A method for extracting and separating nickel, cobalt, tungsten, molybdenum and vanadium

Abstract

The application belongs to the technical field of extraction and specifically relates to a method for extracting and separating nickel, cobalt, tungsten, molybdenum and vanadium, which comprises the following steps: extracting and separating a to-be-processed aqueous phase containing nickel, cobalt, tungsten, molybdenum and vanadium ions and an extraction organic phase to obtain a loaded organic phase rich in tungsten, molybdenum and vanadium ions and a raffinate aqueous phase rich in nickel and cobalt ions; and the extraction organic phase is an acidified organic phase containing an extractant of formula 1, an extractant of formula 2, an extractant of formula 3 and a diluent. Based on the process, the common extraction of tungsten, molybdenum and vanadium ions can be realized, and in addition, the high-selectivity extraction and separation of tungsten, molybdenum, vanadium, nickel and cobalt can also be realized.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of chemical extraction, and particularly relates to a method for extracting and separating nickel, cobalt, tungsten, molybdenum and vanadium. BACKGROUND

[0002] Nickel-molybdenum ore molybdenum extraction slag, desulfurization waste catalyst and waste catalyst are solid wastes containing various valuable metals. If these solid wastes can be effectively recycled, not only the environmental pollution caused by them can be eliminated, but also the sustainable utilization of non-ferrous metal resources can be realized. Taking waste catalyst as an example, the recovery of valuable metals from waste catalyst has always been a research hotspot. The methods for recovering valuable metals from waste catalyst include wet leaching, pyrometallurgical enrichment, roasting-leaching recovery, among which the roasting-leaching process is a relatively mature recovery process. Roasting not only removes oil and carbon, but also converts metal sulfides into metal oxides that are more easily dissolved in acid. Combined with acid leaching, valuable metals can be leached at one time, and finally recovered from the acid leaching solution. The leaching solution containing multiple metal elements is extremely complex due to the complex composition of the leaching raw material and the variable leaching conditions. Often, the leaching solution contains multiple high-concentration valuable metals, and because the pH is low, the occurrence state of metal elements is extremely complex.

[0003] In the acid leaching solution, tungsten, molybdenum and vanadium generally exist in the form of oxygen-containing anions or oxygen-containing polyatomic anions, and nickel and cobalt exist in the form of cations. According to the difference in the form of these elements in the acid leaching solution, solvent extraction is commonly used in industry for separation and recovery. Common extractants include acidic extractants and acidic extractants. When using the above extractants alone, only part of the metal elements in the leaching solution can be preliminarily separated, and the extraction effect is not excellent, making it difficult to achieve group separation and deep separation of all elements, and often requiring other processes to achieve deep separation. At this time, problems such as long process, complex operation, and continuous loss of each metal element in the process, resulting in reduced recovery rate, will be faced. Therefore, researchers have developed a synergistic extraction system. The use of multiple extractants can improve the extraction rate and separation effect, but while improving the extraction rate of metal elements, the extraction rate of impurity metals is also improved, and the separation effect is deteriorated.

[0004] Sun Ying of Jilin University used P204+N235 to extract molybdenum, and found that the mixed extractant can improve the extraction of molybdenum through acid-base coupling effect, and there is a synergistic effect. Others also use this system to extract nickel, cobalt and iron, which can improve the extraction efficiency at the corresponding pH, but the types and contents of metal elements in the treated solution are relatively simple.

[0005] Patent CN 112342389 A discloses a method for recovering molybdenum and nickel from waste chemical catalysts. First, the waste catalyst is wet ground, and the wet ground slurry is leached with sulfuric acid. The leaching solution is first extracted with P204+TPB to extract vanadium, and then back-extracted with sulfuric acid to prepare V2O5. Then P204+N235 is used to extract molybdenum in the raffinate, and ammonia is used to back-extract to prepare ammonium molybdate, and finally the raffinate after molybdenum extraction is impurity-removed to prepare nickel sulfate. This method has many steps, and each step of extraction and back-extraction needs to be purified and impurity-removed.

[0006] Patent US4432949-A discloses a method for separating a mixture of metals in an aqueous solution, first precipitating vanadium, then using LIX64 and LIX51 in sequence to extract and separate nickel and cobalt, and finally obtaining a raffinate containing molybdenum. This method needs to reduce Co(III) to Co(II) to improve the extraction effect, increasing the operation process. In addition, the separation of vanadium uses a precipitation method, which has general separation effect.

