Method for extracting niobium and / or scandium in phosphoric acid solution system

Abstract

The invention belongs to the field of hydrometallurgy, and particularly relates to a method for extracting niobium and / or scandium in a phosphoric acid solution system, which is characterized in that the phosphoric acid solution system containing niobium and / or scandium and an extraction organic phase are subjected to auxiliary extraction under a composite field of ultrasonic-magnetic field to obtain a loaded organic phase. Innovative research shows that extraction is carried out under an ultrasonic-magnetic field composite field, the final physicochemical characteristics of niobium-scandium in a phosphoric acid solution can be adapted accidentally, excellent extraction capacity can be obtained accidentally, and especially excellent scandium-niobium separation selectivity can be obtained under a composite phosphoric acid system containing niobium and scandium.

Description

Technical Field

[0001] This invention relates to the field of hydrometallurgy, specifically to the extraction of niobium and scandium elements from phosphoric acid solution systems. Background Technology

[0002] Niobium (Nb) and scandium (Sc) are key strategic metals in modern industry, widely used in high-temperature alloys, superconducting materials, and electronic ceramics. However, the uneven distribution and low grade of global niobium and scandium resources pose challenges to efficient extraction and utilization. For example, the Bayan Obo deposit has abundant niobium and scandium reserves, but the content is low, making it difficult to effectively enrich them using traditional beneficiation methods, resulting in high extraction costs. Therefore, recovering niobium and scandium from leaching solutions is currently the main utilization method and is key to future efficient utilization. Acid leaching is the main process for leaching and extracting niobium and scandium ore, with sulfuric acid leaching-extraction being the most widely used due to its low cost and mature technology. However, this method has many drawbacks. For calcium-containing minerals (such as the Bayan Obo deposit), sulfuric acid leaching produces a large amount of calcium sulfate precipitate, which not only coats mineral particles and reduces leaching efficiency but also forms scale, affecting the continuity and stability of the process. In addition, sulfuric acid reacts with fluorite to produce corrosive hydrofluoric acid, which corrodes equipment and produces toxic waste gas, causing environmental pollution.

[0003] To address the drawbacks of sulfuric acid leaching, our team developed a phosphoric acid leaching process, exploring its application in the efficient extraction of niobium and nickel ore resources (CN120174214A). The core advantages of this process are: 1. Avoidance of calcium salt precipitation: Calcium phosphate has a higher solubility than calcium sulfate, effectively preventing the precipitation layer from encapsulating mineral particles and sticking to equipment, thereby improving leaching efficiency and continuous equipment operation. 2. Inhibition of hydrofluoric acid formation: The hydrofluoric acid generated from the reaction of phosphoric acid and fluorite combines with phosphate ions to form fluorophosphate complexes, reducing hydrofluoric acid concentration, mitigating equipment corrosion, reducing harmful emissions, and improving environmental performance. 3. Selective leaching: By adjusting acidity, temperature, and leaching time, the phosphoric acid leaching process can achieve selective leaching of niobium and scandium, effectively controlling the leaching of other elements and reducing the difficulty and cost of subsequent separation and purification.

[0004] Phosphoric acid leaching is not only suitable for Bayan Obo mine, but also has broad application prospects for other niobium-tantalum ores such as tantalum-columbite and pyrochlore. Compared with sulfuric acid leaching, which faces problems such as calcium sulfate precipitation and equipment corrosion in these ores, phosphoric acid leaching can effectively overcome these difficulties, improve niobium-tantalum leaching efficiency, and reduce costs. For example, for high-calcium tantalum-columbite, phosphoric acid leaching can avoid calcium sulfate precipitation; in addition, in the phosphoric acid leaching system, phosphoric acid also reacts with silicate minerals to form amorphous silica, reducing the silicon leaching rate and minimizing its interference with subsequent separation and purification.

[0005] Current extraction research mainly focuses on sulfuric acid-hydrofluoric acid and sulfuric acid systems, while research on niobium-scandium extraction from phosphoric acid leachates is still lacking. Patent CN120082752A discloses a selective extraction method for rare earth niobium solutions in a sulfuric acid system, involving niobium extraction with organic matter, acid washing of rare earth elements, and back-extraction to obtain a niobium-rich precipitate. Patent CN117285073A discloses a method for recovering niobium-scandium in a sulfuric acid system, employing sodium sulfate precipitation of rare earth elements, extraction to remove iron, acid washing to remove titanium, back-extraction, and oxalic acid precipitation. Patent CN116287707A discloses a method for extracting niobium in an oxalic acid system, adjusting the pH of the leachate, using quaternary ammonium salts to extract niobium and titanium, and then back-extracting titanium and niobium separately with dilute sulfuric acid and acid. None of these methods are applicable to phosphoric acid systems, and they do not adequately consider scandium recovery. Summary of the Invention

[0006] In view of the lack of extraction methods for niobium and / or scandium in phosphoric acid solution systems, the present invention aims to provide an efficient method for extracting niobium and scandium from phosphoric acid leachate, so as to solve the problem of difficulty in separating and recovering niobium and scandium in niobium-scandium-containing phosphoric acid leachate.

