A method for recovering valuable metals based on double mineral enhanced leaching of pyrite and high-manganese low-cobalt cobalt ore

Abstract

The application discloses a method for recovering valuable metals based on pyrite and high-manganese low-cobalt cobalt ore double mineral enhanced leaching, and belongs to the technical field of mineral processing and metallurgy. The method is characterized in that: high-manganese low-cobalt cobalt ore powder is mixed with pyrite powder, and then leached by a sulfuric acid solution; the leaching solution is first subjected to copper recovery through extraction and reverse extraction by using a Lix984 extraction system, iron removal by using a jarosite method, and finally subjected to cobalt recovery through extraction and reverse extraction by using a Versatic 10 extraction system, so as to obtain a manganese-containing raffinate. The method strengthens the leaching of valuable metals in high-manganese low-cobalt cobalt ore by using pyrite, and simultaneously adopts a combined process of copper separation by using a Lix984 extraction method, iron removal by using a jarosite method and cobalt separation by using a Versatic 10 extraction method, so that efficient separation of copper, cobalt, manganese and other valuable metals is realized in sequence. The method has a short process flow, low reagent consumption cost, and realizes the resource utilization of high-manganese low-cobalt cobalt ore.

Description

TECHNICAL FIELD

[0001] The present application relates to a pyrite and cobalt ore smelting method, in particular to a method for recovering valuable metals based on pyrite and high-manganese low-cobalt cobalt ore double ore intensified leaching, belonging to the technical field of mineral processing and metallurgy. BACKGROUND

[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 the sulfur dioxide reduction method can partially reduce high-valence metals (such as Co 3+ , Mn 4+ ), but its strong corrosion leads to a 30%~50% reduction in equipment life, and the SO2 emission limit in the tail gas is strict (usually <50ppm), with high processing cost; the coke high-temperature reduction method needs to operate above 800℃, with energy consumption of 200~300kWh per ton of ore, carbon emissions increasing by more than 40%, and ash impurities (such as silicon and aluminum) mixed into the slag, reducing the purity of the leaching solution and increasing the difficulty of subsequent separation.

[0003] The direct acid leaching process has very low extraction efficiency for valuable metals in cobalt ore that has not been pretreated, because high-valence oxides (MnO2, Co3O4) are difficult to dissolve in dilute acid, and the leaching rate of cobalt and manganese is generally less than 20%, and the leaching rate of copper is less than 15%. Existing reduction leaching can effectively improve the leaching rate of metals such as cobalt and manganese, for example, Chinese patent application (publication number: CN1401799A) discloses using pyrite as a reducing agent to leach valuable elements Co, Ni, Mn, Cu in cobalt ore, with leaching rates of Co 92~95%, Mn 95~96%, and Ni 55~60%, which effectively improves the leaching rate of valuable metals, but does not achieve separation and recovery of metal ions. Chinese patent application (publication number: CN102021331A) discloses that high-manganese cobalt ore is treated by reduction leaching, preliminary purification, manganese-cobalt separation, and extraction separation to obtain manganese carbonate, copper sulfate, nickel carbonate, and cobalt chloride or cobalt sulfate products, but the process flow is very complex, the efficiency is low, the reagent cost is high, and it is not conducive to industrial production. SUMMARY

[0004] In view of the technical problems existing in the cobalt ore processing process in the prior art, the purpose of the present application is to provide a method for recovering valuable metals based on the synergistic leaching of pyrite and high-manganese low-cobalt cobalt ore, which can enhance the leaching of cobalt, manganese, copper and other valuable metals in cobalt ore under mild conditions based on the synergistic leaching of pyrite and high-manganese low-cobalt cobalt ore, and on this basis, a combined process of Lix984 extraction, sodium jarosite method for removing iron and Versatic 10 extraction for separating cobalt is adopted to realize the efficient separation and recovery of copper, cobalt, manganese and other valuable metals in turn, and the interference of impurity metal ions can be effectively avoided. The method has a short process flow, low reagent consumption cost, realizes the resource utilization of high-manganese low-cobalt cobalt ore, and has the advantages of short process flow and low reagent consumption cost.

