Method for obtaining copper and ferrous sulfate from low-grade sulfur-oxygen mixed iron-copper ore

Abstract

The invention discloses a method for obtaining copper and ferrous sulfate from low-grade sulfur-oxygen mixed iron-copper ore, which comprises the following steps: dry-grinding the iron-copper ore, performing low-temperature roasting modification on the dry-ground ore powder to obtain modified ore powder and roasting flue gas, collecting and cooling the roasting flue gas to obtain a crystallization product, and returning the crystallization product to roasting for recycling. The modified mineral powder is subjected to enhanced acid leaching, the acid leaching condition is controlled, and acid leaching residues and leachate are obtained; extracting and reversely extracting the leachate, controlling extraction and reverse extraction conditions to obtain raffinate, copper-rich liquid and an organic phase, recycling the organic phase after acid pickling and iron removal, performing flocculating settling on the raffinate to obtain supernate and settling slag, and performing evaporative crystallization treatment on the supernate to obtain ferrous sulfate. The method can efficiently recover copper in the refractory low-grade sulfur-oxygen mixed iron-copper ore, fully utilizes iron resources, and has the characteristics of simple process, high applicability, high copper recovery rate and the like. And the follow-up emulsification risk of the copper extraction agent can be effectively reduced, and follow-up recovery of copper is facilitated.

Description

Technical Field

[0001] The invention relates to the technical field of chemical metallurgy, and in particular to a method for obtaining copper and ferrous sulfate from low-grade sulfur-oxygen mixed iron-copper ore. Background Art

[0002] As an important metal, copper is widely used in military manufacturing, new energy and other fields. Due to the large demand, the price of copper has gradually risen, and the competition for copper resources has become more and more fierce. As the copper resources that are easy to handle and have high comprehensive utilization value are becoming increasingly depleted, the copper resources that are difficult to handle, especially the low-grade sulfur-oxygen mixed iron-copper resources, have gradually received attention. At present, the main methods for processing iron-copper ores include flotation-acid leaching, direct acid leaching, flotation-magnetic separation, magnetic separation-flotation, etc., but the above methods are not suitable for processing complex low-grade sulfur-oxygen mixed iron-copper ores.

[0003] For example, the iron content in a complex low-grade sulfur-oxygen mixed iron-copper ore in Tibet is about 33%, and iron mainly exists in the form of non-magnetic limonite; the copper content is about 1%, and the proportion of copper sulfide in the copper phase is 20-30%, and the proportion of copper oxide is as high as more than 70%, and more than 70% of the copper is evenly distributed in the limonite in the form of chemical adsorption and isomorphism, not physically encapsulated. It is impossible to efficiently recover copper by using a single flotation, acid leaching, magnetic separation or combined method. Chinese invention patent CN117165778B discloses a method for recovering iron and copper by modified magnetic separation-acid leaching of high-iron copper ore. The iron-copper ore treated by this method is a non-magnetic iron oxide-encapsulated copper ore. The copper content in the copper ore is 4%, and the copper is encapsulated by iron oxide, most of which is physically encapsulated. The invention uses the modified magnetic separation + acid leaching method to recover both iron and copper in the iron-copper ore, but this method has the problem that the magnetic separation process is prone to copper loss, and it is not suitable for complex low-grade sulfur-oxygen mixed iron-copper ore in which copper is evenly distributed in the limonite in the form of chemical adsorption and isomorphism. In view of this, it is particularly necessary to develop comprehensive recovery technology for complex low-grade sulfur-oxygen mixed iron-copper ores. Summary of the invention

[0004] In view of the defects of the prior art, the present invention provides a method for simplifying the process flow, efficiently obtaining copper from low-grade sulfur-oxygen mixed iron-copper ore, and obtaining ferrous sulfate by utilizing the iron resources therein.

[0005] In order to solve the above technical problems, the present invention adopts the following technical solution: a method for obtaining copper and ferrous sulfate from low-grade sulfur-oxygen mixed iron-copper ore, characterized in that the method is carried out according to the following steps:

[0006] (1) Ore Grinding: Dry-grind the iron-copper ore to obtain dry-ground ore powder.

[0007] (2) adding ammonium sulfate and ammonium chloride to the dry-ground ore powder obtained in step (1), mixing them evenly, and then roasting and modifying them to obtain modified ore powder, wherein the amount of ammonium sulfate is 90-95% of the mass of the ore powder, the amount of ammonium chloride is 5-10% of the mass of the ore powder, the roasting temperature is 350-450° C., and the roasting time is 100-120 min.

