Short-process nickel-cobalt-manganese co-extraction process for hydrometallurgy of lateritic nickel ore

Abstract

The invention belongs to the technical field of hydrometallurgy. Provided is a short-process nickel-cobalt-manganese co-extraction process for hydrometallurgy of lateritic nickel ore. The process comprises the following steps: subjecting an iron- and aluminum-removed leachate of lateritic nickel ore to co-extraction by means of an organic acid extraction system, so as to obtain an enriched nickel-cobalt-manganese solution; and subjecting the enriched nickel-cobalt-manganese solution to impurity extraction by means of a P204 extraction system, so as to obtain a high-purity nickel-cobalt-manganese solution. By means of the co-extraction process, a current hydrometallurgical process for extracting nickel, cobalt and manganese from lateritic nickel ore is simplified, the amounts of an acid, an alkali and an extracting agent, the energy consumption and the amount of water used in the extraction process are greatly reduced, the extraction cost of nickel, cobalt and manganese is reduced, and the process is of great significance to the industrial production of ternary nickel-cobalt-manganese raw materials; moreover, the process can achieve the co-extraction of nickel, cobalt and manganese, the purity of nickel, cobalt and manganese is high, and the loss of nickel and cobalt is low; and the content and proportions of nickel, cobalt and manganese metals in the obtained high-purity nickel-cobalt-manganese solution are adjusted according to the ratio these metals in a ternary precursor product, and finally the high-purity nickel-cobalt-manganese solution is used for preparing a nickel-cobalt-manganese ternary positive electrode material.

Description

A short-process nickel-cobalt-manganese co-extraction process for laterite nickel ore hydrometallurgy Technical Field

[0001] The present invention relates to the technical field of hydrometallurgy, and in particular to a short-process nickel-cobalt-manganese co-extraction process for laterite nickel ore hydrometallurgy. Background Art

[0002] The rapid growth of the global new energy vehicle industry has driven the development of ternary NCM lithium batteries. However, the nickel and cobalt resources used in ternary NCM cathode materials for lithium batteries are very limited. With the increasing depletion of nickel sulfide resources, laterite nickel ore has become an increasingly important development direction for nickel and cobalt resource mining. my country has long relied primarily on imported laterite nickel ore, which significantly increases the cost of extracting nickel and cobalt raw materials. Among laterite nickel ores, limonite-type laterite nickel ore has a low grade (less than 1.3%) and contains significant impurities such as iron, aluminum, chromium, zinc, scandium, calcium, copper, manganese, and magnesium. However, the concentration of metallic impurities such as Fe, Cr, Cu, and Zn in the cathode materials of ternary lithium batteries must be controlled to a level of 1 ppb, which places high demands on the purity of the nickel, cobalt, and manganese raw materials. The ability to cost-effectively and efficiently produce battery-grade nickel, cobalt, and manganese sulfate raw materials has become a decisive factor in the further marketization of ternary power batteries.

[0003] Compared to precipitation and resin methods, solvent extraction is more suitable for extracting target metals from solutions rich in various impurities. Currently, high-purity battery-grade nickel and cobalt sulfate raw materials are primarily obtained domestically and internationally through high-pressure leaching of laterite nickel ore, followed by two-stage neutralization to remove iron and aluminum, followed by two-stage precipitation of MHP (nickel cobalt hydroxide), followed by acid dissolution, followed by impurity extraction with P204, cobalt extraction with P507, magnesium removal with P507, or deep impurity removal with P507 / C272, followed by preparation of battery-grade nickel and cobalt sulfate. However, this process is lengthy and cumbersome, resulting in high nickel and cobalt losses. Furthermore, the MHP precipitation process consumes large amounts of liquid caustic soda, significantly increasing the cost of nickel and cobalt recovery.

[0004] Based on this, some researchers have suggested using HBL116, HBL110 and a synergistic extraction system to directly extract nickel, cobalt and manganese from the high-pressure acid leaching solution of laterite nickel ore through a one-step extraction process, and then prepare the NCM ternary precursor by further proportioning. However, for this type of non-single-component composite extractant, the extraction rate of copper and zinc (especially copper) is significantly higher than that of nickel and cobalt, and there are a large amount of iron, aluminum and chromium impurities and some zinc in the acid leaching solution itself, among which chromium can easily poison the extractant, which causes the impurity concentration of the final nickel cobalt sulfate product to be higher than the standard value and affects the normal operation of the extraction system. In addition, some researchers are currently trying to use P204 to directly remove iron, chromium and aluminum from the acid leaching solution, and then extract nickel and cobalt through an extraction process. However, the amount of water in these two extraction processes is very large, which greatly reduces the production efficiency and limits the industrial operation of the process.