[0005] In order to achieve the above technical purpose, the present application provides a method for recovering valuable metals based on the synergistic leaching of pyrite and high-manganese low-cobalt cobalt ore, which comprises the following steps:

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

[0007] (2) recovering copper from the leaching solution containing cobalt, manganese, copper and iron by using Lix984 extraction system through extraction and stripping to obtain a raffinate containing cobalt, manganese and iron;

[0008] (3) removing iron from the raffinate containing cobalt, manganese and iron by using sodium jarosite method to obtain an iron-removed solution containing cobalt and manganese;

[0009] (4) recovering cobalt from the iron-removed solution containing cobalt and manganese by using Versatic 10 extraction system through extraction and stripping to obtain a raffinate containing manganese.

[0010] The present application is based on the characteristics of low cobalt grade of high-manganese low-cobalt cobalt ore and the difficulty of dissolving high-valence oxides (Co3O4, MnO2) contained therein in dilute acid, which is the main reason for the low leaching rate of cobalt and manganese therein. The present application uses a synergistic leaching method of pyrite and high-manganese low-cobalt cobalt ore, which can promote the efficient reduction leaching of high-valence cobalt and manganese (Co3O4, MnO2) in high-manganese low-cobalt cobalt ore under relatively mild conditions by using pyrite as a reducing agent. The obtained leaching solution mainly contains valuable metal ions such as Co 2+ , Mn 2 + , Cu 2+ and Fe 3+ . The efficient separation of valuable metal ions such as Co 2+ , Mn 2+ , Cu 2+ and Fe 3+ by using a short process and low cost method is one of the important innovations of the present application, and the efficient separation of valuable metal ions such as Co 2+Compared to other metal ions, it affects the removal of Fe by the sodium ferrous sulfate process. 3+ The main metal ions, in this invention, are extracted and separated using the Lix984 extraction system. 2+ The Lix984 extraction system can achieve Cu extraction. 2+ Highly efficient recycling while reducing CO 2+ Mn 2+ The loss, based on this, the reduction leaching process uses a sulfuric acid leaching system, and almost all the iron in the leachate is in the form of Fe. 3+ It exists in the form of sodium ferric sulfate for the removal of Fe. 3+ Provides favorable conditions, while the sodium ferrous sulfate process for Fe 3+ Thorough and selective removal, avoiding Co 2+ Mn 2+ The losses ultimately affected Co. 2+ With Mn 2+ For the separation of Co, this invention employs the Versatic 10 extraction system, which is effective for the extraction of Co. 2+ The extraction selectivity is good, Co 2+ With Mn 2+ High separation coefficient, capable of achieving Co 2+ With Mn 2+ Highly efficient separation and recovery. In summary, this invention employs a combined process of Lix984 extraction for copper separation, sodium ferrous sulfate for iron removal, and Versatic10 extraction for cobalt separation, enabling highly 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 ore powder to the pyrite powder is 100:5~20. If the amount of pyrite is too low (<5%), the high-valent cobalt and manganese in the high-manganese, low-cobalt cobalt ore will not be sufficiently reduced and leached. If the amount of pyrite is too high (>20%), excessive iron impurities will be introduced, increasing the burden on subsequent iron removal and increasing sulfuric acid consumption by more than 15%. The mass ratio of the high-manganese, low-cobalt cobalt ore powder to the pyrite powder is further preferably 100:10~15.

[0012] As a preferred embodiment, the high-manganese, low-cobalt cobalt ore is an oxidizing 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 scheme, the leaching conditions are: the concentration of sulfuric acid solution is 20-50 g / L, the solid-liquid ratio of leaching solution is 2-4 L:1 kg, the stirring rate is 200-300 r / min, the leaching temperature is 50-90 DEG C, and the leaching time is 3-5 hours. Under the preferred leaching conditions, the efficient leaching of valuable metals in the high-manganese and low-cobalt cobalt ore powder can be ensured. The concentration of sulfuric acid solution is further preferably 35-45 g / L. The leaching temperature is further preferably 75-85 DEG C. The solid-liquid ratio of leaching solution is further preferably 3-4 L:1 kg. Under the optimized conditions, the cobalt leaching rate is greater than or equal to 95.47%, the manganese leaching rate is greater than or equal to 79.11%, and the copper leaching rate is greater than or equal to 84.32%.

[0014] As a preferred scheme, in step (2), the extraction is 2-4 stage countercurrent extraction, the phase ratio O / A is 1:2-2:1, the mass concentration of Lix984 extractant in the organic phase is 5-20%, the contact time of each extraction stage is 5-10 min, and the extraction pH is controlled in the range of 1-2. The "phase ratio" referred to in the present application 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 1-2, the selective extraction effect of Lix984 extractant on Cu 2+ can be improved, and the loss of Co 2+ and Mn 2+ metal ions is reduced. The pH adjustment generally uses a sodium hydroxide solution with a concentration of 1 mol / L.