[0007] In summary, existing extraction technologies pay more attention to the separation and recovery of elements such as molybdenum and nickel with high content, while the related technical processes for separating and recovering metal elements in complex multi-metal leaching solution are complex, the loss rate of elements in the recovery process is high, and it is difficult to achieve high selectivity separation of nickel, cobalt, tungsten, molybdenum and vanadium. In view of the problems of low recovery rate, poor separation effect and complex operation process in the extraction and separation of nickel, cobalt, tungsten, molybdenum and vanadium in complex multi-metal leaching solution, it is necessary to develop a new extraction system to recover metal elements with high selectivity and high efficiency. SUMMARY

[0008] In view of the problems of difficult co-extraction of tungsten, molybdenum and vanadium, and more difficult to achieve high selectivity separation of tungsten, molybdenum, vanadium and nickel, cobalt, the first purpose of the present application is to provide a new method for extracting and separating nickel, cobalt, tungsten, molybdenum and vanadium, which aims to achieve co-extraction of tungsten, molybdenum and vanadium, and improve the selectivity of extraction and separation of tungsten, molybdenum, vanadium and nickel, cobalt.

[0009] In the co-ion system of tungsten, molybdenum, vanadium and nickel, cobalt, high selectivity co-extraction of tungsten, molybdenum and vanadium, and reduction of nickel and cobalt extraction, so as to achieve high selectivity of tungsten, molybdenum, vanadium and nickel, cobalt co-extraction separation is a problem that needs to be further solved, in view of the technical problem, the present application provides the following improvement scheme:

[0010] A method for extracting and separating nickel, cobalt, tungsten, molybdenum and vanadium, mixing a water phase containing nickel, cobalt, tungsten, molybdenum and vanadium ions to be treated and an extraction organic phase to extract, and separating to obtain a loaded organic phase rich in tungsten, molybdenum and vanadium ions and a raffinate rich in nickel and cobalt ions;

[0011] The extraction organic phase is an organic phase obtained by acidifying a mixed solution containing a Formula 1 extractant, a Formula 2 extractant, a Formula 3 extractant and a diluent;

[0012]

[0013]

[0014] R1 is C6-C12 alkyl; R2 is H or C6-C12 alkyl; M is H, Na, K or NH4; 10 R1 is C6-C12 alkyl; R2 is H or C6-C12 alkyl; M is H, Na, K or NH4; 10 R1 is C6-C12 alkyl; R2 is H or C6-C12 alkyl; M is H, Na, K or NH4;

[0015] R3 is C6-C12 alkyl; 10 R3 is C6-C12 alkyl;

[0016] R4 is C3-C6 alkyl;

[0017] The volume content of the total extractant of formula 1, formula 2 and formula 3 in the extraction organic phase is 20-70%, wherein the volume ratio of formula 1, formula 2 and formula 3 is 1:1-5:1-5.

[0018] The pH of the starting water phase to be treated for extraction (also referred to as the extraction starting pH) is 0.5-2.

[0019] In view of the problems that tungsten, molybdenum and vanadium exist in complex forms at a low pH, co-extraction is not ideal, and it is difficult to separate them with high selectivity in the system of tungsten, molybdenum, vanadium, nickel and cobalt, the present application innovatively finds that the combined organic phase of formula 1-formula 3, combined with the joint control of pre-acidification process, the content and ratio of extractant and extraction pH, can co-extract tungsten, molybdenum and vanadium, while reducing the extraction rate of nickel and cobalt, and realize the selective separation of multiple metals in the acid leaching solution.

[0020] In the present application, the water phase to be treated is an acidic aqueous solution containing nickel, cobalt, tungsten, molybdenum and vanadium ions; further can be an acid leaching solution of solid waste containing nickel, cobalt, tungsten, molybdenum and vanadium. For example, the solid waste can be at least one of nickel-molybdenum ore molybdenum extraction residue, desulfurization waste catalyst and waste catalyst.

[0021] Preferably, the acid leaching solution is at least one of sulfuric acid leaching solution, hydrochloric acid leaching solution and nitric acid leaching solution.

[0022] In the present application, the concentration of each ion in the water phase to be treated is not particularly required, for example, in the water phase to be treated, the concentration of Ni is between 5-100 g / L, the concentration of Co is between 5-50 g / L, the concentration of Mo is between 5-50 g / L, the concentration of V is between 1-20 g / L, and the concentration of W is between 1-30 g / L.

