents used for copper sulfide flotation of the slurry A include collectors and frothers.

[0057] In an embodiment of the present invention, the collector used for copper sulfide flotation of the slurry A includes butyl xanthate and / or pentyl xanthate.

[0058] In an embodiment of the present invention, the frother used in the copper sulfide flotation of the slurry A includes pine oil.

[0059] In an embodiment of the present invention, the collector used in the copper sulfide flotation of the slurry A is 30g / t ore to 200g / t ore.

[0060] In an embodiment of the present invention, the amount of frother used in the copper sulfide flotation of the slurry A is 5 g / t ore to 80 g / t ore.

[0061] In an embodiment of the present invention, the desliming flotation includes one or more stages, the concentrate obtained from each stage is copper oxide slime a1, the tailings obtained from the last stage are the tailings from the desliming flotation, and the tailings obtained from each stage other than the last stage enter the next stage of flotation operation.

[0062] In an embodiment of the present invention, the reagent used for desliming flotation includes pine oil, and the dosage is 3g / t ore to 30g / t ore.

[0063] In an embodiment of the present invention, the copper oxide flotation includes one or more stages, the concentrate obtained from each stage is copper oxide concentrate, the tailings obtained from the last stage are tailings from copper oxide flotation, and the tailings obtained from each stage other than the last stage enter the next stage of flotation operation.

[0064] In embodiments of the present invention, the reagents used for copper oxide flotation include sulfiding agents and collectors.

[0065] In embodiments of the present invention, the sulfiding agent used for copper oxide flotation includes sodium hydrosulfide and / or sodium sulfide.

[0066] In embodiments of the present invention, the collectors used for copper oxide flotation include butyl xanthate and / or pentyl xanthate.

[0067] In embodiments of the present invention, the amount of sulfiding agent used in copper oxide flotation is 0.8 kg / t ore to 5.0 kg / t ore.

[0068] In embodiments of the present invention, the amount of collector used in copper oxide flotation is 50 g / t ore to 500 g / t ore.

[0069] In an embodiment of the present invention, the magnetic separation includes roughing and cleaning. The concentrate obtained from roughing enters the cleaning process, the tailings obtained from roughing are magnetic separation tailings, the tailings obtained from cleaning are returned to roughing, and the concentrate obtained from cleaning is magnetic separation concentrate.

[0070] In an embodiment of the present invention, the magnetic field strength of the magnetic separation is 0.8T~1.5T.

[0071] In some embodiments of the present invention, the magnetic separation employs a high-gradient magnetic separator.

[0072] In embodiments of the present invention, reverse flotation includes one or more stages, the concentrate obtained from each stage is reverse flotation concentrate, the tailings obtained from the last stage are reverse flotation tailings, and the tailings obtained from each stage other than the last stage enter the next stage of flotation operation.

[0073] In embodiments of the present invention, the collector used in reverse flotation is a fatty acid collector.

[0074] In some embodiments of the present invention, sodium oleate is used as the collector in reverse flotation.

[0075] In embodiments of the present invention, the amount of collector used in reverse flotation is 0.5 kg / t ore to 3 kg / t ore.

[0076] In some embodiments of the present invention, the B portion of ore is granulated with binder and solvent to form solidified pellets with a particle size of 5mm to 30mm, which are then subjected to bio-heap leaching together with color sorting tailings to obtain copper-rich leaching solution B.

[0077] Biological heap leaching can eliminate many costly grinding processes, thus improving economic efficiency.

[0078] In some embodiments of the present invention, pellets made by adding binders and solvents to the B-part ore are naturally dried to form solidified pellets, with the natural drying time being 18h to 150h.

[0079] In some embodiments of the present invention, the bio-heap leaching uses *Thiobacillus ferrooxidans*; the pH value of the leaching heap is 1.6 to 2.0.

[0080] In some embodiments of the present invention, the solvent used for granulation is water, and the amount of water used is 10wt% to 25wt% of the amount of ore in part B.

[0081] In some embodiments of the present invention, the amount of binder used for granulation is 1wt% to 7wt% of the amount of ore in part B.

[0082] In some embodiments of the present invention, the binder used for granulation includes carboxymethyl cellulose and sulfate-resistant cement.

[0083] In some embodiments of the present invention, the binder contains 50 wt% to 70 wt% carboxymethyl cellulose.

[0084] In some embodiments of the present invention, sulfate-resistant cement accounts for 30wt% to 50wt% of the binder.

[0085] In some embodiments of the present invention, the height of the bio-heap leaching is 2m to 4m.

[0086] In some embodiments of the present invention, the leaching cycle of bio-heap leaching is 2 to 12 months.

[0087] In some embodiments of the present invention, dilute sulfuric acid is sprayed during the bioleaching process. The concentration of the dilute sulfuric acid is 0.1 mol / L to 1 mol / L, and the spraying intensity is 0.1 L / min. -1 ·m -2 ~1L·min -1 ·m -2 .

[0088] In embodiments of the present invention, the inoculum amount of *Thiobacillus ferricyanide* is 10wt%~20wt%; the viable bacteria concentration in the *Thiobacillus ferricyanide* inoculum is 10...6 ~10 9 per mL.