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

[0016] Under the preferred conditions, the Lix984 extraction-sulfuric acid stripping process adopted in the present application has a copper recovery rate of greater than or equal to 99.68%.

[0017] As a preferred scheme, the process of removing iron by the jarosite method is: adding jarosite seed crystals to the cobalt-, manganese-, and iron-containing raffinate, adjusting the pH to 2.0-2.5, and reacting at 50-90 DEG C for 0.5-2 hours. The jarosite method has good selectivity for removing Fe 3+ and is thorough in removing Fe 3+ . Under the preferred conditions, the removal rate of iron is greater than or equal to 98%.

[0018] As a more preferred scheme, the addition amount of the jarosite seed crystals in the cobalt-, manganese-, and iron-containing raffinate is 0.5wt.%-1.0wt.%. By introducing an appropriate amount of jarosite seed crystals, the crystallization of Fe 3+ in the form of jarosite can be accelerated.

[0019] As a preferred scheme, in step (4), the extraction is 2-4 stage countercurrent extraction, the extraction phase ratio O / A is 1:2-2:1, the mass concentration of Versatic 10 extractant in the organic phase is 5-20%, the extraction contact time of each stage is 5-10 min, and the extraction pH is controlled in the range of 5-6. The organic phase uses sulfonated kerosene as a diluent. The pH adjustment generally uses a 1 mol / L sodium hydroxide solution. The Versatic 10 extractant does not need to be saponified. Under the preferred extraction conditions, especially when the pH is controlled in the range of 5-6, the selectivity of the Versatic 10 extractant to Co 2+ can be effectively improved, while the extraction of the Versatic 10 extractant to Mn 2+ is inhibited, thereby greatly improving the cobalt-manganese separation coefficient β (Co / Mn). The pH adjustment generally uses a 1 mol / L sodium hydroxide solution.

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

[0021] Under the preferred conditions, the Versatic 10 extraction-sulfuric acid stripping process adopted by the present application has a cobalt recovery rate of ≥99.55% and good cobalt-manganese separation effect.

[0022] The high-manganese low-cobalt cobalt ore powder of the present application is obtained by wet ball milling, screening and drying of high-manganese low-cobalt cobalt ore raw ore. The ball milling is performed to a particle size of about 2 mm, and then the ore slurry is screened using a 200 mesh screen. The undersize is dried to obtain the high-manganese low-cobalt cobalt ore powder.

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

[0024] (1) The technical scheme of the present application uses pyrite to cooperatively reduce and leach high-manganese low-cobalt cobalt ore, which can achieve efficient leaching of high-valence metals (Co3O4, MnO2) in high-manganese low-cobalt cobalt ore under mild conditions, avoids the use of traditional sulfur dioxide reducing agents, completely eliminates the risk of sulfur pollution, saves the roasting process to reduce carbon emissions, and can use dilute acid leaching with an optimized sulfuric acid concentration of 40 g / L (100 g / L is required in the traditional process), thereby reducing acid mist emission and waste liquid treatment pressure.

[0025] (2) The technical scheme of the present application has a high leaching rate of valuable metals in high-manganese and low-cobalt cobalt ore, such as a cobalt leaching rate of ≥95% (a traditional process <80%), a manganese leaching rate of ≥78%, and a copper leaching rate of ≥84%; and the combination process of Lix984 extraction separation of copper, iron removal by jarosite method, and Versatic 10 extraction separation of cobalt has a good metal separation effect, a high recovery rate, a copper recovery rate of up to 99%, a cobalt recovery rate of ≥99%, and an impurity iron removal rate of >98%.

[0026] (3) The technical scheme of the present application cancels the roasting furnace system, reduces equipment investment and direct cost, has a short process flow, and is high in production efficiency, which is beneficial to industrial production. BRIEF DESCRIPTION OF DRAWINGS

[0027] Figure 1 The figure is a process flow diagram of the present application.

[0028] Figure 2 The figure is the thermodynamic calculation data of the reduction process in the leaching process in Example 1, which shows that the high-valence cobalt and manganese in the raw material can be reduced to low-valence form under medium and low temperature conditions after the addition of pyrite, which plays a strengthening role in leaching.