[0007] Niobium and scandium in phosphoric acid systems mainly exist as phosphides and complexes. These substances are stable and difficult to selectively partition in conventional organic phases, making extraction challenging, especially for systems containing both scandium and niobium. It is difficult to achieve highly selective extraction and separation of niobium and scandium using extraction processes. To address this problem, this invention, after in-depth research, provides the following improved solution:

[0008] A method for extracting niobium and / or scandium from a phosphoric acid solution system involves extracting the niobium- and / or scandium-containing phosphoric acid solution system and the extractable organic phase under an ultrasonic-magnetic field-assisted extraction to obtain a loaded organic phase.

[0009] To address the difficulty in extracting scandium and niobium in phosphoric acid systems due to their unique characteristics, this invention innovatively demonstrates that extraction under a combined ultrasonic-magnetic field unexpectedly adapts to the final physicochemical characteristics of niobium and scandium in phosphoric acid solutions, resulting in unexpectedly excellent extraction capabilities. In particular, in complex phosphoric acid systems containing niobium and scandium, excellent scandium-niobium separation selectivity can also be achieved.

[0010] In this invention, the phosphoric acid solution system is a leachate obtained by leaching materials containing niobium and / or scandium with a phosphoric acid solution;

[0011] Preferably, the concentration of the components in the phosphoric acid solution system is not particularly required; for example, the concentration of phosphoric acid is 4~12 mol / L. Furthermore, when the solution system contains niobium, its concentration can be 0.1 g / L~5 g / L; considering recovery efficiency and value, it can further be 0.5~5 g / L, and even further, a low concentration system of 1~1.5 g / L. Additionally, when the solution system contains scandium, its concentration can be 2~50 mg / L; considering recovery efficiency and value, it can further be 10~50 mg / L; even further, a low concentration system of 10~20 mg / L. The process described in this invention can be adapted for the efficient recovery of phosphoric acid systems with low Sc and Nb content, especially for phosphoric acid systems containing both Sc and Nb, where efficient recovery of Sc and Nb can also be achieved.

[0012] Preferably, the phosphoric acid solution system is pretreated with acid, wherein the acid is at least one of hydrochloric acid and sulfuric acid.

[0013] In this invention, the aforementioned pretreatment helps to combine with the subsequent ultrasonic-magnetic field combined field extraction process to further enhance the extraction effect of scandium and niobium.

[0014] In this invention, the acid used in the pretreatment can be an acid solution of any concentration, for example, a saturated solution with a concentration of 5% or higher.

[0015] In this invention, the volume ratio of the phosphoric acid solution system to the acid can be reasonably adjusted as needed, for example, it can be 1:0.05~0.5; further, it can be 1:0.1~0.15.

[0016] The technical solution of the present invention may include three implementation methods with a unified inventive concept: Solution A: When the phosphoric acid solution system is a scandium-containing phosphoric acid solution (that is, a scandium-containing phosphoric acid system with low niobium content, such as below 0.01 g / L or even without niobium), it is subjected to the aforementioned auxiliary extraction to obtain a scandium-loaded organic phase.

[0017] Option B: When the phosphoric acid solution system is a niobium-containing phosphoric acid solution (that is, a niobium-containing phosphoric acid system with low scandium content, such as below 0.5 mg / L or even without scandium), it is subjected to the aforementioned auxiliary extraction to obtain a niobium-loaded organic phase.

[0018] Scheme C: When the phosphoric acid solution system is a phosphoric acid solution containing scandium and niobium, it is first subjected to a first-stage auxiliary extraction to obtain a scandium-loaded organic phase and a niobium-containing raffinate; then the niobium-containing raffinate is subjected to a second-stage auxiliary extraction to obtain a niobium-loaded organic phase.

[0019] In this invention, during the scandium extraction process in schemes A and C, the extractant organic phase for extracting scandium includes extractant A, which comprises C6~C6. 20 Phosphate ester, C6~C 20 Tertiary carbonic acid, C2~C 10 Acylated oxime acids, C6~C 20 At least one of alkyl tertiary amines and trialkylphosphine oxides.

[0020] The phosphate ester can be at least one of phosphate diesters and phosphate triesters, such as typical P204, P507, tributyl phosphate, etc.