[0089] Example The following examples describe the disclosure of this invention in more detail. These examples are merely illustrative, as various modifications and variations will be apparent to those skilled in the art within the scope of this disclosure. Unless otherwise stated, all parts, percentages, and ratios reported in the following examples are based on weight. Unless otherwise stated, all reagents used in the examples are available commercially or synthesized using conventional methods and are ready for use without further processing. Unless otherwise stated, all instruments used in the examples are available commercially.

[0090] Example 1 The ore processed in this embodiment is a low-grade, high-oxidation copper ore mined from the surface layer of an open-pit mine. The copper grade of the ore is 1.2 wt%, the bulk density of the material is 1.68 t / m³, the maximum ore particle size is 800 mm, and the ore oxidation rate is 85 wt%. The main useful minerals in the ore are malachite, as well as small amounts of chrysocolla, covellite, chalcocite, and copper-bearing cuprite. The gangue is mainly composed of quartz, feldspar, muscovite, and clay.

[0091] This embodiment describes a combined beneficiation and smelting process for processing low-grade, high-oxidation-rate copper ore. The process flow is as follows: Figure 1 As shown, the specific situation is as follows: (1) The low-grade, high-oxidation copper ore crushed to a particle size of less than 15 mm is divided into part A, part B and part C according to the particle size; The ore mined from the pit is crushed, and the product is washed using a washing machine and classified using a vibrating screen to obtain coarse particles with a diameter of 10 mm or more, and fine particles with a diameter of less than 10 mm. The yield of the coarse particles is 75 wt%, with a copper grade of 1.25 wt%; the yield of the fine particles is 25 wt%, with a copper grade of 1.05 wt%. The fine particles are then further classified using a hydrocyclone to obtain particles with a diameter of 0.1 mm to 10 mm and particles with a diameter of less than 0.1 mm. The coarse particles with a diameter of 10 mm or more are designated as part A; the particles with a diameter of 0.1 mm to 10 mm are designated as part B; and the particles with a diameter of less than 0.1 mm are designated as part C. (2) Part A is subjected to color sorting to obtain color sorted concentrate and color sorted tailings; the color sorting uses the portion with high reflectivity in the 450nm~570nm wavelength band as the color sorted concentrate; the copper grade of the color sorted concentrate is 2.3wt%, the yield of the color sorted concentrate is 42wt%, and the enrichment ratio is 1.92; the copper grade of the color sorted tailings is 0.5wt%, and the yield of the color sorted tailings is 58wt%; (3) The color sorting concentrate is ground to a grinding concentration of 68 wt%. The grinding product is classified using a hydrocyclone, and the overflow fineness is -0.074 mm, accounting for 74 wt%, to obtain a pulp A with a pulp concentration of 32 wt%. Pulp A is subjected to copper sulfide flotation to obtain copper sulfide concentrate and sulfur tailings. The copper sulfide flotation includes a roughing stage, a scavenging stage, and a cleaning stage. The middlings obtained during the flotation process are returned to the previous stage of flotation. The reagents used in the copper sulfide flotation of pulp A include a collector (butyl xanthate, 50 g / ton of ore) and a frother (pine oil, 20 g / ton of ore). Copper sulfide concentrate was roasted and then wet leached to obtain copper-rich leachate A1. Using process A1, see Figure 2 The tailings from the sulfur beneficiation process are sequentially subjected to desliming flotation, copper oxide flotation, and magnetic separation. The concentrate obtained from desliming flotation is copper oxide slime, and the resulting tailings are then subjected to copper oxide flotation. The concentrate obtained from copper oxide flotation is copper oxide concentrate, and the resulting tailings are then subjected to magnetic separation. The concentrate obtained from magnetic separation is magnetic separation concentrate, and the resulting tailings are magnetic separation tailings. The copper oxide slime, copper oxide concentrate, and magnetic separation concentrate are then subjected to wet leaching. The specific beneficiation process is as follows: Pine oil (5g / ton of ore) was added to the sulfur tailings for a first-stage desliming flotation. The resulting concentrate was copper oxide slime, and the resulting tailings were the tailings from the desliming flotation. The tailings from the desliming flotation are subjected to copper oxide flotation, which includes two roughing stages and two scavenging stages. The concentrate obtained from each stage is copper oxide concentrate, and the tailings obtained from the last stage are the tailings from copper oxide flotation. The tailings obtained from each stage except the last stage enter the next stage of flotation. The reagents used in copper oxide flotation include sulfiding agent (sodium hydrosulfide, 2.5 kg / ton of ore) and collector (butyl xanthate, 250 g / ton of ore). The tailings from copper oxide flotation are separated using a high-gradient magnetic separator, which includes a roughing stage and a cleaning stage. The tailings obtained from the roughing stage are magnetic tailings, the tailings obtained from the cleaning stage are returned to the roughing stage, and the concentrate obtained from the cleaning stage is magnetic concentrate. The field strengths for the roughing and cleaning stages are 1.2T and 1.0T, respectively. (4) After dehydration, the ore in part B is granulated. The added binder (carboxymethyl cellulose and hydrochloric acid resistant cement in a mass ratio of 6:4) is 3.5 wt% of the ore in part B, and the added water (as a solvent) is 15 wt% of the ore in part B. The granulation particle size is 20 mm, and then it is naturally dried and cured for 30 h to obtain cured pellets. Solidified pellets and color sorting tailings were subjected to bio-heap leaching to obtain copper-rich leachate B; The bioleaching process involved a heap height of 4 m and a pH value of 1.8–2.0. Dilute sulfuric acid was sprayed during the bioleaching process at a concentration of 0.2 mol / L and a spraying intensity of 0.4 L / min. -1 ·m -2~0.6L·min -1 ·m -2 The bioleaching process used *Thiobacillus ferrooxidans*; the inoculum size of *Thiobacillus ferrooxidans* was 15 wt%; the viable cell concentration in the *Thiobacillus ferrooxidans* inoculum was 10... 8 ~10 9 Cells / mL; the bio-heap leaching cycle is 9 months; (5) Using the C1 process, the C portion of ore is directly wet leached to obtain copper-rich leachate C.