[0005] Summary of the Invention

[0006] The purpose of the present invention is to overcome the above-mentioned technical deficiencies and propose a short-process nickel-cobalt-manganese co-extraction process for laterite nickel ore hydrometallurgy, so as to solve the technical problems in the prior art of extracting nickel and cobalt from laterite nickel ore, such as complicated procedures, high alkali and water consumption, low purity of the extracted nickel and cobalt, and large nickel and cobalt loss.

[0007] The present invention provides a short-process nickel-cobalt-manganese co-extraction process for laterite nickel ore hydrometallurgy, comprising the following steps:

[0008] Step S1, using an organic acid extraction system to co-extract the iron-aluminum-removed laterite nickel ore leachate to obtain an enriched nickel, cobalt and manganese solution;

[0009] Step S2: extracting the enriched nickel-cobalt-manganese solution with a P204 extraction system to obtain a high-purity nickel-cobalt-manganese solution.

[0010] Compared with the prior art, the present invention has the following beneficial effects:

[0011] The co-extraction process of the present invention simplifies the current hydrometallurgical process for extracting nickel, cobalt and manganese from laterite nickel ore, greatly reduces the large consumption and energy consumption of acid, alkali, extractant and water during the extraction of nickel, cobalt and manganese, and reduces the cost of nickel, cobalt and manganese extraction. It has important practical significance for the industrial production and application of ternary nickel, cobalt and manganese raw materials. At the same time, the process of the present invention can realize the co-extraction of nickel, cobalt and manganese, with high nickel, cobalt and manganese purity and low nickel and cobalt loss. The high-purity nickel, cobalt and manganese sulfate solution finally obtained can be directly used to prepare nickel, cobalt and manganese ternary positive electrode materials. BRIEF DESCRIPTION OF THE DRAWINGS

[0012] FIG1 is a process flow chart of an embodiment of a short-process nickel-cobalt-manganese co-extraction process for laterite nickel ore hydrometallurgy provided by the present invention. DETAILED DESCRIPTION

[0013] In order to make the purpose, technical solutions and advantages of the present invention more clearly understood, the present invention will be further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not intended to limit the present invention.

[0014] The present invention provides a short-process nickel-cobalt-manganese co-extraction process for laterite nickel ore hydrometallurgy, comprising the following steps:

[0015] Step S1, using an organic acid extraction system to co-extract the iron-aluminum-removed laterite nickel ore leachate to obtain an enriched nickel, cobalt and manganese solution;

[0016] Step S2: extracting the enriched nickel-cobalt-manganese solution with a P204 extraction system to obtain a high-purity nickel-cobalt-manganese solution.

[0017] The present invention first extracts nickel, cobalt, manganese and copper, zinc and trace amounts of aluminum, chromium and other impurities in the laterite nickel ore iron-aluminum leachate by an organic acid extraction system, and then removes impurities in the enriched nickel, cobalt and manganese solution using a P204 extraction system to obtain a battery-grade nickel, cobalt and manganese sulfate product. The co-extraction stage achieves the enrichment of nickel, cobalt and manganese and various impurities in the laterite nickel ore iron-aluminum leachate, so that the water volume during the P204 impurity removal is reduced by about 30 times (when the nickel, cobalt and manganese concentration is enriched to 120g / L required for commercialization), which has important practical significance for promoting the industrial production application of nickel, cobalt and manganese ternary raw materials. The process flow is brief, eliminates the precipitation of MHP (nickel cobalt hydroxide) and acid dissolution steps in the current conventional laterite nickel ore hydrometallurgical process, simplifies the extraction section process when extracting nickel and cobalt, not only saves a large amount of reagent consumption, energy consumption and production costs, improves the recovery rate of nickel and cobalt, but also greatly improves the production efficiency of nickel, cobalt and manganese products.

[0018] In this embodiment, the above-mentioned laterite nickel ore iron and aluminum removal leachate is obtained by sequentially subjecting the laterite nickel ore to high-pressure leaching, first-stage neutralization for iron and aluminum removal, and second-stage neutralization for iron and aluminum removal steps.