[0008] (3) The flue gas generated in step (2) is collected and cooled to obtain an ammonium salt crystal product which is returned for roasting and recycling.

[0009] (4) The modified ore powder obtained in step (2) is subjected to enhanced acid leaching to obtain acid leaching residue and leaching liquid after enhanced solid-liquid separation, wherein the leaching liquid-solid ratio is 3:1, the leaching temperature is 40-60° C., the leaching time is 2-3 h, the amount of sulfuric acid is 8-10% of the modified ore powder, the leaching aid is sodium fluoride, the amount of which is 2-3% of the mass of the modified ore powder, and sodium fluoride is added in batches after about 30 min of acid leaching.

[0010] (5) The leaching solution obtained in step (4) is directly extracted to obtain a raffinate and a copper-containing organic phase, wherein the extractant is 15% ZJ988 + 75% sulfonated kerosene, the extraction O / A ratio is 1.7:1, and the extraction time is 3-5 minutes.

[0011] (6) stripping the copper-containing organic phase obtained in step (5) to obtain a copper-rich solution and an organic phase, wherein the stripping solution is a dilute sulfuric acid solution with a concentration of 15%, and the stripping O / A ratio is 2:1.

[0012] (7) The raffinate obtained in step (5) is subjected to flocculation and sedimentation treatment to obtain sediment residue and supernatant, wherein the flocculants are polyacrylamide and gelatin, the amount of polyacrylamide is 0.5-1 g / L, the amount of gelatin is 2-3 g / L, the flocculation temperature is 70-80°C, stirring is performed for 20-40 minutes, and standing is performed for 1-2 hours.

[0013] (8) The supernatant obtained in step (7) is subjected to evaporation and crystallization to obtain ferrous sulfate.

[0014] The iron-copper ore described in step (1) is a low-grade sulfur-oxygen mixed copper ore with a high iron content. The iron mainly exists in the form of non-magnetic limonite. The copper oxide accounts for more than 70% of the copper phase, and the copper sulfide accounts for 20-30%. More than 70% of the copper is distributed in the limonite in the form of chemical adsorption and isomorphism, not physical inclusion. In addition, the iron-copper ore is severely muddy, and its main components include: Cu: 0.9-1.2%, Fe: 30.0-35.0%, Al: 1.2%, Cu: 0.9-1.2%, Fe: 0.9-1.2%, Al: 0.9- ... 2 O 3 :7.0~8.0%、SiO 2 :11~12%, CaO: 14~15%, S: 0.8~1.5%, MgO: 0.2~0.3%.

[0015] In step (1), the grinding particle size is controlled at -0.045 mm, accounting for 100%, which is conducive to the dissociation and exposure of copper monomers.

[0016] In step (2), the roasting temperature is relatively low, i.e., 350 to 450° C., and the ratio of ammonium sulfate to ammonium chloride is 9:1 to 9.5:0.5. Too much ammonium chloride will increase the content of cuprous chloride with poor water solubility, which is not conducive to the dissolution of copper. After the dry-ground ore powder is roasted and modified by mixed ammonium salt, the copper sulfide and copper oxide in the ore powder can react with the ammonium salt to be converted into copper sulfate and copper chloride with good water solubility, and the modified ore powder presents a loose structure, which is conducive to the further release of copper.

[0017] In step (4), the copper leaching rate is greater than 85%, the iron ion content in the leachate is 15-20 g / L, the copper ion content is 1.2-1.5 g / L, and the iron-copper concentration difference is much higher than that of conventional copper oxide leachate; and the enhanced leaching agent is sodium fluoride. On the one hand, compared with calcium fluoride, sodium fluoride has better solubility in acidic solution, which is conducive to the release of fluoride ions; on the other hand, the fluoride ion has a small radius and is easier to penetrate into the mineral structure, reducing the potential difference caused by the migration of hydrogen ions, promoting the diffusion of hydrogen ions in the mineral, and strengthening the displacement and desorption of copper in the mineral by hydrogen ions. At the same time, fluoride ions can corrode minerals under acidic conditions and release copper ions adsorbed in the minerals. In addition, since the iron content of iron-copper ore is relatively high, a large amount of iron ions enter the solution during the enhanced leaching process, and some of the iron ions are trivalent. During the copper extraction process, the trivalent iron ions are hydrolyzed to generate Fe(OH) 3 The colloidal particles prevent the oil droplets from aggregating and causing severe emulsification of the copper extractant, while the presence of fluoride ions not only destroys the iron-containing emulsion, but also inhibits the formation of water-in-oil emulsions, which is beneficial to the subsequent copper extraction.