[0092] The experimental results show that the total recovery rate of the color sorting concentrate after regrinding and re-sorting is 81.35%, the total acid consumption for leaching each concentrate is 0.80 tons of acid / ton of copper, and the leaching rate is 91.52%; the acid consumption for bio-heap leaching is 4.5 tons of acid / ton of copper, and the leaching rate is 64.54%; the acid consumption for direct wet leaching of ore C is 5.35 tons of acid / ton of copper, and the leaching rate is 65.31%.

[0093] Comparative Example 1 The ore processed in this comparative example is the same as that in Example 1. The specific process method used in this comparative example is as follows: The raw ore is crushed to a particle size of less than 15 mm, and then all of it is fed into a ball mill for grinding. The grinding concentration is 68 wt%. The grinding product is classified using a hydrocyclone, and the overflow fineness is -0.074 mm, accounting for 74 wt%, to obtain slurry A with a slurry concentration of 32 wt%. Slurry A is subjected to copper sulfide flotation to obtain copper sulfide concentrate and tailings. The copper sulfide flotation includes a roughing stage, a scavenging stage, and a four-stage cleaning stage. The middlings obtained during the flotation process are returned to the previous stage of flotation. The reagents used in the copper sulfide flotation of slurry A include a collector (butyl xanthate, 40 g / ton of ore) and a frother (pine oil, 15 g / ton of ore). Copper sulfide concentrate was roasted and then wet leached to obtain copper-rich leachate A1. The tailings from the sulfur beneficiation process are sequentially subjected to desliming flotation, copper oxide flotation, and magnetic separation. The concentrate obtained from desliming flotation is copper oxide slime, and the resulting tailings are then subjected to copper oxide flotation. The concentrate obtained from copper oxide flotation is copper oxide concentrate, and the resulting tailings are then subjected to magnetic separation. The concentrate obtained from magnetic separation is magnetic separation concentrate, and the resulting tailings are magnetic separation tailings. The copper oxide slime, copper oxide concentrate, and magnetic separation concentrate are then subjected to wet leaching. The specific beneficiation process is as follows: Pine oil (20g / ton of ore) was added to the sulfur tailings for a first-stage desliming flotation. The resulting concentrate was copper oxide slime, and the resulting tailings were the tailings from the desliming flotation. The tailings from the desliming flotation are subjected to copper oxide flotation, which includes two roughing stages and two scavenging stages. The concentrate obtained from each stage is copper oxide concentrate, and the tailings obtained from the last stage are the tailings from copper oxide flotation. The tailings obtained from each stage except the last stage enter the next stage of flotation. The reagents used in copper oxide flotation include sulfiding agent (sodium hydrosulfide, 4 kg / ton of ore) and collector (butyl xanthate, 400 g / ton of ore). The tailings from copper oxide flotation are separated using a high-gradient magnetic separator, which includes a roughing stage and a cleaning stage. The tailings obtained from the roughing stage are magnetic tailings, the tailings obtained from the cleaning stage are returned to the roughing stage, and the concentrate obtained from the cleaning stage is magnetic concentrate. The field strengths for the roughing and cleaning stages are 1.2T and 1.0T, respectively.

[0094] Ultimately, the total copper recovery rate in the beneficiation process was only 51.68%, resulting in a significant loss of metal. This was partly due to the low grade of the raw ore, which naturally leads to a lower recovery rate, and partly due to the poor selectivity of the large amount of severely muddy fine particles, which worsened the flotation process and thus contributed to the low recovery rate. Furthermore, the flotation reagents used in this case—sodium hydrosulfide, butyl xanthate, and pine oil—were used in large quantities, resulting in high reagent costs. The total acid consumption for leaching each concentrate was 2.1 tons of acid per ton of copper, with a leaching rate of 83.37%. Moreover, all ores in this case required grinding, significantly increasing grinding costs (such as grinding plant construction, auxiliary materials, and energy consumption).