[0019] In some specific embodiments of the present invention, the above-mentioned laterite nickel ore iron and aluminum removal leachate comprises the following components: Ni 3.2-4 g / L, Co 0.32-0.48 g / L, Mn 2.6-3.5 g / L, Mg 4-5.2 g / L, Ca 0.1-0.3 g / L, Fe 0-0.001 g / L, Al 0.01-0.03 g / L, Cr 0-0.005 g / L, Sc 0.02-0.04 g / L, Zn 0.015-0.04 g / L, and Cu 0.007-0.016 g / L.

[0020] Preferably, the organic acid extraction system comprises: an organic acid extractant, a first diluent and a co-solvent.

[0021] Preferably, in the organic acid extraction system, the organic acid extractant is at least one of DY319 or Versatic10, preferably DY319. The DY319 extractant used in the present invention has a product composition of 2-hexyl undecanoic acid (C 16 H 32 O2), has high selectivity for nickel, cobalt, and manganese, and has low water solubility. It can completely extract nickel and cobalt from laterite nickel ore leachate, and the oil content of the raffinate is very low, reducing the pressure on wastewater treatment. Furthermore, the inventors found in experiments that the oil content gradually decreases as the saponification rate of the organic acid extractant decreases.

[0022] Preferably, in the organic acid extraction system, the first diluent is sulfonated kerosene, and the dilution rate of the organic acid extractant is 10-50%, including but not limited to 10%, 20%, 30%, 40%, 50%, etc.

[0023] Preferably, in the organic acid extraction system, the cosolvent is at least one of TBP and tridecanol. The addition of the cosolvent in the present invention can increase the solubility of the organic acid extractant in the first diluent, thereby promoting phase separation efficiency during the extraction reaction. Furthermore, the volume ratio of the cosolvent to the first diluent is 1:(3-7), including but not limited to 1:3, 1:4, 1:5, 1:6, 1:7, etc.

[0024] Preferably, the organic acid extraction system is saponified before extraction. The saponifying agent includes any one of sodium hydroxide, nickel hydroxide (sodium hydroxide + nickel sulfate mother liquor converted to soap) or ammonia water, or a combination of at least two. This patent is illustrated with the liquid alkali (sodium hydroxide) commonly used in the industry. Furthermore, the mass fraction of the sodium hydroxide solution is 5-40%, including but not limited to 10%, 17%, 25%, 32%, 40%, etc.; stirring is required for sodium soap, the sodium soap rate is 30-70%, including but not limited to 30%, 40%, 50%, 60%, 70%, etc., and the saponification level is 1-2.

[0025] Preferably, the P204 extraction system comprises: P204 and a second diluent.

[0026] Preferably, in the P204 extraction system, the second diluent is sulfonated kerosene, and the dilution rate of P204 is 10-50%, including but not limited to 10%, 20%, 30%, 40%, 50%, etc.

[0027] Preferably, the P204 extraction system is saponified before extraction. Furthermore, the saponifying agent includes any one or two of sodium hydroxide, nickel hydroxide (sodium hydroxide + nickel sulfate mother liquor to soap) or ammonia water. Furthermore, sodium soap is performed using sodium hydroxide solution, and the mass fraction of the sodium hydroxide solution is 5-40%, including but not limited to 10%, 17%, 25%, 32%, 40%, etc.; stirring is required for sodium soap, and the sodium soap rate is controlled to be 30-70%, including but not limited to 30%, 40%, 50%, 60%, 70%, etc., and the saponification level is 1-2, etc.

[0028] In this embodiment, the above step S1 specifically includes:

[0029] Step S11, using an organic acid extraction system to co-extract the laterite nickel ore iron- and aluminum-removed leachate to obtain an organic phase loaded with nickel, cobalt, and manganese;

[0030] Step S12, washing the nickel-cobalt-manganese loaded organic phase with a first washing liquid to remove calcium, magnesium and some impurities such as iron, aluminum, chromium, and scandium from the nickel-cobalt-manganese loaded organic phase, thereby obtaining an organic phase loaded with nickel-cobalt-manganese and impurities such as copper, zinc, and aluminum;

[0031] Step S13, using the first stripping solution to strip the organic phase loaded with nickel, cobalt, manganese and impurities such as copper, zinc, and aluminum, so that the nickel, cobalt, manganese and impurities in the organic phase loaded with nickel, cobalt, manganese and impurities such as copper, zinc, and aluminum are stripped to obtain an enriched nickel, cobalt, and manganese solution.