[0021] Further, the extractant A includes at least one of P204, P507, tert-carbonic acid, acetyloxyoxime acid, mixed trialkylamines, tributyl phosphate, and a mixture of trialkylphosphine oxides; more preferably, it is P507. Studies have shown that using P507 in combination with the ultrasonic-magnetic field composite field described in this invention can further synergistically adapt to the phosphoric acid system, which helps to further improve the extraction effect of scandium.

[0022] In this invention, the extracted organic phase further includes a hydrophobic diluent. The hydrophobic diluent includes, for example, at least one selected from kerosene, carbon tetrachloride, hexane, and isooctane.

[0023] Furthermore, the content of extractant A is 2~50v, further can be 20~40v; even further can be 30~35v.

[0024] Preferably, during scandium extraction, the O / A volume ratio is 1:5 to 3:1; more preferably, it is 1:1 to 2; and even more preferably, it is 1:1 to 1.5. Studies have shown that the preferred ratio can further improve the synergy between the extraction volume and the ultrasonic-magnetic field composite field, and can further synergistically adapt to the phosphoric acid system, which helps to further improve the scandium extraction effect.

[0025] During the extraction of scandium, there are no special requirements for the extraction temperature. For example, it can be 15℃~50℃, or even room temperature of 20~30℃.

[0026] During the extraction of scandium, the extraction time can be adjusted reasonably according to the phase separation situation, as long as oil and water phase separation can be achieved, for example, it can be 5~20 minutes.

[0027] In the niobium extraction process of embodiments B and C of the present invention, the extractant organic phase for extracting niobium includes extractant B, which comprises C6~C6. 20 Phosphate ester, C4~C 10 Alkyl ketones, C5~C 10 Cycloalkanes, C6~C 20 Alkylamine, C6~C 20Alkyl alcohols, C2~C 10 At least one of the amides.

[0028] In this invention, C4~C 10 Alkyl ketones can be asymmetric ketones. (C5~C) 10 Cycloalkanes can be five-membered or six-membered cycloalkanes.

[0029] Preferably, the extractant B is C6~C 20 Alkyl alcohols; more preferably, the extractant B comprises C8~C64. 16 Alkyl alcohols; further, C 10 ~C 14 Alkyl alcohols. The alkyl alcohol is a component with hydroxyl groups on an alkyl carbon chain of the stated carbon number, and the number of hydroxyl groups can be 1 to 2; the alkyl carbon chain can be a straight-chain or branched carbon chain. Furthermore, the alkyl alcohol is C10-2000. 10 ~C 14 Straight-chain alkyl alcohols. This invention demonstrates that using a preferred extractant B, combined with the ultrasonic-magnetic field composite extraction process described in this invention, can further adapt to the characteristics of niobium in the phosphoric acid system, helping to further improve the extraction capacity and selectivity of niobium.

[0030] In this invention, the extracted organic phase contains a hydrophobic diluent, wherein the content of extractant B is 10-70%, further 40-60%, and even further 45-50%.

[0031] Preferably, during the extraction of niobium, the O / A volume ratio is 1~3:1; more preferably, it can be 1~2:1.

[0032] During the extraction of niobium, the extraction temperature can be, for example, 15℃~50℃.

[0033] During the extraction of niobium, the extraction time can be adjusted reasonably according to the phase separation situation, for example, it can be 5~20 minutes.

[0034] In this invention, when only one type of niobium or scandium is used for extraction, extractant A and extractant B can be selected from the same type of extractant. Furthermore, even for a composite phosphoric acid system containing scandium and niobium, extractant A and extractant B can also be selected from the same type of extractant. In this case, the niobium extraction effect after scandium extraction can be improved by increasing the content of the extractant for niobium extraction and increasing the organic ratio. For example, in the organic phase of scandium extraction, the content of extractant A is controlled at 20-40 v%, and the W / O ratio is 1-2:1; in the organic phase of niobium extraction, the content of extractant B is controlled at 55-70 v%, and the W / O ratio is 1:2-3. Further, during the niobium extraction process, the niobium-containing raffinate after scandium extraction is pretreated with acid.

[0035] To further achieve the extraction and separation of scandium and niobium in the scandium-niobium composite phosphoric acid system, extractant A can be preferably a phosphate ester extractant, and extractant B can be a different type of extractant, such as an alkyl alcohol.

[0036] The ultrasonic-magnetic field composite field described in this invention refers to the simultaneous presence of both ultrasonic and magnetic field auxiliary effects during the extraction process.

[0037] In this invention, the ultrasonic intensity is 0.1 W / cm² to 1 W / cm²; more preferably, it can be 0.3 W / cm² to 0.6 W / cm². In this invention, the magnetic field intensity is 500 to 5000 Oe; more preferably, it can be 2000 to 5000 Oe. In this invention, under the preferred composite field, the extraction effect of niobium and scandium in the phosphoric acid system can be further enhanced.