[0095] Comparative Example 2 The ore processed in this comparative example is the same as that in Example 1. The specific process method used in this comparative example is as follows: The raw ore is crushed to a particle size of less than 15 mm, and then all of it is fed into a ball mill for grinding. The grinding concentration is 68 wt%. The grinding product is classified using a hydrocyclone, and the overflow fineness is -0.074 mm, accounting for 74 wt%, to obtain slurry A with a slurry concentration of 32 wt%. Slurry A is subjected to copper sulfide flotation to obtain copper sulfide concentrate and tailings. The copper sulfide flotation includes a roughing stage, a scavenging stage, and a four-stage cleaning stage. The middlings obtained during the flotation process are returned to the previous stage of flotation. The reagents used in the copper sulfide flotation of slurry A include a collector (butyl xanthate, 40 g / ton of ore) and a frother (pine oil, 20 g / ton of ore). The sulfur tailings are directly leached by wet leaching, while the copper sulfide concentrate is leached by wet leaching after roasting.

[0096] Ultimately, the combined acid consumption for leaching copper sulfide concentrate and tailings was 5.85 tons of acid per ton of copper, which is very high, with a leaching rate of 74.65%. In addition, all ores in this case required grinding, which greatly increased grinding costs and resulted in high beneficiation costs.

[0097] Example 2 The ore processed in this embodiment is a low-grade, high-oxidation copper ore mined from the surface layer of an open-pit mine. The ore has a copper grade of 1.0 wt%, a bulk density of 1.67 t / m³, a maximum ore particle size of 800 mm, and an oxidation rate of 90 wt%. The main useful mineral in the ore is malachite, with small amounts of chalcocite and covellite. The gangue mainly consists of quartz, calcite, feldspar, and dolomite. This low-grade, high-oxidation copper ore contains a large amount of acid-consuming gangue, and the acid consumption for direct leaching is higher than 20 tons of acid per ton of copper.

[0098] The combined beneficiation and smelting process for processing low-grade, high-oxidation copper ore in this embodiment is detailed below: (1) The low-grade, high-oxidation copper ore crushed to a particle size of less than 18 mm is divided into part A, part B and part C according to the particle size; The ore mined from the mine is crushed, and the product is washed using a washing machine and classified using a vibrating screen to obtain coarse particles with a diameter of 10 mm or more, and fine particles with a diameter of less than 10 mm. The yield of the coarse particles is 65 wt%, with a copper grade of 1.05 wt%; the yield of the fine particles is 35 wt%, with a copper grade of 0.92 wt%. The fine particles are then further classified using a hydrocyclone to obtain particles with a diameter of 0.1 mm to 10 mm and particles with a diameter of less than 0.1 mm. The coarse particles with a diameter of 10 mm or more are designated as part A; the particles with a diameter of 0.1 mm to 10 mm are designated as part B; and the particles with a diameter of less than 0.1 mm are designated as part C. (2) Part A is subjected to color sorting to obtain color sorted concentrate and color sorted tailings; the color sorting uses the portion with high reflectivity in the 450nm~570nm wavelength band as the color sorted concentrate; the copper grade of the color sorted concentrate is 2.1wt%, the yield of the color sorted concentrate is 35wt%, and the enrichment ratio is 2.1; the copper grade of the color sorted tailings is 0.4wt%, and the yield of the color sorted tailings is 65wt%. (3) The color sorting concentrate is ground to a grinding concentration of 70 wt%. The grinding product is classified using a hydrocyclone, and the overflow fineness is -0.074 mm, accounting for 73 wt%, to obtain a pulp A with a pulp concentration of 31 wt%. Pulp A is subjected to copper sulfide flotation to obtain copper sulfide concentrate and sulfur tailings. The copper sulfide flotation includes a roughing stage, a scavenging stage, and a cleaning stage. The middlings obtained during the flotation process are returned to the previous stage of flotation. The reagents used in the copper sulfide flotation of pulp A include a collector (butyl xanthate, 40 g / ton of ore) and a frother (pine oil, 15 g / ton of ore). Copper sulfide concentrate was roasted and then wet leached to obtain copper-rich leachate A1. Using process A2, see Figure 3The sulfur tailings were subjected to reverse flotation to obtain reverse flotation concentrate a2 (calcium-magnesium gangue) and high-copper tailings. The high-copper tailings were then wet-leached to obtain copper-rich leachate A2. The reverse flotation process included a roughing stage and a scavenging stage. The concentrates obtained from each stage were the reverse flotation concentrate a2, and the tailings obtained from the scavenging stage were the reverse flotation tailings. The tailings obtained from the roughing stage were then sent to the scavenging stage. The collector used in the reverse flotation was a fatty acid collector (sodium oleate, 0.8 kg / t ore). (4) For color sorting tailings and B part ore, due to high acid consumption and low grade, the economic benefits of heap leaching are poor, so they are directly used as final tailings; (5) The C2 process is adopted, see Figure 4 The ore in section C is subjected to reverse flotation to obtain reverse flotation concentrate c2 (calcium magnesium gangue) and copper oxide slime; the obtained copper oxide slime is then leached by wet process. Reverse flotation includes a roughing stage and a scavenging stage. The concentrate obtained from each stage is the reverse flotation concentrate C2, and the tailings obtained from the scavenging stage are the reverse flotation tailings. The tailings obtained from the roughing stage are then sent to the scavenging stage. The collector used in reverse flotation is a fatty acid collector (sodium oleate, 1.0 kg / t ore).