[0032] Preferably, in step S11, the ratio (O / A) is 1:(0.5-5), including but not limited to 1:0.5, 1:1, 1:2, 1:3, 1:4, 1:5, etc.; the extraction temperature is 20-60°C, including but not limited to 20°C, 30°C, 40°C, 50°C, 60°C, etc.; the extraction time is 2-15min, including but not limited to 2min, 4min, 6min, 8min, 10min, 12min, 15min, etc.; the extraction stage is 2-10, for example, it can be 2, 3, 4, 5, 6, 7, 8, 9, 10, etc.

[0033] Preferably, in step S12, the first washing liquid is a sulfuric acid solution with a concentration of 0.1-0.5 mol / L, including but not limited to 0.1 mol / L, 0.2 mol / L, 0.3 mol / L, 0.4 mol / L, 0.5 mol / L, etc.; the phase ratio (O / A) is (3-12):1, including but not limited to 3:1, 4:1, 5:1, 6:1, 7:1, 8:1, 9:1, 10:1, 11:1, 12:1, etc.; the washing temperature is 20-60°C, including but not limited to 20°C, 30°C, 40°C, 50°C, 60°C, etc.; the washing time is 5-30 min, including but not limited to 5 min, 10 min, 15 min, 20 min, 25 min, 30 min, etc.; the washing level is 2-9, for example, it can be level 2, level 3, level 4, level 5, level 6, level 7, level 8, level 9, etc.

[0034] Preferably, in step S12, the first washing liquid is added to the iron- and aluminum-removed laterite nickel ore leachate in the co-extraction section of the organic acid extraction system to achieve extraction and recovery of nickel, cobalt, and manganese in the first washing liquid.

[0035] Preferably, in step S13, the first stripping liquid is a sulfuric acid solution with a concentration of 1-3 mol / L, including but not limited to 1 mol / L, 2 mol / L, 3 mol / L, etc.; the phase ratio (O / A) is (1-35):1, including but not limited to 1:1, 5:1, 10:1, 15:1, 20:1, 25:1, 30:1, 35:1, etc.; the stripping temperature is 20-60°C, including but not limited to 20°C, 30°C, 40°C, 50°C, 60°C, etc.; the stripping time is 3-30 min, including but not limited to 3 min, 5 min, 10 min, 15 min, 20 min, 25 min, 30 min, etc.; the stripping stage is 3-8, for example, it can be 3, 4, 5, 6, 7, 8, etc.

[0036] In this embodiment, the above step S2 specifically includes:

[0037] Step S21: extract the enriched nickel-cobalt-manganese solution with a P204 extraction system to remove copper, zinc, chromium, calcium, iron, aluminum and part of manganese impurities to obtain a high-purity nickel-cobalt-manganese solution.

[0038] Preferably, in step S21, the ratio (O / A) is 1:(0.2-2), including but not limited to 1:0.2, 1:0.5, 1:1.5, 1:2, etc.; the extraction temperature is 20-60°C, including but not limited to 20°C, 30°C, 40°C, 50°C, 60°C, etc.; the extraction time is 2-15min, including but not limited to 2min, 4min, 6min, 8min, 10min, 15min, etc.; the extraction level is 2-13, for example, it can be level 2, level 3, level 4, level 5, level 6, level 7, level 8, level 9, level 10, level 11, level 12, level 13, etc.

[0039] In some preferred embodiments of the present invention, the above step S2 further includes:

[0040] Step S22: Wash the loaded organic phase with a second washing liquid to remove impurities such as Fe and Cr in the loaded organic phase, thereby realizing the recycling of the P204 extractant.

[0041] Preferably, in step S22, the second washing liquid is a hydrochloric acid solution with a concentration of 0.5-2 mol / L, including but not limited to 0.5 mol / L, 1 mol / L, 1.5 mol / L, 2 mol / L, etc.; the phase (O / A) is (3-13):1, including but not limited to 3:1, 4:1, 5:1, 6:1, 7:1, 8:1, 9:1, 10:1, 11:1, 12:1, 13:1, etc.; the washing temperature is 20-60°C, including but not limited to 20°C, 30°C, 40°C, 50°C, 60°C, etc.; the washing time is 5-30 min, including but not limited to 5 min, 10 min, 15 min, 20 min, 25 min, 30 min, etc., and the number of washing stages is 3-8, for example, it can be stage 3, stage 4, stage 5, stage 6, stage 7, stage 8, etc.