[0018] In step (5), the primary extraction rate of copper is more than 98%, and the primary extraction rate of trivalent iron is only 1-2%. The copper extractant used is ZJ988+sulfonated kerosene. The ZJ988 extractant has strong selectivity for copper and weak extraction performance for trivalent iron, but its performance for extracting trivalent iron is weaker than that of other extractants, and is suitable for extraction of copper sulfate solution with a large difference in copper and iron concentrations.

[0019] In step (7), the flocculation temperature is 70-80°C, and the flocculant used is a combination of polyacrylamide and gelatin. Gelatin has a good flocculation and silicon removal effect. The combined use can significantly reduce the impurity content of the raffinate.

[0020] Compared with the prior art, the advantages of the present invention are:

[0021] 1. Flotation-magnetic separation and magnetic separation-flotation are only applicable to iron-copper ores containing magnetic iron and copper that are easy to float. These two methods are not applicable to sulfur-oxygen mixed iron-copper ores that do not contain magnetic iron. Compared with a single flotation method, copper sulfide accounts for a small proportion in sulfur-oxygen mixed iron-copper ores, and the flotation method cannot significantly improve the recovery rate of copper oxide in sulfur-oxygen mixed iron-copper ores, resulting in a low copper recovery rate. The present invention can efficiently recover copper in difficult-to-treat low-grade sulfur-oxygen mixed iron-copper ores through the technical solution of ammonium salt roasting modification-enhanced leaching-efficient extraction-flocculation sedimentation-evaporation crystallization, and make full use of iron resources, avoiding the problem that other methods are not suitable for treating low-grade sulfur-oxygen mixed iron-copper ores, and has the characteristics of simple process, strong applicability, and high copper recovery rate.

[0022] 2. There are many problems in the direct acid leaching method for treating low-grade sulfur-oxygen mixed iron-copper ore. On the one hand, the proportion of copper sulfide in the iron-copper ore is 20-30%, and more than 70% of the copper is distributed in the limonite in the form of chemical adsorption and isomorphism. It is difficult to leach copper sulfide by direct acid leaching, resulting in low copper leaching rate and high acid consumption. On the other hand, the high iron ion content of the leachate affects the subsequent copper recovery; although the flotation-acid leaching method can effectively recover most of the copper sulfide in the iron-copper ore, most of the copper is evenly distributed in the limonite, and acid leaching cannot obtain a higher copper leaching rate. The present invention uses low-temperature roasting modification to convert most of the copper that is difficult to leach into copper with good water solubility in advance, and at the same time uses sodium fluoride to strengthen the leaching of copper, and effectively reduces the risk of emulsification of subsequent copper extractants, which is beneficial to the subsequent recovery of copper, and greatly improves the resource utilization rate of difficult-to-treat low-grade sulfur-oxygen mixed iron-copper ore. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] Figure 1 It is a process flow chart of the present invention. DETAILED DESCRIPTION

[0024] The following is combined with Figure 1 The present invention is further described by specific embodiments:

[0025] Example 1: A certain iron-copper ore in Tibet was treated according to the process of the present invention. The composition of the iron-copper ore is shown in Table 1, and the physical phase of copper is shown in Table 2:

[0026] Table 1

[0027]

[0028] Table 2

[0029]

[0030] The specific steps are as follows:

[0031] (1) Ore Grinding: Dry-grind the iron-copper ore to obtain dry-ground ore powder.

[0032] (2) adding ammonium sulfate and ammonium chloride to the dry-ground ore powder obtained in step (1), mixing the mixture and then roasting and modifying the mixture to obtain a modified ore powder, wherein the amount of ammonium sulfate is 90% of the mass of the ore powder, the amount of ammonium chloride is 10% of the mass of the ore powder, the roasting temperature is 400° C., and the roasting time is 100 min.

[0033] (3) The flue gas generated in step (2) is collected and cooled to obtain an ammonium salt crystal product which is returned for roasting and recycling.