[0099] The experimental results show that the acid consumption for leaching the reverse flotation tailings of the color sorting concentrate is 3.20 tons of acid / ton of copper, with a leaching rate of 85.23%, and the acid consumption for leaching the copper oxide slime obtained from the C part of the ore is 4.25 tons of acid / ton of copper, with a leaching rate of 68.18%.

[0100] Comparative Example 3 The ore processed in this comparative example is the same as that in Example 2. The specific process method used in this comparative example is as follows: The raw ore is crushed to a particle size of less than 18 mm, and then all of it is fed into a ball mill for grinding. The grinding concentration is 70%, and the grinding product is classified using a hydrocyclone. The overflow fineness is -0.074 mm, accounting for 73%, resulting in slurry A with a slurry concentration of 31 wt%. Slurry A is subjected to copper sulfide flotation to obtain copper sulfide concentrate and tailings. The copper sulfide flotation includes a roughing stage, a scavenging stage, and a cleaning stage. The middlings obtained during the flotation process are returned to the previous stage of flotation. The reagents used in the copper sulfide flotation of slurry A include a collector (butyl xanthate, 35 g / ton of ore) and a frother (pine oil, 15 g / ton of ore). Copper sulfide concentrate was roasted and then wet leached to obtain copper-rich leachate A1. The tailings from the sulfur beneficiation process are sequentially subjected to desliming flotation, copper oxide flotation, and magnetic separation. The concentrate obtained from desliming flotation is copper oxide slime, and the resulting tailings are then subjected to copper oxide flotation. The concentrate obtained from copper oxide flotation is copper oxide concentrate, and the resulting tailings are then subjected to magnetic separation. The concentrate obtained from magnetic separation is magnetic separation concentrate, and the resulting tailings are magnetic separation tailings. The copper oxide slime, copper oxide concentrate, and magnetic separation concentrate are then subjected to wet leaching. The specific beneficiation process is as follows: Pine oil (15g / ton of ore) was added to the sulfur tailings for a first-stage desliming flotation. The resulting concentrate was copper oxide slime, and the resulting tailings were the tailings from the desliming flotation. The tailings from the desliming flotation are subjected to copper oxide flotation, which includes two roughing stages and two scavenging stages. The concentrate obtained from each stage is copper oxide concentrate, and the tailings obtained from the last stage are the tailings from copper oxide flotation. The tailings obtained from each stage except the last stage enter the next stage of flotation. The reagents used in copper oxide flotation include sulfiding agent (sodium hydrosulfide, 3.5 kg / ton of ore) and collector (butyl xanthate, 350 g / ton of ore). The tailings from copper oxide flotation are separated using a high-gradient magnetic separator, which includes a roughing stage and a cleaning stage. The tailings obtained from the roughing stage are magnetic tailings, the tailings obtained from the cleaning stage are returned to the roughing stage, and the concentrate obtained from the cleaning stage is magnetic concentrate. The field strengths for the roughing and cleaning stages are 1.2T and 1.0T, respectively.

[0101] Ultimately, the total copper recovery rate was only 49.61%, with a significant loss of metal. This was partly due to the low grade of the raw ore, which naturally leads to a lower recovery rate, and partly due to the poor selectivity of the large amount of severely muddy fine particles, which worsened flotation and thus resulted in a low recovery rate. Furthermore, the flotation reagents used in this case—sodium hydrosulfide, butyl xanthate, and pine oil—were used in large quantities, resulting in high reagent costs. The total acid consumption for leaching each concentrate was 15.11 tons of acid per ton of copper, with a leaching rate of 63.31%, mainly due to the high acid consumption caused by the presence of calcium-magnesium gangue in the ore. Moreover, all ores in this case required grinding, significantly increasing grinding costs (grinding workshop construction, auxiliary materials, energy consumption, etc.).

[0102] Comparative Example 4 The ore processed in this comparative example is the same as that in Example 2. The specific process method used in this comparative example is as follows: The raw ore is crushed to a particle size of less than 18 mm, and then all of it is fed into a ball mill for grinding. The grinding concentration is 70%, and the grinding product is classified using a hydrocyclone. The overflow fineness is -0.074 mm, accounting for 73 wt%, resulting in slurry A with a slurry concentration of 31 wt%. Slurry A is subjected to copper sulfide flotation to obtain copper sulfide concentrate and tailings. The copper sulfide flotation includes a roughing stage, a scavenging stage, and a cleaning stage. The middlings obtained during the flotation process are returned to the previous stage of flotation. The reagents used in the copper sulfide flotation of slurry A include a collector (butyl xanthate, 35 g / ton of ore) and a frother (pine oil, 15 g / ton of ore). The sulfur tailings are directly leached by wet leaching, while the copper sulfide concentrate is leached by wet leaching after roasting.

[0103] Ultimately, the combined leaching acid consumption of copper sulfide concentrate and tailings was 35.14 tons of acid per ton of copper. This ore contains a large amount of calcium-magnesium gangue, resulting in very high acid consumption and a leaching rate of 55.32%. In addition, all ores in this case required grinding, which greatly increased grinding costs and resulted in high beneficiation costs.