[0042] To avoid redundancy, the composition of the second-stage iron and aluminum removal leaching solution of laterite nickel ore in the following embodiments of the present invention is shown in Table 1.

[0043] Table 1

[0044] Example 1

[0045] (1) Preparation of DY319 extraction organic phase: DY319, tridecanol and sulfonated kerosene were mixed and stirred in a volume ratio of 4:1:5, that is, the dilution rate of DY319 was 40%, and then sodium soap was performed using a 32% mass fraction sodium hydroxide solution, the sodium soap rate was 60%, and the saponification level was 1.

[0046] (2) DY319 co-extraction of nickel, cobalt and manganese:

[0047] ① The leaching solution from the second-stage iron and aluminum removal of laterite nickel ore requires no further treatment. The saponified organic phase from the DY319 extraction was mixed with the leaching solution from the second-stage iron and aluminum removal of laterite nickel ore in a volume ratio of 1:3. The extraction temperature was 45°C, the extraction time was 8 minutes, and the number of extraction stages was four. The composition and oil content of the raffinate are shown in Table 2 below. The oil content is based on data from a one-month continuous operation of the extraction tank. The industrial requirement for oil content is <100 mg / L. This low oil content significantly reduces wastewater treatment pressure.

[0048] Table 2 Raffinate composition and oil content

[0049] ② The nickel, cobalt, and manganese-loaded DY319 organic phase was washed with 0.4 mol / L sulfuric acid solution. The volume ratio of the organic phase to the sulfuric acid solution was 3:1, the washing temperature was 45°C, the washing time was 20 minutes, and the number of washing stages was 5. Simultaneously, the washing liquid was incorporated into the second-stage iron and aluminum removal leachate of the laterite nickel ore in the extraction section. The composition of the raffinate described above is the test result after the washing liquid was incorporated into the extraction section.

[0050] ③ The nickel, cobalt, and manganese in the organic phase were stripped with 2.25 mol / L sulfuric acid solution. The volume ratio of the organic phase to the sulfuric acid solution was controlled at 8:1, the stripping temperature was 45°C, the stripping time was 14 minutes, and the stripping stage was 6. The composition of the enriched nickel, cobalt, and manganese sulfate solution obtained by stripping is shown in Table 3 below.

[0051] Table 3 Composition of enriched nickel cobalt manganese sulfate solution

[0052] (3) Preparation of P204 extraction organic phase: P204 and sulfonated kerosene were mixed and stirred in a volume ratio of 1:3, that is, the dilution rate of P204 was 25%, and then sodium soap was performed using 32% sodium hydroxide solution, the sodium soap rate was 60%, and the saponification level was 1.

[0053] (4) P204 impurities:

[0054] ① The saponified P204 extracted organic phase was mixed with the enriched nickel cobalt manganese sulfate solution in a volume ratio of 1:1. The extraction temperature was 45°C, the extraction time was 8 min, and the extraction stage was 3. Fe, Al, Ca, Cu, Sc, Zn, Cr and part of Mn in the nickel cobalt manganese sulfate solution were extracted and removed. The composition of the nickel cobalt manganese sulfate solution product after impurity removal is shown in Table 4 below.

[0055] ② Use 1.5 mol / L hydrochloric acid to wash all impurities such as Cu, Zn, Al, etc. in the loaded organic phase, control the volume ratio of the organic phase to the hydrochloric acid solution to 11:1, the washing temperature to 45 ° C, the washing time to 20 min, the washing stage to 6, and the washed extractant to be saponified and recycled into the tank.