[0023] In the present application, the pH of the water phase to be treated is controlled at 0.5-2 before extraction, and then mixed with the extraction organic phase for extraction. In the present application, the extraction initial pH and the composition of the extraction organic phase and the combined acidification treatment are synergistically improved for the co-extraction of tungsten, molybdenum and vanadium, and the selective separation efficiency of tungsten, molybdenum and vanadium, and nickel and cobalt.

[0024] In the present application, the combined control of the acidification, the volume content of each extractant in the organic phase, the ratio and the extraction pH of the combination of formula 1-3 is synergistically improved for the extraction rate of tungsten, molybdenum and vanadium, and the high efficiency selectivity of tungsten, molybdenum and vanadium, and nickel and cobalt.

[0025] As a preferred, in the formula 1, the R1, R2 is C6-C 10 straight chain or branched alkyl; preferably C7-C9 branched alkyl. Considering the effect and cost, the extractant of formula 1 is preferably formula 1-A:

[0026]

[0027] As a preferred, in the formula 2, the R3 is C6-C 10 straight chain alkyl, preferably C7-C9 straight chain alkyl.

[0028] Further preferably, the extractant of formula 2 is formula 2-A:

[0029]

[0030] As a preferred, in the formula 3, the R4 is C3-C5 straight chain alkyl. Preferably, the extractant of formula 3 is formula 3-A:

[0031]

[0032] The present application research found that controlling the content and the ratio of the components of formula 1-3 in the extraction organic phase helps to further improve the synergistic effect of the components, and further synergistically improve the extraction rate of tungsten, molybdenum and vanadium, and the high efficiency selectivity of tungsten, molybdenum and vanadium, and nickel and cobalt.

[0033] As a preferred, in the extraction organic phase, the total content of formula 1, formula 2 and formula 3 extractants is 20-50v%, further preferably 30-40v.%, wherein the volume ratio of formula 1, formula 2 and formula 3 is 1:1-3:1.5-3.

[0034] In the present application, the diluent has no special requirements, for example, the diluent is a liquid hydrocarbon organic matter, preferably at least one of sulfonated kerosene, No. 260 solvent oil, aviation kerosene.

[0035] In the present application, the mixed solution containing formula 1, formula 2, formula 3 and diluent is subjected to acidification treatment to obtain the extraction organic phase. The present application finds that the acidification treatment of the mixed solution containing formula 1 to formula 3 and diluent can further improve the synergy of the components, further improve the co-extraction efficiency of tungsten, molybdenum and vanadium, and improve the separation effect of tungsten, molybdenum, vanadium and nickel-cobalt.

[0036] As preferred, the acid used in the acidification treatment stage is one or more of sulfuric acid, hydrochloric acid and nitric acid.

[0037] In the present application, the acidification degree is 90-100%.

[0038] In the present application, the extraction operation can be carried out based on the existing means. For example, the extraction method is single-stage extraction or multi-stage extraction, and when it is multi-stage extraction, it can be countercurrent extraction. Preferably, the extraction stage is 1-10 stages.

[0039] In the present application, the O / A volume ratio of the extraction stage is 5:1-1:5.

[0040] As preferred, the pH of the extraction is 0.8-1.5. That is, the pH of the aqueous phase is preferably controlled to be 0.8-1.5, and then mixed with the extraction organic phase to carry out extraction.

[0041] Further preferably, the pH of the extraction is 1.2-1.3.

[0042] In the present application, the loaded organic phase is subjected to stripping treatment to obtain a stripping solution rich in tungsten, molybdenum and vanadium ions.

[0043] The stripping agent is an alkali solution, and preferably a mixed solution of one or more of sodium hydroxide, ammonia, sodium carbonate, sodium bicarbonate or ammonium bicarbonate with a pH of 8-14.

[0044] In the present application, the organic phase after stripping can be recycled as the extraction organic phase.

[0045] Advantages

[0046] The present application innovatively finds that the combination of formula 1 to formula 3, the pre-acidification process, the content and proportion of the extraction agent and the combined control of the solution pH can realize synergy, improve the co-extraction effect of tungsten, molybdenum and vanadium, and further reduce the accompanying extraction of nickel-cobalt to realize high-efficiency selective separation.