[0104] Comparative Example 5 The ore processed in this comparative example is the same as that in Example 2. The specific process method used in this comparative example is as follows: The raw ore is crushed to a particle size of less than 18 mm, and then all of it is fed into a ball mill for grinding. The grinding concentration is 70%, and the grinding product is classified using a hydrocyclone. The overflow fineness is -0.074 mm, accounting for 73 wt%, resulting in slurry A with a slurry concentration of 31 wt%. Slurry A is subjected to copper sulfide flotation to obtain copper sulfide concentrate and tailings. The copper sulfide flotation includes a roughing stage, a scavenging stage, and a cleaning stage. The middlings obtained during the flotation process are returned to the previous stage of flotation. The reagents used in the copper sulfide flotation of slurry A include a collector (butyl xanthate, 35 g / ton of ore) and a frother (pine oil, 15 g / ton of ore). The sulfur tailings are subjected to reverse flotation to obtain reverse flotation concentrate (calcium-magnesium gangue) and high-copper tailings. The reverse flotation includes a roughing stage and a scavenging stage. The concentrates obtained from each stage are reverse flotation concentrates, and the tailings obtained from the scavenging stage are reverse flotation tailings (high-copper tailings). The tailings obtained from the roughing stage are then sent to the scavenging stage. The collector used in the reverse flotation is a fatty acid collector (sodium oleate, 1.2 kg / t ore). Hydrometallurgical leaching of roasted copper sulfide concentrate; hydrometallurgical leaching of high-copper tailings.

[0105] Ultimately, the combined acid consumption for leaching copper sulfide concentrate and high-copper tailings was 7.22 tons of acid per ton of copper, which is very high, with a leaching rate of 65.35%. In addition, all ores in this case required grinding, which greatly increased grinding costs and resulted in high beneficiation costs.

[0106] Example 3 The ore processed in this embodiment is a low-grade, high-oxidation copper ore mined from the surface layer of an open-pit mine. The copper grade of the ore is 1.3wt%, the bulk density of the material is 1.72t / m³, the maximum ore particle size is 800mm, and the ore oxidation rate is 95wt%. The main useful minerals in the ore are chrysocolla, as well as small amounts of chalcocite, malachite, and lapis lazuli. The gangue is mainly composed of quartz, muscovite, feldspar, etc., and the ore is severely muddy.

[0107] The combined beneficiation and smelting process for processing low-grade, high-oxidation copper ore in this embodiment is detailed below: (1) The low-grade, high-oxidation copper ore crushed to a particle size of less than 20 mm is divided into part A, part B and part C according to the particle size; The ore mined from the mine is crushed, and the product is washed using a washing machine and classified using a vibrating screen to obtain coarse particles with a diameter of 10 mm or more, and fine particles with a diameter of less than 10 mm. The yield of the coarse particles is 55 wt%, with a copper grade of 1.25 wt%; the yield of the fine particles is 45 wt%, with a copper grade of 1.37 wt%. The fine particles are then further classified using a hydrocyclone to obtain particles with a diameter of 0.1 mm to 10 mm and particles with a diameter of less than 0.1 mm. The coarse particles with a diameter of 10 mm or more are designated as part A; the particles with a diameter of 0.1 mm to 10 mm are designated as part B; and the particles with a diameter of less than 0.1 mm are designated as part C. (2) Part A is subjected to color sorting to obtain color sorted concentrate and color sorted tailings; the color sorting uses the portion with high reflectivity in the 450nm~570nm wavelength band as the color sorted concentrate; the copper grade of the color sorted concentrate is 2.2wt%, the yield of the color sorted concentrate is 40wt%, and the enrichment ratio is 1.76; the copper grade of the color sorted tailings is 0.6wt%, and the yield of the color sorted tailings is 60wt%; (3) The color sorting concentrate is ground to a grinding concentration of 68 wt%. The grinding product is classified using a hydrocyclone, and the overflow fineness is -0.074 mm, accounting for 68 wt%, to obtain a pulp A with a pulp concentration of 28 wt%. Pulp A is subjected to copper sulfide flotation to obtain copper sulfide concentrate and sulfur tailings. The copper sulfide flotation includes a roughing stage, a scavenging stage, and a cleaning stage. The middlings obtained during the flotation process are returned to the previous stage of flotation. The reagents used in the copper sulfide flotation of pulp A include a collector (butyl xanthate, 40 g / ton of ore) and a frother (pine oil, 12 g / ton of ore). Copper sulfide concentrate was roasted and then wet leached to obtain copper-rich leachate A1. Using the A3 process, for sulfur tailings, since the main copper-bearing mineral in the ore is chrysocolla, the ore has poor beneficiation properties. Therefore, no further beneficiation is carried out. The sulfur tailings are directly wet leached to obtain copper-rich leachate A2. (4) After dehydration, the ore in part B is granulated. The added binder (carboxymethyl cellulose and hydrochloric acid resistant cement in a mass ratio of 7:3) is 4.0 wt% of the ore in part B, and the added water (as a solvent) is 14 wt% of the ore in part B. The granulation particle size is 25 mm, and then it is naturally dried and cured for 35 h to obtain cured pellets. Solidified pellets and color sorting tailings were subjected to bio-heap leaching to obtain copper-rich leachate B; The bioleaching process involved a heap height of 3 meters and a pH value of 1.8–2.0. Dilute sulfuric acid was sprayed during the bioleaching process at a concentration of 0.25 mol / L and a spraying intensity of 0.4 L / min. -1 ·m -2 ~0.6L·min-1 ·m -2 The bioleaching process uses *Thiobacillus ferrooxidans*; the inoculum size of *Thiobacillus ferrooxidans* is 20 wt%; the viable cell concentration in the *Thiobacillus ferrooxidans* inoculum is 10... 8 ~10 9 Cells / mL; the bio-heap leaching cycle is 6 months; (5) Using the C1 process, the C portion of ore is directly wet leached to obtain copper-rich leachate C.