[0056] Table 4 Composition of nickel cobalt manganese sulfate solution after impurity removal

[0057] Example 2

[0058] In the ternary nickel-cobalt-manganese positive electrode material, the higher the ratio of nickel and cobalt, the greater the energy and power density of the ternary battery. Ternary lithium batteries have developed from the 5 series and 6 series to the current 9 series. Therefore, in order to reduce the proportion of manganese in the nickel-cobalt-manganese sulfate solution, a nickel-cobalt-manganese sulfate solution with a nickel-cobalt-manganese ratio close to 9:1:1 is prepared. On the basis of Example 1, the volume ratio of the saponified P204 extracted organic phase to the enriched nickel-cobalt-manganese sulfate solution can be adjusted to 1.4:1. Other parameters remain unchanged. The composition of the obtained nickel-cobalt-manganese sulfate solution product is shown in Table 5 below.

[0059] Table 5 Composition of enriched nickel cobalt manganese sulfate solution

[0060] Example 3

[0061] To reduce the manganese content in the nickel-cobalt-manganese sulfate solution, the DY319 co-extraction process can be adjusted based on Example 1. The DY319 dilution rate in the co-extraction stage was reduced to 34%. Since the reduction in dilution rate was minimal, the saponification rate of DY319, the volume ratio of the organic phase extracted with DY319 to the second-stage iron- and aluminum-removed leachate from laterite nickel ore, and the number of extraction stages remained unchanged to ensure that DY319 completely extracted the nickel and cobalt from the second-stage leachate. The composition and oil content of the raffinate (second-stage leachate) after DY319 extraction are shown in Table 6 below.

[0062] Table 6 Raffinate composition and oil content

[0063] The composition of the raffinate indicates that the Mn content in the loaded organic phase has decreased, as have the concentrations of Ca and Mg impurities. To prevent excessive Mn removal in the wash stage, the ratio of organic phase to acid in the wash stage was adjusted to 4:1. Other parameters remained unchanged, resulting in the composition of the enriched nickel-cobalt-manganese sulfate solution shown in Table 7. Due to the relatively low loss of nickel and cobalt during the impurity removal stage, the nickel and cobalt concentrations in the enriched sulfuric acid solution increased.

[0064] Table 7 Composition of enriched nickel cobalt manganese sulfate solution

[0065] In the subsequent P204 impurity removal stage, in order to reduce the loss of nickel, cobalt and manganese during extraction, the volume ratio of the organic phase loaded with nickel manganese sulfate to the saponified extractant was reduced to 0.7:1. Other conditions remained unchanged. The composition of the obtained nickel cobalt manganese sulfate solution after impurity removal is shown in Table 8 below.

[0066] Table 8 Composition of nickel cobalt manganese sulfate solution after impurity removal

[0067] In summary, the co-extraction process of the present invention can effectively regulate the manganese content in a battery-grade ternary nickel-cobalt-manganese sulfate solution by jointly controlling the process conditions of the organic acid co-extraction stage and the P204 extraction stage. Specifically, in the co-extraction stage, by reducing the DY319 dilution rate, saponification rate, volume ratio of the organic phase extracted with saponified DY319 to the second-stage leachate, or any combination of at least two, the manganese extraction rate of DY319 under the same conditions can be reduced, thereby reducing the manganese content in the enriched nickel-cobalt-manganese solution. If the Mn extraction rate decreases, the number of extraction stages can be appropriately reduced, and the concentration of impurities such as Zn, Al, Ca, Cr, and Fe in the DY319 organic phase loaded with nickel, cobalt, and manganese can be reduced. In this case, the sulfuric acid concentration in the wash stage, the volume ratio relative to the organic phase, the number of wash stages, or any combination of at least two of these can be appropriately reduced. In the subsequent P204 impurity removal stage, increasing the dilution rate of P204, the saponification rate, and the volume ratio of the saponified P204 extracted organic phase to the enriched nickel, cobalt and manganese sulfate can increase the extraction rate of manganese by P204, and also achieve the purpose of reducing the manganese proportion in the final nickel, cobalt and manganese solution.

[0068] The specific embodiments of the present invention described above do not limit the scope of protection of the present invention. Any other corresponding changes and modifications made based on the technical concept of the present invention should be included in the scope of protection of the claims of the present invention.

Claims

1. A short-process nickel-cobalt-manganese co-extraction process for laterite nickel ore hydrometallurgy, characterized in that: The following steps are involved: Step S1, using an organic acid extraction system to co-extract the iron-aluminum-removed laterite nickel ore leachate to obtain an enriched nickel-cobalt-manganese solution; Step S2: extracting the enriched nickel-cobalt-manganese solution with a P204 extraction system to obtain a high-purity nickel-cobalt-manganese solution.