[0034] (4) The modified ore powder obtained in step (2) is subjected to enhanced acid leaching, and acid leaching residue and leaching liquid are obtained after enhanced solid-liquid separation, wherein the leaching liquid-solid ratio is 3:1, the leaching temperature is 50° C., the leaching time is 2.5 h, the amount of sulfuric acid is 10% of the modified ore powder, the leaching aid is sodium fluoride, and the amount is 2.5% of the mass of the modified ore powder. Sodium fluoride is added in batches after acid leaching for 30 min.

[0035] (5) The leaching solution obtained in step (4) is directly extracted to obtain a raffinate and a copper-containing organic phase, wherein the extractant is 15% ZJ988 + 75% sulfonated kerosene, the extraction O / A ratio is 1.7:1, and the extraction time is 3 min.

[0036] (6) stripping the copper-containing organic phase obtained in step (5) to obtain a copper-rich solution and an organic phase, wherein the stripping solution is a dilute sulfuric acid solution with a concentration of 15%, and the stripping O / A ratio is 2:1.

[0037] (7) The raffinate obtained in step (5) is subjected to flocculation and sedimentation treatment to obtain sediment residue and supernatant, wherein the flocculants are polyacrylamide and gelatin, the amount of polyacrylamide is 1 g / L, the amount of gelatin is 2 g / L, the flocculation temperature is 80°C, stirring for 20 minutes, and standing for 1 hour.

[0038] (8) The supernatant obtained in step (7) is subjected to evaporation and crystallization to obtain ferrous sulfate.

[0039] In this embodiment, a copper-rich solution (which can be used for direct electrowinning) with a copper content of 47.5 g / L and a total copper recovery rate of 85.21% and a ferrous sulfate crystal product with a purity of 90.32% are finally obtained.

[0040] Example 2: A certain iron-copper ore in Tibet was treated according to the process of the present invention. The composition of the iron-copper ore is shown in Table 3, and the copper phase is shown in Table 4:

[0041] Table 3

[0042]

[0043] Table 4

[0044]

[0045] The specific steps are as follows:

[0046] (1) Ore Grinding: Dry-grind the iron-copper ore to obtain dry-ground ore powder.

[0047] (2) adding ammonium sulfate and ammonium chloride to the dry-ground ore powder obtained in step (1), mixing them evenly, and then roasting and modifying them to obtain modified ore powder, wherein the amount of ammonium sulfate is 95% of the mass of the ore powder, the amount of ammonium chloride is 5% of the mass of the ore powder, the roasting temperature is 360° C., and the roasting time is 120 min.

[0048] (3) The flue gas generated in step (2) is collected and cooled to obtain an ammonium salt crystal product which is returned for roasting and recycling.

[0049] (4) The modified ore powder obtained in step (2) is subjected to enhanced acid leaching, and acid leaching residue and leaching liquid are obtained after enhanced solid-liquid separation, wherein the leaching liquid-solid ratio is 3:1, the leaching temperature is 40° C., the leaching time is 3 h, the amount of sulfuric acid is 8% of the modified ore powder, the leaching aid is sodium fluoride, and the amount is 3% of the mass of the modified ore powder. Sodium fluoride is added in batches after acid leaching for 30 min.

[0050] (5) The leaching solution obtained in step (4) is directly extracted to obtain a raffinate and a copper-containing organic phase, wherein the extractant is 15% ZJ988 + 75% sulfonated kerosene, the extraction O / A ratio is 1.7:1, and the extraction time is 3 min.

[0051] (6) stripping the copper-containing organic phase obtained in step (5) to obtain a copper-rich solution and an organic phase, wherein the stripping solution is a dilute sulfuric acid solution with a concentration of 15%, and the stripping O / A ratio is 2:1.

[0052] (7) The raffinate obtained in step (5) is subjected to flocculation and sedimentation treatment to obtain sediment residue and supernatant, wherein the flocculants are polyacrylamide and gelatin, the amount of polyacrylamide is 0.5 g / L, the amount of gelatin is 2.5 g / L, the flocculation temperature is 77°C, stirring is performed for 30 minutes, and standing is performed for 2 hours.

[0053] (8) The supernatant obtained in step (7) is subjected to evaporation and crystallization to obtain ferrous sulfate.

