Method for recovering valuable metals based on pyrite and high-manganese low-cobalt type asbolite double-ore enhanced leaching

Abstract

The invention discloses a method for recovering valuable metals based on pyrite and high-manganese low-cobalt type asbolite double-ore enhanced leaching, and belongs to the technical field of mineral processing and metallurgy. The method comprises the following steps: mixing high-manganese low-cobalt type asbolite powder and pyrite powder, leaching by adopting a sulfuric acid solution, firstly extracting and reversely extracting a leaching solution by adopting a Lix984 extraction system to recover copper, removing iron by adopting a sodium jarosite method, and finally extracting and reversely extracting by adopting a Versatic10 extraction system to recover cobalt, so as to obtain manganese-containing raffinate. According to the method, leaching of valuable metals in high-manganese low-cobalt type asbolite is strengthened through pyrite, meanwhile, a combined process of extracting and separating copper through Lix984, removing iron through a sodium jarosite method and extracting and separating cobalt through Versatic 10 is adopted, efficient separation of the valuable metals such as copper, cobalt and manganese is sequentially achieved, the method is short in technological process, the agent consumption cost is low, and the method is suitable for industrial production. The resource utilization of the high-manganese low-cobalt type asbolite is realized.

Description

Technical Field

[0001] The present invention relates to a metallurgical method for pyrite and cobalt ore, and in particular to a method for recovering valuable metals by enhanced leaching of pyrite and high-manganese, low-cobalt cobalt ore, belonging to the technical field of mineral processing and metallurgy. Background Art

[0002] Traditional cobalt ore processing technology generally relies on sulfur dioxide (SO2) gas or coke as a reducing agent, which has significant environmental and process defects. Although sulfur dioxide reduction can partially reduce high-valent metals (such as Co 3+ 、Mn 4+ ), but its strong corrosiveness shortens equipment life by 30% to 50%, and the SO2 emission limit in the tail gas is strict (usually <50ppm), resulting in high processing costs; the coke high-temperature reduction method needs to operate above 800°C, with energy consumption of 200 to 300kWh per ton of ore, increasing carbon emissions by more than 40%, and ash impurities (such as silicon and aluminum) mixed into the slag, reducing the purity of the leachate and increasing the difficulty of subsequent separation.

[0003] Direct acid leaching is extremely inefficient for extracting valuable metals from untreated cobalt ore. This is because high-valent oxides (MnO₂ and Co₃O₄) are insoluble in dilute acid. Leaching rates for cobalt and manganese are generally below 20%, and copper is less than 15%. Existing reduction leaching methods can effectively improve the leaching rates of metals like cobalt and manganese. For example, a Chinese patent application (publication number: CN1401799A) discloses the use of pyrite as a reducing agent to leach the valuable elements Co, Ni, Mn, and Cu from cobalt ore, achieving leaching rates of 92-95% for Co, 95-96% for Mn, and 55-60% for Ni. While this method effectively improves the leaching rate of valuable metals, it does not achieve separation and recovery of metal ions. A Chinese patent application (publication number: CN102021331A) discloses processing high-manganese cobalt ore through four process steps: reduction leaching, preliminary purification, manganese and cobalt separation, and extraction separation to obtain manganese carbonate, copper sulfate, nickel carbonate, and cobalt chloride or cobalt sulfate products. However, the process is very complicated, inefficient, and has high reagent costs, making it unsuitable for industrial production. Summary of the Invention

[0004] In response to the technical problems existing in the cobalt ore processing process in the prior art, the object of the present invention is to provide a method for recovering valuable metals based on the enhanced leaching of pyrite and high-manganese, low-cobalt cobalt ore. The method is based on the synergistic leaching of pyrite and high-manganese, low-cobalt cobalt ore, which can enhance the leaching of valuable metals such as cobalt, manganese, and copper in the cobalt ore under mild conditions. On this basis, a combined process of Lix984 extraction and separation of copper, sodium ferroaluminate method for iron removal, and Versatic 10 extraction and separation of cobalt is adopted to sequentially achieve efficient separation and recovery of valuable metals such as copper, cobalt, and manganese, and can effectively avoid interference from impurity metal ions. The method has a short process flow, low reagent consumption cost, and realizes the resource utilization of high-manganese, low-cobalt cobalt ore.