[0108] The experimental results show that the acid consumption for leaching sulfur tailings from color sorting concentrate after regrinding and re-sorting is 2.3 tons of acid / ton of copper, with a leaching rate of 89.24%; the acid consumption for leaching from bio-heap leaching is 3.26 tons of acid / ton of copper, with a leaching rate of 79.51%; and the acid consumption for direct wet leaching of ore in section C is 3.67 tons of acid / ton of copper, with a leaching rate of 83.12%.

[0109] Comparative Example 6 The ore processed in this comparative example is the same as that in Example 3. The specific process method used in this comparative example is as follows: The raw ore is crushed to a particle size of less than 20 mm, and then all of it is fed into a ball mill for grinding. The grinding concentration is 68%. The grinding product is classified using a hydrocyclone, and the overflow fineness is -0.074 mm, accounting for 68 wt%, to obtain slurry A with a slurry concentration of 28 wt%. Slurry A is subjected to copper sulfide flotation to obtain copper sulfide concentrate and tailings. The copper sulfide flotation includes a roughing stage, a scavenging stage, and a four-stage cleaning stage. The middlings obtained during the flotation process are returned to the previous stage of flotation. The reagents used in the copper sulfide flotation of slurry A include a collector (butyl xanthate, 45 g / ton of ore) and a frother (pine oil, 15 g / ton of ore). The sulfur tailings are directly leached by wet leaching, while the copper sulfide concentrate is leached by wet leaching after roasting.

[0110] Ultimately, the combined acid consumption for leaching copper sulfide concentrate and tailings was 4.11 tons of acid per ton of copper, with a leaching rate of 86.32%. Moreover, all ores required grinding, which significantly increased grinding costs (grinding workshop construction, auxiliary materials, energy consumption, etc.).

[0111] The above description is merely a preferred embodiment of the present invention and is not intended to limit the invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A hydrometallurgical process for the treatment of low grade high oxidation copper ores, characterized in that, The application relates to a copper ore processing method. The low-grade high-oxidation-rate copper ore crushed to a particle size of 25 mm or less is divided into A, B and C parts according to particle size; the particle size of the A part is 10 mm or more; the particle size of the B part is 0.1 mm to 10 mm; the particle size of the C part is 0.1 mm or less; The A part is subjected to color selection to obtain color selection concentrate and color selection tailings; the color selection takes the part with high reflectivity in the 450 nm to 570 nm wave band as the color selection concentrate, and the enrichment ratio is 1 to 5; The color selection concentrate is ground to obtain ore pulp A; the ore pulp A is subjected to copper sulfide flotation to obtain copper sulfide concentrate and sulfur selection tailings; The obtained copper sulfide concentrate is roasted and then subjected to wet leaching to obtain copper-rich leaching liquid A1; The sulfur selection tailings are treated by one of a1 process, a2 process and a3 process to obtain copper-rich leaching liquid A2; The C part of the ore is treated by c1 process or c2 process to obtain copper-rich leaching liquid C; The a1 process: sequentially performing desliming flotation, copper oxide flotation and magnetic separation; the obtained concentrate of the desliming flotation is copper oxide slurry a1, and the obtained tailings are subjected to copper oxide flotation; the obtained concentrate of the copper oxide flotation is copper oxide concentrate, and the obtained tailings are subjected to magnetic separation; the obtained concentrate of the magnetic separation is magnetic separation concentrate, and the obtained tailings are magnetic separation tailings; the copper oxide slurry a1, the copper oxide concentrate and the magnetic separation concentrate are subjected to wet leaching; The a2 process: performing reverse flotation to obtain reverse flotation concentrate a2 and high-copper tailings as tailings; the obtained high-copper tailings are subjected to wet leaching; The a3 process: direct wet leaching; The c1 process: direct wet leaching; The c2 process: performing reverse flotation to obtain reverse flotation concentrate c2 and copper oxide slurry c2 as tailings; the obtained copper oxide slurry c2 is subjected to wet leaching; The ore oxidation rate of the low-grade high-oxidation-rate copper ore is 70 wt% or more, and the copper grade is 2 wt% or less.