[0054] In this embodiment, a copper-rich solution (which can be used for direct electrowinning) with a copper content of 51.8 g / L and a total copper recovery rate of 85.92% and a ferrous sulfate crystal product with a purity of 89.10% are finally obtained.

[0055] Example 3: A certain iron-copper ore in Tibet was treated according to the process of the present invention. The composition of the iron-copper ore is shown in Table 5, and the copper phase is shown in Table 6:

[0056] Table 5

[0057]

[0058] Table 6

[0059]

[0060] The specific steps are as follows:

[0061] (1) Ore Grinding: Dry-grind the iron-copper ore to obtain dry-ground ore powder.

[0062] (2) adding ammonium sulfate and ammonium chloride to the dry-ground ore powder obtained in step (1), mixing them evenly, and then roasting and modifying them to obtain modified ore powder, wherein the amount of ammonium sulfate is 92% of the mass of the ore powder, the amount of ammonium chloride is 8% of the mass of the ore powder, the roasting temperature is 450° C., and the roasting time is 110 min.

[0063] (3) The flue gas generated in step (2) is collected and cooled to obtain an ammonium salt crystal product which is returned for roasting and recycling.

[0064] (4) The modified ore powder obtained in step (2) is subjected to enhanced acid leaching, and acid leaching residue and leaching liquid are obtained after enhanced solid-liquid separation, wherein the leaching liquid-solid ratio is 3:1, the leaching temperature is 60° C., the leaching time is 3 h, the amount of sulfuric acid is 10% of the modified ore powder, the leaching aid is sodium fluoride, and the amount is 3% of the mass of the modified ore powder. Sodium fluoride is added in batches after acid leaching for 30 min.

[0065] (5) The leaching solution obtained in step (4) is directly extracted to obtain a raffinate and a copper-containing organic phase, wherein the extractant is 15% ZJ988 + 75% sulfonated kerosene, the extraction O / A ratio is 1.7:1, and the extraction time is 3 min.

[0066] (6) stripping the copper-containing organic phase obtained in step (5) to obtain a copper-rich solution and an organic phase, wherein the stripping solution is a dilute sulfuric acid solution with a concentration of 15%, and the stripping O / A ratio is 2:1.

[0067] (7) The raffinate obtained in step (5) is subjected to flocculation and sedimentation treatment to obtain sediment residue and supernatant, wherein the flocculants are polyacrylamide and gelatin, the amount of polyacrylamide is 0.7 g / L, the amount of gelatin is 3 g / L, the flocculation temperature is 70°C, stirring is 40 minutes, and standing is 2 hours.

[0068] (8) The supernatant obtained in step (7) is subjected to evaporation and crystallization to obtain ferrous sulfate.

[0069] In this embodiment, a copper-rich solution (which can be used for direct electrowinning) with a copper content of 50.3 g / L and a total copper recovery rate of 86.52% and a ferrous sulfate crystal product with a purity of 89.93% are finally obtained.

[0070] The present invention has been described in detail above. The above description is only a preferred embodiment of the present invention and should not limit the scope of implementation of the present invention. That is, all equivalent changes and modifications made within the scope of this application should still fall within the scope of the present invention.

Claims

1. A method for obtaining copper and ferrous sulfate from low-grade sulfur-oxygen mixed iron-copper ore, characterized in that: Follow these steps: (1) Grinding: Dry grinding the iron and copper ore to obtain dry ground ore powder; (2) adding ammonium sulfate and ammonium chloride to the dry-ground ore powder obtained in step (1), mixing them evenly, and then roasting and modifying them to obtain modified ore powder; wherein the amount of ammonium sulfate is 90-95% of the mass of the ore powder, the amount of ammonium chloride is 5-10% of the mass of the ore powder, the roasting temperature is 350-450° C., and the roasting time is 100-120 min; (3) collecting the flue gas generated in step (2), cooling the obtained ammonium salt crystal product and returning it to the roasting cycle for reuse; (4) performing enhanced acid leaching on the modified ore powder obtained in step (2), and obtaining acid leaching residue and leachate after enhanced solid-liquid separation; (5) directly extracting the leaching solution obtained in step (4) to obtain a raffinate and a copper-containing organic phase, wherein the extractant is sulfonated kerosene and the extraction time is 3-5 min; (6) stripping the copper-containing organic phase obtained in step (5) to obtain a copper-rich solution and an organic phase, wherein the stripping solution is a dilute sulfuric acid solution; (7) subjecting the raffinate obtained in step (5) to flocculation and sedimentation treatment to obtain sediment residue and supernatant, wherein the flocculants are polyacrylamide and gelatin, the amount of polyacrylamide is 0.5-1 g / L, the amount of gelatin is 2-3 g / L, the flocculation temperature is 70-80° C., stirring for 20-40 min, and standing for 1-2 h; (8) subjecting the supernatant obtained in step (7) to evaporation and crystallization to obtain ferrous sulfate.