[0029] Figure 3 The figure is an XRD comparison chart of the high-manganese and low-cobalt cobalt ore before and after leaching in Example 1, which shows that the hard manganese mineral phase in the raw ore disappears after the synergistic leaching with pyrite, indicating that the high-valence manganese in the raw ore is reduced to low-valence. DETAILED DESCRIPTION

[0030] The following examples are intended to further illustrate the content of the present application, rather than limit the scope of protection of the claims of the present application.

[0031] In the following specific examples, X-ray diffraction (XRD) and X-ray fluorescence spectroscopy (XRF) are used to analyze the phase composition of the calcined product and the leaching residue, and inductively coupled plasma (ICP) is used to detect the concentration of cobalt, manganese and other elements in the leaching solution.

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

[0033] Example 1

[0034] The main components and mass content of the raw material of a cobalt ore in Yunnan are as follows: Co 0.38%, Mn 10.95%, Cu 0.52%, and Fe 3.12%.

[0035] The main components and mass content of the raw material of pyrite are as follows: Fe 45.2%, S 48.5%, and SiO2 3.1%.

[0036] 1. Raw material pretreatment:

[0037] The raw ore is crushed and wet ball milled to a particle size of ≤74 μm (200 mesh), and dried at 105 ℃ for 12 hours.

[0038] Effect: The specific surface area of the ore powder reaches more than 3200 cm² / g, which is beneficial to subsequent leaching.

[0039] 2. Reduction mixing:

[0040] The cobalt ore powder and the 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: The pyrite acts as a reducing agent, avoiding high-temperature roasting and reducing energy consumption.

[0042] 3. Acid leaching:

[0043] The sulfuric acid concentration is 40 g / L, the liquid-solid ratio is 4:1 L / kg, the constant temperature is 85 ℃, the stirring speed is 250 r / min, and the stirring time is 4 hours.

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

[0045] 4. Solid-liquid separation: The leaching slurry is filtered, the filter residue is washed twice with deionized water (liquid-solid ratio 1:1), and the filtrate is combined.

[0046] Effect: The total metal recovery rate is >99.5%, and the residual cobalt in the slag is <0.02%.

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

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

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

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

[0051] Effect: The Cu recovery rate is 99.65%; the Cu concentration of the stripping solution is 31.2 g / L; and the total loss rate of Co and Mn is <0.3%.

[0052] 6. Iron removal by jarosite method: 0.7% jarosite seed is added to the raffinate, the pH is adjusted to 2.3, and the reaction is carried out at 90 ℃ for 1.5 hours.

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

[0054] 7. Cobalt stripping (3rd stage countercurrent extraction): organic phase: 10% Versatic 10 + 90% sulfonated kerosene.

[0055] pH was adjusted to 5.5 using 1 mol / L NaOH solution, O / A = 1:1, contact time 10 min / stage.

[0056] Stripping: 1.0 mol / L H2SO4, O / A = 1:2, 1 stage stripping.

[0057] Effect: Co recovery 99.55%, cobalt-manganese separation factor β (Co / Mn) 350, Co concentration in stripping solution 28.5 g / L.

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

[0059] Example 2

[0060] The composition of the raw material of a low-grade cobalt laterite in Congo: Co 0.22%, Mn 8.73%, Cu 0.31%, Fe 2.85%.

[0061] The main components and mass content of the raw material of pyrite: Fe 45.2%, S 48.5%, SiO2 3.1%.

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

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

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

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

[0066] 6. Iron removal by jarosite method: 0.9 wt.% jarosite seed was added to the raffinate, pH was adjusted in two stages (2.5 to 2.0), 90°C reaction for 1.5 hours.

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

[0068] Step 7 refers to Example 1.

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

[0070] Comparative Example 1

[0071] The only difference compared with Example 1 is that steps 5 and 6 are replaced, i.e. first perform step 6 of the jarosite process to remove iron, and then perform step 5 of the copper extraction. The other steps refer to Example 1.

[0072] Problem:

[0073] During the jarosite process to remove iron, Cu 2+ co-precipitates with Fe 3+ , and 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) remains in the raffinate, which interferes with cobalt extraction, and the cobalt recovery rate drops to 91.7%.

[0075] Comparative Example 2

[0076] The only difference compared with Example 1 is that first perform step 7 of the cobalt extraction, and then perform step 5 of the copper extraction and step 6 of the jarosite process to remove iron in sequence. The other steps refer to Example 1.

[0077] Problem:

[0078] Initial pH conflict: Versatic 10 requires weak acidity (pH ≥ 5) to separate cobalt from manganese, but the leaching solution has a pH of about 0.8, which needs to be adjusted to 5.5 (consumes NaOH 12.5 kg / ton of ore).