[0005] In order to achieve the above technical objectives, the present invention provides a method for recovering valuable metals by enhanced leaching of pyrite and high-manganese, low-cobalt cobaltite, which comprises the following steps:

[0006] (1) mixing cobalt clay ore powder with high-manganese, low-cobalt pyrite powder and leaching with sulfuric acid solution to obtain a leachate containing cobalt, manganese, copper and iron;

[0007] (2) The leaching solution containing cobalt, manganese, copper and iron is subjected to extraction and back extraction using the Lix984 extraction system to recover copper, thereby obtaining a raffinate containing cobalt, manganese and iron;

[0008] (3) removing iron from the raffinate containing cobalt, manganese and iron by a sodium ferroalloy method to obtain an iron-removing liquid containing cobalt and manganese;

[0009] (4) The iron removal liquid containing cobalt and manganese is subjected to extraction and back extraction using the Versatic 10 extraction system to recover cobalt and obtain a manganese-containing raffinate.

[0010] The present invention is based on the characteristics of high manganese, low cobalt type cobalt ore with low cobalt grade and the high-valent oxides (Co3O4, MnO2) contained in it being difficult to dissolve in dilute acid, which is the main reason for the low leaching rate of cobalt and manganese therein. The present invention adopts a collaborative leaching method of pyrite and high manganese, low cobalt type cobalt ore. The use of pyrite as a reducing agent can promote the efficient reduction leaching of high-valent cobalt and manganese (Co3O4, MnO2) in the high manganese, low cobalt type cobalt ore under relatively mild conditions. The obtained leachate mainly contains Co 2+ 、Mn 2 + 、Cu 2+ and Fe 3+ Valuable metal ions such as Co are produced by using a short process and low cost method. 2+ 、Mn 2+ 、Cu 2+ and Fe 3+ The efficient separation of valuable metal ions is one of the important innovations of the present invention. 2+Compared with other metal ions, it is the most important metal ion to affect the removal of Fe by sodium ferroaluminate. 3+ The present invention preferentially uses Lix984 extraction system to extract and separate Cu 2+ , Lix984 extraction system can achieve Cu 2+ High efficiency recovery, while reducing Co 2+ 、Mn 2+ On this basis, a sulfuric acid leaching system is used based on the reduction leaching process, and almost all the iron in the leachate is Fe 3+ It exists in the form of sodium ferroaluminate method to remove Fe 3+ Provides favorable conditions, while the sodium ferroaluminate method has a great impact on Fe 3+ Remove thoroughly and selectively, avoiding Co 2+ 、Mn 2+ The loss will eventually 2+ With Mn 2+ The present invention adopts the Versatic 10 extraction system, which is effective for the separation of Co 2+ The extraction selectivity is good, Co 2+ With Mn 2+ High separation coefficient, capable of achieving Co 2+ With Mn 2+ Efficient separation and recovery. In summary, the present invention adopts a combined process of Lix984 extraction and separation of copper, natantrolite method for iron removal, and Versatic10 extraction and separation of cobalt, which can achieve efficient separation and recovery of valuable metals such as copper, iron, cobalt, and manganese.

[0011] As a preferred embodiment, the mass ratio of the high-manganese, low-cobalt cobalt earth ore powder to the pyrite powder is 100:5-20. If the pyrite dosage is too low (<5%), the reduction leaching of the high-valent cobalt and manganese in the high-manganese, low-cobalt cobalt earth ore will be insufficient. If the pyrite dosage is too high (>20%), excessive iron impurities will be introduced, increasing the burden of subsequent iron removal and increasing sulfuric acid consumption by more than 15%. The mass ratio of the high-manganese, low-cobalt cobalt earth ore powder to the pyrite powder is more preferably 100:10-15.