[0047] The present application uses a new extraction system to extract and separate nickel-cobalt, tungsten-molybdenum-vanadium from the acid leaching solution of waste catalyst containing nickel-cobalt-tungsten-molybdenum-vanadium. This method has good separation effect of nickel-cobalt, tungsten-molybdenum-vanadium, less loss of organic phase, is friendly to the environment, and is easy to realize industrialization. Specific implementation method

[0048] Example 1

[0049] Aqueous phase: waste catalyst mixed acid leaching solution, in which Ni 23.56 g / L, Co 13.8 g / L, Mo 25.4 g / L, V 5.9 g / L, W 1.94 g / L, pH value 1.98, the pH value is adjusted to 1.2 (initial pH) by sulfuric acid.

[0050] Organic phase (extraction organic phase): 5% of formula 1-A + 10% of formula 2-A + 20% of formula 3-A + 65% of sulfonated kerosene (volume fraction), the organic phase is contacted with 0.5 mol / L of H2SO4 before extraction, 100% acidification.

[0051] Strip agent: 2 mol / L NaOH solution.

[0052] Extraction: the aqueous phase and the organic phase are mixed and placed in a water bath constant temperature shaking box, the temperature is set to 25℃, the shaking time is 15 min, after shaking, it is placed in a 20℃ constant temperature water bath pot for static separation, the separation time is 15 min, the upper and lower two phases are obtained, the upper phase is the loaded organic phase containing tungsten, molybdenum and vanadium, and the lower phase is the raffinate containing nickel and cobalt.

[0053] Stripping: the loaded organic phase is mixed with the stripping agent and placed in a water bath constant temperature shaking box, the temperature is set to 30℃, the shaking time is 10 min, after shaking, it is placed in a 20℃ constant temperature water bath pot for static separation, the separation time is 10 min, the upper and lower two phases are obtained, the upper phase is the organic phase, and the lower phase is the stripping solution rich in tungsten, molybdenum and vanadium.

[0054] Analysis: after the extraction and stripping are stable, the raffinate and the stripping solution are sampled and analyzed, and the results are as follows:

[0055] Results: the extraction rate of tungsten is 99.4%, the extraction rate of molybdenum is 99.2%, the extraction rate of vanadium is 99.7%, the extraction rate of nickel is 0.55%, and the extraction rate of cobalt is 0.38%. In the stripping solution, Mo 62.08 g / L, V 14.68 g / L, W 4.7 g / L, the stripping rate of molybdenum is 98.56%, the stripping rate of vanadium is 99.8%, and the stripping rate of tungsten is 97.62%.

[0056] Example 2

[0057] Compared with Example 1, the only difference is the change of the ratio of formula 1-A, formula 2-A and formula 3-A in the organic phase, and the experimental groups are as follows:

[0058] In the organic phase, the extraction components include 35% of formula 1-A, formula 2-A and formula 3-A in total volume ratio, and the difference lies in the change of the volume ratio of the three, for example:

[0059] A: The volume ratio of Formula 1-A, Formula 2-A, and Formula 3-A is 1:2:2, that is, in the extraction organic phase, there are 7% of Formula 1-A+14% of Formula 2-A+14% of Formula 3-A (volume fraction);

[0060] B: The volume ratio of Formula 1-A, Formula 2-A, and Formula 3-A is 1:3:3, that is, in the extraction organic phase, there are 5% of Formula 1-A+15% of Formula 2-A+15% of Formula 3-A.

[0061] C: The volume ratio of Formula 1-A, Formula 2-A, and Formula 3-A is 1:1:1.5, that is, in the extraction organic phase, there are 10% of Formula 1-A+10% of Formula 2-A+15% of Formula 3-A+65% of sulfonated kerosene (volume fraction)

[0062] Other operations and parameters are the same as in Example 1; analysis: after the extraction and stripping stability, the raffinate and stripping liquid are sampled and analyzed, and the results are as follows:

[0063] Results:

[0064] A: The extraction rate of tungsten is 99.7%, the extraction rate of molybdenum is 99.1%, the extraction rate of vanadium is 99.7%, the extraction rate of nickel is 0.67%, and the extraction rate of cobalt is 0.42%.

[0065] B: The extraction rate of tungsten is 99.6%, the extraction rate of molybdenum is 99.7%, the extraction rate of vanadium is 99.8%, the extraction rate of nickel is 0.25%, and the extraction rate of cobalt is 0.18%.