2. The method for obtaining copper and ferrous sulfate from low-grade sulfur-oxygen mixed iron-copper ore according to claim 1, characterized in that: The iron-copper ore described in step (1) is a low-grade sulfur-oxygen mixed copper ore, in which iron mainly exists in the form of non-magnetic limonite, copper oxide accounts for more than 70% of the copper phase, copper sulfide accounts for 20-30%, and more than 70% of the copper is distributed in the limonite in the form of chemical adsorption and isomorphism, not physical inclusion, and the main components include: Cu: 0.9-1.2%, Fe: 30.0-35.0%, Al2O3: 7.0-8.0%, SiO2: 11-12%, CaO: 14-15%, S: 0.8-1.5%, MgO: 0.2-0.3%.

3. The method for obtaining copper and ferrous sulfate from low-grade sulfur-oxygen mixed iron-copper ore according to claim 1, characterized in that: In step (1), the grinding particle size is controlled at -0.045 mm, accounting for 100%, so as to facilitate the dissociation and exposure of copper monomers.

4. The method for obtaining copper and ferrous sulfate from low-grade sulfur-oxygen mixed iron-copper ore according to claim 1, characterized in that: In step (2), the roasting temperature is 350-450° C., the ratio of ammonium sulfate to ammonium chloride is 9:1-9.5:0.5, and after the dry-ground ore powder is roasted and modified by mixed ammonium salt, the copper sulfide and copper oxide in the ore powder react with the ammonium salt to be converted into copper sulfate and copper chloride with good water solubility, and the modified ore powder presents a loose structure, which is conducive to the further release of copper.

5. The method for obtaining copper and ferrous sulfate from low-grade sulfur-oxygen mixed iron-copper ore according to claim 1, characterized in that: In step (4), the copper leaching rate is greater than 85%, the iron ion content in the leaching solution is 15-20 g / L, and the copper ion content is 1.2-1.5 g / L; the enhanced leaching aid used in the enhanced acid leaching process is sodium fluoride.

6. The method for obtaining copper and ferrous sulfate from low-grade sulfur-oxygen mixed iron-copper ore according to claim 1, characterized in that: In step (5), the primary extraction rate of copper is above 98%, the primary extraction rate of trivalent iron is 1-2%, and the copper extractant used is ZJ988+sulfonated kerosene.

7. The method for obtaining copper and ferrous sulfate from low-grade sulfur-oxygen mixed iron-copper ore according to claim 1, characterized in that: In step (7), the flocculation temperature is 70-80° C., and the flocculant used is a combination of polyacrylamide and gelatin to improve the flocculation and silicon removal effect and reduce the impurity content of the raffinate.

8. The method for obtaining copper and ferrous sulfate from low-grade sulfur-oxygen mixed iron-copper ore according to claim 1, characterized in that: In step (4), the modified ore powder is subjected to enhanced acid leaching to obtain a leaching liquid-to-solid ratio of 3:1, the leaching temperature is 40-60° C., and the leaching time is 2-3 hours; sulfuric acid is used for acid leaching, and the amount of sulfuric acid is 8-10% of the modified ore powder; sodium fluoride is used as a leaching aid, and the amount of sodium fluoride is 2-3% of the mass of the modified ore powder. Sodium fluoride is added in batches after acid leaching for 30 minutes.

9. The method for obtaining copper and ferrous sulfate from low-grade sulfur-oxygen mixed iron-copper ore according to claim 1, characterized in that: In step (5), the extractant is 15% ZJ988 + 75% sulfonated kerosene, and the extraction O / A ratio is 1.7:

1.

10. The method for obtaining copper and ferrous sulfate from low-grade sulfur-oxygen mixed iron-copper ore according to claim 1, characterized in that: In step (6), the stripping solution is a 15% dilute sulfuric acid solution, and the stripping O / A ratio is 2:1.

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