[0012] As a preferred solution, the high-manganese, low-cobalt cobalt ore is an oxidized mineral with a cobalt grade of 0.3% to 0.5% and a manganese grade of 10% to 15%. The main phases of the high-manganese, low-cobalt cobalt ore include pyrolusite, kaolinite, hematite, and chlorite.

[0013] As a preferred solution, the leaching conditions are: the concentration of the sulfuric acid solution is 20~50g / L, the leaching liquid-solid ratio is 2~4L:1kg, the stirring rate is 200~300r / min, the leaching temperature is 50~90°C, and the leaching time is 3~5 hours. Under the preferred leaching conditions, efficient leaching of valuable metals in high-manganese, low-cobalt cobalt ore powder can be guaranteed. The concentration of the sulfuric acid solution is further preferably 35~45g / L. The leaching temperature is further preferably 75~85°C. The leaching liquid-solid ratio is further preferably 3~4L:1kg. Under optimized conditions, the cobalt leaching rate is ≥95.47%, the manganese leaching rate is ≥79.11%, and the copper leaching rate is ≥84.32%.

[0014] As a preferred solution, in step (2), the extraction is 2 to 4 stages of countercurrent extraction, the extraction phase ratio O / A is 1:2 to 2:1, the mass concentration of the Lix984 extractant in the organic phase is 5 to 20%, the contact time of each stage of extraction is 5 to 10 minutes, and the extraction pH is controlled in the range of 1 to 2. The "relatively speaking" in the present invention refers to the phase volume ratio. Sulfonated kerosene is used as a diluent in the organic phase. Under the preferred extraction conditions, especially when the pH is controlled in the range of 1 to 2, the extraction efficiency of the Lix984 extractant for Cu can be improved. 2+ The selective extraction effect reduces Co 2+ With Mn 2+ The pH is generally adjusted using a 1 mol / L sodium hydroxide solution.

[0015] As a preferred solution, in step (2), the stripping stage is 1 to 2, the stripping solution is a 1.0 to 2.0 mol / L sulfuric acid solution, and the stripping phase ratio O / A is 1:1 to 3:1.

[0016] The present invention adopts the Lix984 extraction-sulfuric acid stripping process, and under preferred conditions, the copper recovery rate is ≥99.68%.

[0017] As a preferred solution, the process of removing iron by the sodium ferroalite method is as follows: adding sodium ferroalite seed crystals to the raffinate containing cobalt, manganese and iron, adjusting the pH to 2.0-2.5, and reacting at 50-90°C for 0.5-2 hours. 3+ Good selectivity, removing Fe 3+ Thoroughly, under optimal conditions, the iron removal rate is ≥98%.

[0018] As a more preferred solution, the amount of the sodium ferrosite seed crystals added to the raffinate containing cobalt, manganese and iron is 0.5wt.%~1.0wt.%. By introducing an appropriate amount of sodium ferrosite seed crystals, Fe 3+ Accelerates crystallization in the form of sodium ferroalloy.

[0019] As a preferred solution, in step (4), the extraction is 2 to 4 stages of countercurrent extraction, the extraction phase ratio O / A is 1:2 to 2:1, the mass concentration of the Versatic10 extractant in the organic phase is 5 to 20%, the contact time of each stage of extraction is 5 to 10 minutes, and the extraction pH is controlled in the range of 5 to 6. Sulfonated kerosene is used as a diluent for the organic phase. The pH is generally adjusted using a sodium hydroxide solution with a concentration of 1 mol / L. The Versatic10 extractant does not need to be saponified. Under the preferred extraction conditions, especially when the pH is controlled in the range of 5 to 6, the Versatic10 extractant can effectively improve the Co 2+ The extraction selectivity of Versatic10 was also improved, while the extraction of Mn 2+ The extraction of cobalt and manganese can significantly improve the separation coefficient β (Co / Mn). The pH is generally adjusted with a sodium hydroxide solution with a concentration of 1 mol / L.