[0066] C: The extraction rate of tungsten is 99.37%, the extraction rate of molybdenum is 99.43%, the extraction rate of vanadium is 99.82%, the extraction rate of nickel is 0.51%, and the extraction rate of cobalt is 0.39%.

[0067] Example 3

[0068] Compared with Example 1, the only difference is that the total content percentage of Formula 1-A, Formula 2-A, and Formula 3-A is changed, and the experimental groups are as follows:

[0069] That is, in the organic phase, the extraction components include Formula 1-A, Formula 2-A, and Formula 3-A with a volume ratio of 1:2:4, and the total volume content of the extractant is as follows:

[0070] A: 27%, that is, in the extraction organic phase, there are 3% of Formula 1-A+6% of Formula 2-A+18% of Formula 3-A+the balance of sulfonated kerosene (volume fraction);

[0071] B: 49%, that is, in the extraction organic phase, there are 7% of Formula 1-A+14% of Formula 2-A+28% of Formula 3-A+51% of sulfonated kerosene (volume fraction)

[0072] C: 70%, i.e. in the organic phase of extraction, 10% of formula 1-A + 20% of formula 2-A + 40% of 3-A + 30% of sulfonated kerosene (volume fraction)

[0073] Other operations and parameters are the same as in Example 1.

[0074] Results:

[0075] A: the extraction rate of tungsten is 99.7%, the extraction rate of molybdenum is 99.76%, the extraction rate of vanadium is 99.94%, the extraction rate of nickel is 0.68%, and the extraction rate of cobalt is 1.03%.

[0076] B: the extraction rate of tungsten is 97.53%, the extraction rate of molybdenum is 97.46%, the extraction rate of vanadium is 98.85%, the extraction rate of nickel is 1.88%, and the extraction rate of cobalt is 2.35%.

[0077] C: the extraction rate of tungsten is 97.41%, the extraction rate of molybdenum is 96.14%, the extraction rate of vanadium is 97.1%, the extraction rate of nickel is 3.42%, and the extraction rate of cobalt is 3.75%.

[0078] Example 4

[0079] Compared with Example 1, the only difference is that the conditions of the extraction stage are changed, and the experimental groups are:

[0080] A: the initial pH value is adjusted to 0.88 with sulfuric acid.

[0081] B: the initial pH value is adjusted to 1.64 with sulfuric acid.

[0082] C: the initial pH value is adjusted to 1.3 with sulfuric acid.

[0083] Other operations and parameters are the same as in Example 1.

[0084] Results:

[0085] A: the extraction rate of tungsten is 99.93%, the extraction rate of molybdenum is 99.34%, the extraction rate of vanadium is 98.7%, the extraction rate of nickel is 0.47%, and the extraction rate of cobalt is 0.29%.

[0086] B: the extraction rate of tungsten is 99.18%, the extraction rate of molybdenum is 99.4%, the extraction rate of vanadium is 99.9%, the extraction rate of nickel is 1.94%, and the extraction rate of cobalt is 2.31%.

[0087] C: the extraction rate of tungsten is 99.64%, the extraction rate of molybdenum is 99.36%, the extraction rate of vanadium is 99.57%, the extraction rate of nickel is 0.45%, and the extraction rate of cobalt is 0.26%.

[0088] Comparative Example 1:

[0089] The difference between Example 1 and Comparative Example 1 is that the type of extractant is changed. The experimental groups are as follows:

[0090] Organic phase:

[0091] A: 10% of Formula 2-A + 25% of Formula 3-A + 65% of sulfonated kerosene (volume fraction)

[0092] B: 10% of Formula 1-A + 25% of Formula 2-A + 65% of sulfonated kerosene (volume fraction)

[0093] C: 10% of Formula 1-A + 25% of Formula 3-A + 65% of sulfonated kerosene (volume fraction)

[0094] D: 5% of Formula 1-B + 10% of Formula 2-A + 20% of Formula 3-A + 65% of sulfonated kerosene (volume fraction)

[0095]

[0096] Formula 1-B is

[0097] Other operations and parameters are the same as in Example 1.

[0098] Results:

[0099] A: The extraction rate of tungsten is 93.13%, the extraction rate of molybdenum is 80.45%, the extraction rate of vanadium is 91.23%, the extraction rate of nickel is 4.82%, and the extraction rate of cobalt is 7.19%.