2. The hydrometallurgical process for treating low grade high oxidation copper ores according to claim 1, characterized in that, The ore oxidation rate of the low-grade high-oxidation-rate copper ore is 80 wt% to 100 wt%, and the copper grade is 0.4 wt% to 1.5 wt%; The pulp concentration of the ore pulp A is 26 wt% to 38 wt%; the particle size of the ore pulp A is that the particle size of the particles with a particle size of 0.074 mm or less accounts for 65 wt% to 78 wt%.

3. The hydrometallurgical process for treating low grade high oxidation copper ores according to claim 1, characterized in that, The copper sulfide flotation of the ore pulp A includes roughing, scavenging and cleaning, wherein the cleaning stage number is 2 to 5; the obtained middlings in the flotation process are returned to the previous stage of the flotation operation; The reagent used in the copper sulfide flotation of the ore pulp A includes a collecting agent and a frother; The collecting agent used in the copper sulfide flotation of the ore pulp A includes butyl xanthate and / or amyl xanthate; The frother used in the copper sulfide flotation of the ore pulp A includes pine oil; The dosage of the collecting agent used in the copper sulfide flotation of the ore pulp A is 30 g / t of ore to 200 g / t of ore; The dosage of the frother used in the copper sulfide flotation of the ore pulp A is 5 g / t of ore to 80 g / t of ore.

4. The hydrometallurgical process for the treatment of low grade high oxidation copper ores according to claim 1, characterized in that, The desliming flotation includes one stage or two or more stages, the obtained concentrate of each stage is copper oxide slurry a1, the obtained tailings of the last stage are the tailings of the desliming flotation, and the obtained tailings of each stage except the last stage are subjected to the next stage of the flotation operation; The reagent used in desliming flotation includes pine oil, and the dosage is 3 g / t ore to 30 g / t ore.

5. The hydrometallurgical process for treating low grade high oxidation copper ores according to claim 1, characterized in that, The copper oxide flotation includes one or more than two stages, and the concentrate obtained in each stage is a copper oxide concentrate, the tailings obtained in the last stage is the tailings of copper oxide flotation, and the tailings obtained in each stage except the last stage enters the next stage of flotation operation; The reagent used in copper oxide flotation includes a sulfidizing agent and a collector; The sulfidizing agent used in copper oxide flotation includes sodium hydrosulfide and / or sodium sulfide; The collector used in copper oxide flotation includes butyl xanthate and / or amyl xanthate; The dosage of the sulfidizing agent used in copper oxide flotation is 0.8 kg / t ore to 5.0 kg / t ore; The dosage of the collector used in copper oxide flotation is 50 g / t ore to 500 g / t ore.

6. The hydrometallurgical process for processing low grade high oxidation copper ore according to claim 1, characterized in that, The magnetic separation includes roughing and cleaning, the concentrate obtained in roughing enters cleaning, the tailings obtained in roughing is the tailings of magnetic separation, the tailings obtained in cleaning returns to roughing, and the concentrate obtained in cleaning is the concentrate of magnetic separation; The field strength of the magnetic separation is 0.8 T to 1.5 T.

7. The hydrometallurgical process of claim 1, wherein the process is characterized in that, The reverse flotation includes one or more than two stages, and the concentrate obtained in each stage is a reverse flotation concentrate, the tailings obtained in the last stage is the tailings of reverse flotation, and the tailings obtained in each stage except the last stage enters the next stage of flotation operation; The collector used in reverse flotation is a fatty acid collector; The dosage of the collector used in reverse flotation is 0.5 kg / t ore to 3 kg / t ore.

8. The hydrometallurgical process according to any one of claims 1 to 7, characterized in that, The B part of ore is granulated by adding a binder and a solvent to form solidified pellets with a particle size of 5 mm to 30 mm, and is subjected to bioheap leaching together with the tailings of color selection to obtain a copper-rich leach liquor B; the bioheap leaching uses iron-oxidizing thiobacillus; the pH value of the heap leaching is 1.6 to 2.

0.

9. The hydrometallurgical process according to claim 8, characterized in that, The solvent used in granulation is water, and the amount of water used is 10 wt% to 25 wt% of the amount of the B part of ore; The dosage of the binder used in granulation is 1 wt% to 7 wt% of the amount of the B part of ore; The binder used in granulation includes carboxymethyl cellulose and sulfate-resistant cement; The carboxymethyl cellulose in the binder accounts for 50 wt% to 70 wt%; The sulfate-resistant cement in the binder accounts for 30 wt% to 50 wt%.

10. The hydrometallurgical process of claim 8, wherein the process is characterized by, The height of the bioleaching heap is 2m-4m; the leaching period of the bioleaching is 2-12 months; during the bioleaching process, dilute sulfuric acid is sprayed, the concentration of the dilute sulfuric acid is 0.1mol / L-1mol / L, and the spraying intensity of the dilute sulfuric acid is 0.1L·min -1 ·m -2 ~1L·min -1 ·m -2 ; the inoculation amount of the Acidithiobacillus ferroxidans inoculum is 10wt%-20wt%; the viable bacteria concentration in the Acidithiobacillus ferroxidans inoculum is 10 6 ~10 9 / mL.

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