[0020] As a preferred solution, in step (4), the stripping stage is 1 to 2, the stripping solution is a 0.5 to 1.5 mol / L sulfuric acid solution, and the stripping phase ratio O / A is 1:1 to 1:3.

[0021] The present invention adopts the Versatic10 extraction-sulfuric acid stripping process. Under preferred conditions, the recovery rate of cobalt is ≥99.55%, and the cobalt and manganese separation effect is good.

[0022] The high-manganese, low-cobalt cobalt earth ore powder of the present invention is obtained by wet ball milling, screening and drying the high-manganese, low-cobalt cobalt earth ore, which is ball milled to a particle size of about 2 mm, and then the ore pulp is screened using 200 mesh, and the screened material is dried to obtain the high-manganese, low-cobalt cobalt earth ore powder.

[0023] Compared with the prior art, the technical solution of the present invention has the following beneficial technical effects:

[0024] (1) The technical solution of the present invention adopts pyrite to cooperate with high-manganese, low-cobalt cobalt ore reduction leaching, which can achieve efficient leaching of high-valent metals (Co3O4, MnO2) in high-manganese, low-cobalt cobalt ore under mild conditions, avoid the use of traditional sulfur dioxide reducing agents, completely eliminate the risk of sulfur pollution, and at the same time save the roasting process to reduce carbon emissions. Dilute acid leaching can be used, and the sulfuric acid concentration is optimized to 40g / L (the traditional process requires 100g / L), reducing acid mist emissions and waste liquid treatment pressure.

[0025] (2) The technical solution of the present invention has a high leaching rate for valuable metals in high-manganese, low-cobalt cobalt ore, for example, the cobalt leaching rate is ≥95% (traditional process <80%), the manganese leaching rate is ≥78%, and the copper leaching rate is ≥84%. Moreover, through the combined process of Lix984 extraction and separation of copper, sodium iron alum method for iron removal, and Versatic 10 extraction and separation of cobalt, the metal separation effect is good and the recovery rate is high, the copper recovery rate is as high as 99%, the cobalt recovery rate is ≥99%, and the impurity iron removal rate is >98%.

[0026] (3) The technical solution of the present invention eliminates the roasting furnace system, which reduces equipment investment and direct costs. In addition, the process flow is short and the production efficiency is high, which is conducive to industrial production. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 It is a process flow chart of the present invention.

[0028] Figure 2 The thermodynamic calculation data of the reduction process in the leaching process in Example 1 shows that the addition of pyrite can reduce the high-valent cobalt and manganese in the raw materials to low-valent forms under medium and low temperature conditions, which has an enhanced effect on leaching.

[0029] Figure 3 This is the XRD comparison diagram of the high-manganese, low-cobalt cobalt ore before and after leaching in Example 1. It can be seen that the hard manganese mineral phase in the original ore disappears after co-leaching with pyrite, indicating that the high-valent manganese in the original ore is reduced to a low-valent state. DETAILED DESCRIPTION

[0030] The following examples are intended to further illustrate the present invention in detail, but are not intended to limit the scope of protection of the claims of the present invention.

[0031] In the following specific examples, X-ray diffraction (XRD) and X-ray fluorescence spectroscopy (XRF) were used to analyze the phase composition of the roasted product and the leached residue, and inductively coupled plasma (ICP) was used to detect the concentrations of elements such as cobalt and manganese in the leachate.

[0032] The chemical agents used in the following specific examples are all conventional commercially available products.

[0033] Example 1

[0034] The main components and mass content of a cobalt ore raw material in Yunnan are: Co0.38%, Mn10.95%, Cu0.52%, Fe3.12%.

[0035] The main components and mass content of pyrite raw materials are: Fe45.2%, S48.5%, SiO23.1%.