[0100] B: The extraction rate of tungsten is 90.18%, the extraction rate of molybdenum is 91.4%, the extraction rate of vanadium is 89.21%, the extraction rate of nickel is 10.31%, and the extraction rate of cobalt is 8.54%.

[0101] C: The extraction rate of tungsten is 9.27%, the extraction rate of molybdenum is 8.15%, the extraction rate of vanadium is 2.88%, the extraction rate of nickel is 1.55%, and the extraction rate of cobalt is 0.77%.

[0102] D: The extraction rate of tungsten is 92.53%, the extraction rate of molybdenum is 90.2%, the extraction rate of vanadium is 90.97%, the extraction rate of nickel is 7.34%, and the extraction rate of cobalt is 6.52%.

[0103] Comparative Example 2

[0104] The difference between Example 1 and Comparative Example 2 is that the volume ratio of Formula 1-A-Formula 2-A-Formula 3-A in the organic phase is the same as in Example 1, and the difference is that the total volume content is 15%. Other operations and parameters are the same as in Example 1.

[0105] The extraction rate of tungsten is 65.42%, the extraction rate of molybdenum is 70.28%, the extraction rate of vanadium is 75.14%, the extraction rate of nickel is 2.68%, and the extraction rate of cobalt is 1.98%.

[0106] Comparative Example 3

[0107] Compared with Example 1, the only difference is that the organic phase is changed, and the difference is as follows:

[0108] The organic phase is 5% of formula 1-A+10% of formula 2-A+20% of formula 3-A+65% of sulfonated kerosene (volume fraction). Among them, 1-A is contacted with 10 mol / L NaOH before extraction for saponification, and the saponification rate is 60%. 2-A is contacted with 0.5 mol / L H2SO4 before extraction, and 100% acidification. After pretreatment of the raw material, the organic phase is formed by mixing.

[0109] Other operations and parameters are the same as those in Example 1.

[0110] The extraction rate of tungsten is 93.4%, the extraction rate of molybdenum is 94.2%, the extraction rate of vanadium is 94.7%, the extraction rate of nickel is 6.22%, and the extraction rate of cobalt is 7.84%.

[0111] Comparative Example 4

[0112] Compared with Example 1, the only difference is that formula 1-A, formula 2-A and formula 3-A of the organic phase are not treated together, and the difference is as follows:

[0113] The organic phase is 5% of formula 1-A+10% of formula 2-A+20% of formula 3-A+65% of sulfonated kerosene (volume fraction). 2-A is contacted with 0.5 mol / L H2SO4 before extraction, and 100% acidification. After acidification of formula 2-A, formula 1-A and formula 3-A of the set proportion are mixed to form the organic phase. After pretreatment of the raw material, the organic phase is formed by mixing.

[0114] Other operations and parameters are the same as those in Example 1.

[0115] The extraction rate of tungsten is 95.77%, the extraction rate of molybdenum is 94.13%, the extraction rate of vanadium is 95.04%, the extraction rate of nickel is 6.57%, and the extraction rate of cobalt is 8.34%.

[0116] Comparative Example 5

[0117] Compared with Example 1, the only difference is that the initial pH of the aqueous phase is controlled to be 2.5, and other operations and parameters are the same as those in Example 1.

[0118] Results:

[0119] The extraction rate of tungsten is 85.41%, the extraction rate of molybdenum is 86.33%, the extraction rate of vanadium is 81.69%, the extraction rate of nickel is 9.55%, and the extraction rate of cobalt is 10.38%.

Claims

1. A method for extracting and separating nickel, cobalt, tungsten, molybdenum and vanadium, characterized in that, Mixing the treated water phase containing nickel, cobalt, tungsten, molybdenum, vanadium ions and the extraction organic phase to carry out extraction separation, to obtain the loaded organic phase enriched with tungsten, molybdenum and vanadium and the raffinate water phase enriched with nickel and cobalt; The extraction organic phase is an organic phase containing formula 1 extractant, formula 2 extractant, formula 3 extractant and diluent after acidification treatment; Formula 1 Formula 2 Formula 3 R1 and R2 are individually C6~C 10 Alkyl group; wherein M is H, Na, K or NH4; R3 is C6~C 10 Alkyl groups; R4 is C3-C6 alkyl; The total volume content of formula 1, formula 2 and formula 3 in the extraction organic phase is 20-70v%, wherein the volume ratio of formula 1, formula 2 and formula 3 is 1:1-5:1-5; The pH of the treated water phase at the beginning of extraction is 0.5-2.