2. According to claim 1, the short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy is characterized in that: The laterite nickel ore iron and aluminum removal leaching solution is obtained by sequentially subjecting the laterite nickel ore to high pressure leaching, first stage neutralization iron and aluminum removal, and second stage neutralization iron and aluminum removal steps.

3. The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 1, characterized in that: The laterite nickel ore iron and aluminum removal leaching solution comprises the following components: Ni 3.2-4 g / L, Co 0.32-0.48 g / L, Mn 2.6-3.5 g / L, Mg 4-5.2 g / L, Ca 0.1-0.3 g / L, Fe 0-0.001 g / L, Al 0.01-0.03 g / L, Cr 0-0.004 g / L, Sc 0.012-0.035 g / L, Zn 0.015-0.035 g / L, and Cu 0.007-0.016 g / L.

4. The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 1, characterized in that: The organic acid extraction system comprises: an organic acid extractant, a first diluent and a co-solvent.

5. The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 4, characterized in that: In the organic acid extraction system, the organic acid extractant is at least one of DY319 and Versatic10, the first diluent is sulfonated kerosene, and the co-solvent is at least one of TBP and tridecanol; the dilution rate of the organic acid extractant is 10-50%, and the volume ratio of the co-solvent to the first diluent is 1:(3-7).

6. The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 1, characterized in that: The P204 extraction system includes: P204 and a second diluent.

7. The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 6, characterized in that: In the P204 extraction system, the second diluent is sulfonated kerosene, and the dilution rate of P204 is 10-50%.

8. The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 1, characterized in that: The organic acid extraction system or the P204 extraction system is subjected to saponification treatment before extraction; the saponifying agent is any one of sodium hydroxide, nickel hydroxide or ammonia water or a combination of at least two thereof.

9. The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 8, characterized in that: The saponifying agent is a sodium hydroxide solution, and the mass fraction of the sodium hydroxide solution is 5-40%, the sodium soap rate is 30-70%, and the saponification level is 1-2.

10. The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 1, characterized in that: The step S1 specifically includes: Step S11, using an organic acid extraction system to co-extract the laterite nickel ore iron-aluminum-removed leaching solution to obtain a first organic phase loaded with nickel, cobalt and manganese; Step S12, washing the first organic phase loaded with nickel, cobalt and manganese with a first washing liquid to obtain a second organic phase loaded with nickel, cobalt and manganese; Step S13, using the first stripping solution to strip the second nickel-cobalt-manganese loaded organic phase to obtain an enriched nickel-cobalt-manganese solution.

11. The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 10, characterized in that: In the step S11, the ratio of O:A is 1:(0.5-5), the extraction temperature is 20-60°C, the extraction time is 2-15min, and the extraction level is 2-10.

12. The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 10, characterized in that: In the step S12, the first washing liquid is a sulfuric acid solution with a concentration of 0.1-0.5 mol / L, the ratio of O:A is (3-12):1, the washing temperature is 20-60°C, the washing time is 5-30 min, and the washing level is 2-9.

13. The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 10, characterized in that: In the step S12, the first washing liquid is added to the iron-aluminum-removed laterite nickel ore leaching liquid in the co-extraction section of the organic acid extraction system to achieve extraction and recovery of nickel, cobalt and manganese in the first washing liquid.

14. The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 10, characterized in that: In step S13, the first stripping solution is a sulfuric acid solution with a concentration of 1-3 mol / L, the ratio of O:A is (1-35):1, the stripping temperature is 20-60°C, the stripping time is 3-30 min, and the stripping stage is 3-8.

15. [Corrected 27.08.2024 in accordance with Rule 91] The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 1, characterized in that: In the step S2, the ratio of O:A is 1:(0.2-2), the extraction temperature is 20-60°C, the extraction time is 2-15min, and the extraction level is 2-13.

16. The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 1, characterized in that: The step S2 further comprises: The loaded organic phase is washed with a second washing liquid.

17. The short-process nickel-cobalt-manganese co-extraction process of laterite nickel ore hydrometallurgy according to claim 16, characterized in that: In step S2, the second washing liquid is a hydrochloric acid solution with a concentration of 0.5-2 mol / L, the ratio of O:A is (3-13):1, the washing temperature is 20-60°C, the washing time is 5-30 min, and the washing level is 3-8.

Images