[0036] 1. Raw material pretreatment:

[0037] The raw ores were crushed and wet-milled to a particle size of ≤74 μm (200 mesh) and dried at 105 °C for 12 h.

[0038] Effect: The specific surface area of ​​the mineral powder reaches over 3200 cm² / g, which is beneficial for subsequent leaching.

[0039] 2. Restore the mixture:

[0040] Cobalt ore powder and pyrite powder are mixed in a mass ratio of 100:10 (i.e. the mass of pyrite is 10% of the mass of cobalt ore powder).

[0041] Effect: Pyrite acts as a reducing agent to avoid high-temperature roasting and reduce energy consumption.

[0042] 3. Acid leaching:

[0043] The concentration of sulfuric acid was 40 g / L, the liquid-to-solid ratio was 4:1 L / kg, stirring was carried out at a constant temperature of 85°C for 4 hours, and the stirring speed was 250 r / min.

[0044] Effect: Co leaching rate is 96.2%; Mn leaching rate is 80.3%; Cu leaching rate is 84.8%; Fe leaching rate is 98.5%.

[0045] 4. Solid-liquid separation: Filter the leached slurry, wash the residue twice with deionized water (liquid-solid ratio 1:1), and combine the filtrates.

[0046] Effect: Total metal recovery rate>99.5%, residual cobalt in slag<0.02%.

[0047] 5. Copper extraction (three-stage countercurrent extraction):

[0048] Organic phase: 10% Lix984 + 90% sulfonated kerosene.

[0049] The pH was adjusted to 1.5 using 1 mol / L sodium hydroxide solution, the extraction O / A ratio was 1:1, and the contact time was 8 min / stage.

[0050] Stripping: 1.5mol / L H2SO4, O / A=2:1, 1st stage stripping.

[0051] Results: Cu recovery rate was 99.65%; Cu concentration in stripping solution was 31.2 g / L; total loss rate of Co and Mn was less than 0.3%.

[0052] 6. Iron removal by sodium ferroaluminate method: Add 0.7% sodium ferroaluminate seed crystals to the raffinate, adjust the pH to 2.3, and react at 90℃ for 1.5 hours.

[0053] Effect: Fe removal rate is 99.1%; total loss rate of Co and Mn is less than 0.5%.

[0054] 7. Cobalt extraction (three-stage countercurrent extraction): Organic phase: 10% Versatic10 + 90% sulfonated kerosene.

[0055] The pH was adjusted to 5.5 using 1 mol / L sodium hydroxide solution, the extraction O / A ratio was 1:1, and the contact time was 10 min / stage.

[0056] Stripping: 1.0 mol / LH2SO4, O / A=1:2, 1st stage stripping.

[0057] Effect: The Co recovery rate was 99.55%, the cobalt-manganese separation coefficient β (Co / Mn) reached 350, and the Co concentration in the stripping solution was 28.5 g / L.

[0058] Mn in manganese raffinate 2+ Purity>99.5%.

[0059] Example 2

[0060] The raw material composition of a low-grade cobalt ore in Congo is: Co0.22%, Mn8.73%, Cu0.31%, Fe2.85%.

[0061] The main components and mass content of pyrite raw materials are: Fe45.2%, S48.5%, SiO23.1%.

[0062] Steps 1 and 2 refer to Example 1.

[0063] 3. Acid leaching: Sulfuric acid concentration is 40 g / L, liquid-to-solid ratio is 4:1 L / kg, constant temperature stirring is 80℃ for 4 hours, stirring speed is 250 r / min.

[0064] Effect: Co leaching rate is 94.7%; Mn leaching rate is 76.3%; Cu leaching rate is 82.1%; Fe leaching rate is 97.6%.

[0065] Steps 4 and 5 refer to Example 1.

[0066] 6. Iron removal by sodium ferroalloy method: Add 0.9wt.% sodium ferroalloy seed crystals to the raffinate, adjust the pH in two stages (2.5 to 2.0), and react at 90℃ for 1.5 hours.