[0079] After adjusting the pH, Fe 3+ hydrolyzes and precipitates, clogging the extraction tank, and the cobalt recovery rate is only 89.4%.

[0080] Comparative Example 3

[0081] The only difference compared with Example 1 is that in step 2, the reduction mixture is mixed with a mass ratio of 100:25 of cobalt ore powder and pyrite powder (i.e. the mass of pyrite is 25% of the mass of cobalt ore powder). The other steps refer to Example 1.

[0082] Problem:

[0083] The addition amount of pyrite powder is too high, and the excess pyrite powder induces the encapsulation and co-precipitation of cobalt by iron and sulfur precipitates, as well as the secondary precipitation of cobalt sulfide, resulting in a decrease in cobalt leaching rate to 79.8%. The Co leaching rate is reduced to 79.8%, the Mn leaching rate is reduced to 69.2%, the Fe leaching rate is 99.3%, and the Fe 3+ concentration in the leaching solution 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] The only difference compared with Example 1 is that the reduction mixture in Step 2: cobalt ore powder and pyrite powder are mixed in a mass ratio of 100:3 (i.e. the mass of pyrite is 3% of the mass of cobalt ore powder). Other steps refer to Example 1.

[0086] Problem:

[0087] Due to insufficient reducing agent, high-valence manganese and cobalt are not fully reduced, and the Co leaching rate is reduced to 83.2%, lower than 96.2% in Example 1.

[0088] Comparative Example 5

[0089] The only difference compared with Example 1 is that the cobalt extraction in Step 7 (three-stage countercurrent extraction):

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

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

[0092] Stripping: 1.0 mol / L H2SO4, O / A = 1:2, 1-stage stripping.

[0093] Problem:

[0094] Effect: The Co recovery rate is 72.4%, and the cobalt-manganese separation coefficient β (Co / Mn) is only 8.5. The purity of the manganese raffinate Mn 2+ is 89.7%, and the cobalt content is 0.83 g / L. Under the condition that Versatic 10 is not saponified, the cobalt recovery rate is only 72.4% (separation coefficient β = 8.5) at pH = 2.5, proving that Versatic 10 is the key to realizing cobalt-manganese separation by controlling the pH at around 5.5 without saponification.

Claims

1. A method for recovering valuable metals by enhanced leaching of pyrite and high-manganese, low-cobalt cobaltite, characterized in that: Includes the following steps: (1) Mix high-manganese, low-cobalt cobalt ore powder with pyrite powder and leach with sulfuric acid solution to obtain a leachate containing cobalt, manganese, copper and iron; (2) The leaching solution containing cobalt, manganese, copper and iron was extracted and back-extracted using the Lix984 extraction system to recover copper, and the raffinate containing cobalt, manganese and iron was obtained. (3) The raffinate containing cobalt, manganese and iron was de-ironed by the sodium ferric sulfate method to obtain a de-ironized solution containing cobalt and manganese; (4) The cobalt and manganese-containing iron removal liquid was extracted and back-extracted using the Versatic10 extraction system to recover cobalt and obtain manganese-containing raffinate.

2. The method for recovering valuable metals by enhanced leaching of pyrite and high-manganese, low-cobalt cobaltite according to claim 1, characterized in that: The mass ratio of the high-manganese, low-cobalt cobalt 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 oxidizing 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 sulfuric acid solution is 20~50g / L, the leaching liquid-to-solid ratio is 2~4L:1kg, the stirring rate is 200~300r / min, the leaching temperature is 50~90℃, 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 cobaltite according to claim 1, characterized in that: In step (2), the extraction is a 2-4 stage countercurrent extraction with an extraction ratio of O / A = 1:2-2:1, the mass concentration of Lix984 extractant in the organic phase is 5-20%, the contact time of each extraction stage is 5-10 min, and the extraction pH is controlled within the range of 1-2; the back-extraction stage is 1-2, the back-extraction solution is a 1.0-2.0 mol / L sulfuric acid solution, and the back-extraction ratio is O / A = 1:1-3:

1.

6. The method for recovering valuable metals by enhanced leaching of pyrite and high-manganese, low-cobalt cobaltite according to claim 1, characterized in that: The process of removing iron using the sodium ferrous sulfate method is as follows: sodium ferrous sulfate seed crystals are added to the raffinate containing cobalt, manganese and iron, the pH is adjusted to 2.0~2.5, and the reaction is carried out at 50~90℃ for 0.5~2 hours.

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

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