2. The method for extracting and separating nickel, cobalt, tungsten, molybdenum and vanadium according to claim 1, characterized in that, The treated water phase is an acidic aqueous solution containing nickel, cobalt, tungsten, molybdenum and vanadium ions.

3. The method for extracting and separating nickel, cobalt, tungsten, molybdenum and vanadium according to claim 2, characterized in that, The treated water phase is an acid leaching solution containing nickel, cobalt, tungsten, molybdenum and vanadium elements and / or compounds of the solid.

4. The method for separating and extracting nickel, cobalt, tungsten, molybdenum and vanadium according to claim 3, characterized in that, The solid is one or more of nickel-molybdenum ore molybdenum extraction residue and waste catalyst.

5. The method for separating and extracting nickel, cobalt, tungsten, molybdenum and vanadium according to claim 3, characterized in that, The acid leaching solution is at least one of sulfuric acid leaching solution, hydrochloric acid leaching solution and nitric acid leaching solution.

6. The method for separating and extracting nickel, cobalt, tungsten, molybdenum and vanadium according to claim 1, characterized in that In the treated water phase, the concentration of Ni is between 5-100g / L, the concentration of Co is between 5-50g / L, the concentration of Mo is between 5-50g / L, the concentration of V is between 1-20g / L and the concentration of W is between 1-30g / L.

7. The method for separating and extracting nickel, cobalt, tungsten, molybdenum and vanadium according to claim 1, wherein the step of separating and extracting nickel, cobalt, tungsten, molybdenum and vanadium is performed by using a solvent extraction method. In the formula 1, R1, R2are C6~C 10 straight chain or branched alkyl.

8. The method for separating and extracting nickel, cobalt, tungsten, molybdenum and vanadium according to claim 1, wherein, R1 and R2 are C7-C9 branched alkyl.

9. The method for separating and extracting nickel, cobalt, tungsten, molybdenum and vanadium according to claim 1, wherein, In Formula 2, R3is a linear alkyl group of C6-Ci8. 10 .

10. The method for extracting and separating nickel, cobalt, tungsten, molybdenum and vanadium according to claim 9, characterized in that, In formula 2, R3 is C7-C9 straight-chain alkyl.

11. The method for separating and extracting nickel, cobalt, tungsten, molybdenum and vanadium according to claim 1, wherein, In formula 3, R4 is C3-C5 straight-chain alkyl.

12. The method for separating and extracting nickel, cobalt, tungsten, molybdenum and vanadium according to any one of claims 1-11, wherein, The total volume content of formula 1, formula 2 and formula 3 in the extraction organic phase is 20-50v%, wherein the volume ratio of formula 1, formula 2 and formula 3 is 1:1-3:1.5-3.

13. The method for extracting and separating nickel, cobalt, tungsten, molybdenum and vanadium according to claim 12, characterized in that, The total volume content of formula 1, formula 2 and formula 3 in the extraction organic phase is 30-40v%.

14. The method for separating and extracting nickel, cobalt, tungsten, molybdenum and vanadium according to claim 1, wherein, The diluent is a liquid hydrocarbon organic matter. ​ 15. The method for extracting and separating nickel, cobalt, tungsten, molybdenum and vanadium according to claim 14, characterized in that, The diluent is at least one of sulfonated kerosene, No. 260 solvent oil and aviation kerosene.

16. The method for separating and extracting nickel, cobalt, tungsten, molybdenum and vanadium as claimed in claim 1, wherein, The acid used in the acidification treatment stage is one or more of sulfuric acid, hydrochloric acid and nitric acid.

17. The process for separation of nickel, cobalt, tungsten, molybdenum and vanadium by solvent extraction as claimed in claim 1 wherein, The O / A volume ratio in the extraction stage is 5:1-1:

5. ​ 18. The process for separation of nickel, cobalt, tungsten, molybdenum and vanadium by solvent extraction as claimed in claim 1 wherein, The loaded organic phase is subjected to stripping treatment to obtain a stripping solution enriched with tungsten, molybdenum and vanadium ions. ​ 19. The method for separating and extracting nickel, cobalt, tungsten, molybdenum and vanadium according to claim 18, wherein, The stripping uses one or more of sodium hydroxide, sodium carbonate and sodium bicarbonate.

Images