[0067] Effect: Fe removal rate is 98.8%; total loss rate of Co and Mn is less than 0.5%.

[0068] Step 7 refers to Example 1.

[0069] Comprehensive recovery rate: Cu 99.71%, Co 99.52%, Fe removal rate 98.8%.

[0070] Comparative Example 1

[0071] Compared with Example 1, the only difference is that steps 5 and 6 are replaced, that is, the iron removal by the yellow sodium ferroalloy method in step 6 is performed first, and then the copper extraction in step 5 is performed. The other steps are referred to Example 1.

[0072] question:

[0073] During the iron removal process using sodium ferroalloy, Cu 2+ with Fe 3+ Co-precipitation, the copper loss rate is as high as 18.3%.

[0074] During the copper extraction process, a small amount of iron (Fe < 0.1 g / L) remained in the raffinate, interfering with the cobalt extraction, and the cobalt recovery rate dropped to 91.7%.

[0075] Comparative Example 2

[0076] Compared with Example 1, the only difference is that the cobalt extraction in step 7 is performed first, and then the copper extraction in step 5 and the iron removal by the natrona method in step 6 are performed in sequence. The other steps are the same as those in Example 1.

[0077] question:

[0078] Initial pH conflict: Versatic 10 requires weak acidity (pH ≥ 5) to separate cobalt and manganese, but the pH of the leachate is ≈ 0.8, so the pH needs to be significantly adjusted to 5.5 (consuming 12.5 kg of NaOH per ton of ore).

[0079] Fe after pH adjustment 3+ Hydrolysis and precipitation blocked the extraction tank, and the cobalt recovery rate was only 89.4%.

[0080] Comparative Example 3

[0081] Compared with Example 1, the only difference is that in step 2, the reduction mixing is performed by mixing cobalt ore powder and pyrite powder in a mass ratio of 100:25 (i.e., the mass of pyrite is 25% of the mass of cobalt ore powder). The other steps are the same as in Example 1.

[0082] question:

[0083] The amount of pyrite powder added was too high. Excessive pyrite powder induced the iron-sulfur precipitate to encapsulate and co-precipitate cobalt, and produced secondary precipitation of cobalt sulfide, resulting in the cobalt leaching rate being reduced to 79.8%. As a result, the Co leaching rate was reduced to 79.8%, the manganese leaching rate was reduced to 69.2%, the iron leaching rate was 99.3%, and the leachate Fe 3+ The concentration reaches 12.7 g / L and contains divalent iron ions, which is not conducive to the subsequent iron removal process.

[0084] Comparative Example 4

[0085] Compared with Example 1, the only difference is that in step 2, the reduction mixing is performed by mixing cobalt ore powder and pyrite powder in a mass ratio of 100:3 (i.e., the mass of pyrite is 3% of the mass of cobalt ore powder). The other steps are the same as in Example 1.

[0086] question:

[0087] Due to insufficient reducing agent, high-valent manganese and cobalt were not fully reduced, and the Co leaching rate dropped to 83.2%, which was lower than 96.2% in Example 1.

[0088] Comparative Example 5

[0089] Compared with Example 1, the only difference is that the cobalt extraction in step 7 (three-stage countercurrent extraction) is:

[0090] Organic phase: 10% Versatic 10 + 90% sulfonated kerosene.

[0091] The pH was adjusted to 2.5 using 1 mol / L sodium hydroxide solution, the extraction phase ratio O / A was 1:1, and the contact time was 10 min / stage.

[0092] Stripping: 1.0 mol / LH2SO4, O / A=1:2, 1st stage stripping.

[0093] question:

[0094] Effect: Co recovery rate is 72.4%, and the cobalt-manganese separation coefficient β (Co / Mn) is only 8.5. 2+ The purity was 89.7%, and the cobalt content was 0.83 g / L. Without saponification of Versatic 10, the cobalt recovery rate at pH 2.5 was only 72.4% (separation coefficient β = 8.5). This demonstrates that controlling the pH around 5.5 is key to achieving cobalt-manganese separation without saponification of Versatic 10.

Claims

1. A method for recovering valuable metals by enhanced leaching of pyrite and high-manganese, low-cobalt cobaltite, characterized by: The following steps are involved: (1) mixing high-manganese, low-cobalt cobalt earth ore powder with pyrite powder and leaching with sulfuric acid solution to obtain a leachate containing cobalt, manganese, copper and iron; (2) The leachate containing cobalt, manganese, copper and iron is subjected to extraction and back extraction using the Lix984 extraction system to recover copper, thereby obtaining a raffinate containing cobalt, manganese and iron; (3) removing iron from the raffinate containing cobalt, manganese and iron by a sodium ferroalloy method to obtain an iron-removing liquid containing cobalt and manganese; (4) The iron removal liquid containing cobalt and manganese is subjected to extraction and back extraction using the Versatic 10 extraction system to recover cobalt and obtain a manganese-containing raffinate.

2. The method for recovering valuable metals by enhanced leaching of pyrite and high-manganese, low-cobalt cobalt ore according to claim 1, wherein: The mass ratio of the high-manganese, low-cobalt cobalt earth ore powder to the pyrite powder is 100:5~20.

3. A method for recovering valuable metals by enhanced leaching of pyrite and high-manganese, low-cobalt cobalt ore according to claim 1 or 2, characterized in that: The high-manganese, low-cobalt cobalt ore is an oxidized mineral with a cobalt grade of 0.3% to 0.5% and a manganese grade of 10% to 15%.

4. A method for recovering valuable metals by enhanced leaching of pyrite and high-manganese, low-cobalt cobalt ore according to claim 1 or 2, characterized in that: The leaching conditions are as follows: the concentration of the sulfuric acid solution is 20-50 g / L, the leaching liquid-solid ratio is 2-4 L:1 kg, the stirring rate is 200-300 r / min, the leaching temperature is 50-90° C., and the leaching time is 3-5 hours.

5. The method for recovering valuable metals by enhanced leaching of pyrite and high-manganese, low-cobalt cobalt ore according to claim 1, wherein: In step (2), the extraction is 2 to 4 stages of countercurrent extraction, the extraction phase ratio O / A = 1:2 to 2:1, the mass concentration of the Lix984 extractant in the organic phase is 5 to 20%, the extraction contact time of each stage is 5 to 10 minutes, and the extraction pH is controlled in the range of 1 to 2; the number of back extraction stages is 1 to 2 stages, the back extraction liquid is a 1.0 to 2.0 mol / L sulfuric acid solution, and the back extraction phase ratio O / A = 1:1 to 3:

1.

6. The method for recovering valuable metals by enhanced leaching of pyrite and high-manganese, low-cobalt cobalt ore according to claim 1, characterized in that: The process of removing iron by the natanthalite method is as follows: adding natanthalite seed crystals to the raffinate containing cobalt, manganese and iron, adjusting the pH to 2.0-2.5, and reacting at 50-90° C. for 0.5-2 hours.

7. The method for recovering valuable metals by enhanced leaching of pyrite and high-manganese, low-cobalt cobalt ore according to claim 6, characterized in that: The amount of the natanthracite seed crystals added to the raffinate containing cobalt, manganese and iron is 0.5 wt.% to 1.0 wt.%.

8. The method for recovering valuable metals by enhanced leaching of pyrite and high-manganese, low-cobalt cobalt ore according to claim 1, characterized in that: In step (4), the extraction is a 2-4 stage countercurrent extraction, the extraction phase ratio O / A is 1:2-2:1, the mass concentration of the Versatic10 extractant in the organic phase is 5-20%, the contact time of each stage of extraction is 5-10 min, and the extraction pH is controlled in the range of 5-6; The stripping stage is 1~2, the stripping solution is 0.5~1.5mol / L sulfuric acid solution, and the stripping phase ratio O / A=1:1~1:3.

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