[0038] Beneficial effects

[0039] This invention innovatively demonstrates that the extraction performed under a combined ultrasonic-magnetic field unexpectedly adapts to the final physicochemical characteristics of niobium-scandium in phosphoric acid solution, resulting in unexpectedly excellent extraction capabilities. In particular, in a complex phosphoric acid system containing niobium and scandium, excellent scandium-niobium separation selectivity can also be obtained. Attached Figure Description

[0040] Figure 1 This is a flowchart of the technical solution. Detailed Implementation

[0041] To better understand the present invention, the following embodiments are further illustrations of the present invention, but the content of the present invention is not limited to the following embodiments.

[0042] The phosphoric acid leaching solution used in this embodiment of the invention is for Bayan Obo ore.

[0043] The phosphoric acid solution system described in this invention also allows the presence of at least one impurity selected from Fe, Ti, Ce, Si, Ca, Na, Mg, Al, and Mn. For example, the Fe content can be below 4 g / L, and more specifically, it can be 2 to 3.5 g / L.

[0044] The Ti content can be below 0.4 g / L, and further can be 0.1~0.2 g / L.

[0045] The Ce content can be below 0.1 g / L, and further can be 0.01~0.05 g / L.

[0046] The Si content can be below 0.2 g / L, and further can be 0.01~0.1 g / L.

[0047] The Ca content can be below 5 g / L, and further can be 1~4 g / L.

[0048] The sodium content can be below 10 g / L, and further can be 2~8 g / L.

[0049] The Mg content can be below 1 g / L, and further can be 0.1~0.5 g / L.

[0050] The Al content can be below 1 g / L, and further can be 0.1~0.5 g / L.

[0051] The Mn content can be below 1 g / L, and further can be 0.1~1 g / L.

[0052] As an alternative, in the following cases, the concentrations of the main elements in the leachate are shown in Table 1, and the concentration of phosphoric acid is 6~7M.

[0053]

[0054] In the following examples, the extraction ratio refers to the volume ratio, and the content of the components in the organic phase refers to the volume percentage.

[0055] Example 1

[0056] (1) The niobium-scandium-containing leachate (Table 1) is mixed with the first organic phase in a 1:1 ratio, wherein the first organic phase contains 30% p2O4 and 70% kerosene;

[0057] (2) The above dispersion system was placed in a combined ultrasonic and magnetic field, the temperature was set to 20℃, and it was oscillated for 10 minutes. The ultrasonic intensity was 0.5 W / cm², and the magnetic field intensity was 3000 Oe.

[0058] (3) After separating the above dispersion system, a scandium-containing organic phase and a niobium-containing extract residue were obtained. The extraction rate of scandium was 85.63% and the extraction rate of niobium was 5.28%.

[0059] (4) The extract residue is mixed with the second organic phase in a 1:1 ratio, wherein the second organic phase comprises 50% octanol and 50% kerosene;

[0060] (5) The above dispersion system was placed in a combined ultrasonic and magnetic field and oscillated for 15 minutes. The ultrasonic intensity was 0.5 W / cm² and the magnetic field intensity was 3000 Oe.

[0061] (6) After separating the above dispersion system, a niobium-containing organic phase was obtained, with a niobium extraction rate of 78.63%;

[0062] (7) Scandium-enriched phase was obtained by back-extracting scandium-containing organic phase with 5 mol / L sodium hydroxide at an O / A ratio of 1:1, and scandium oxide was obtained by calcination at 500℃; the overall recovery rate of scandium in the whole process was 72.53%.

[0063] (7) Niobium-enriched material was obtained by back-extracting the niobium-containing organic phase with 8 mol / L sulfuric acid at a ratio of 1:2, and niobium oxide was obtained by calcination at 650℃; the overall recovery rate of niobium throughout the process was 65.36%.

[0064] Example 2

[0065] Compared with Example 1, the only difference is that the composition of the first organic phase in step 1 and the ratio of the first extraction process are changed. Specifically, the first organic phase contains 35% p507 and 65% kerosene; the ratio of water phase to organic phase is 2:1; and other operations and parameters are the same as in Example 1.

[0066] The result was that the scandium extraction rate in step 3 was 90.56%.

[0067] Example 3

[0068] Compared with Example 1, the only difference is that in step 4, the second organic phase includes 45% lauryl alcohol and 55% kerosene; and the ratio of the extract residue to the organic phase is 1:1; all other operations and parameters are the same as in Example 1.

[0069] The result was that the extraction rate of niobium in step 6 was 90.86%.

[0070] As demonstrated in Examples 1 and 3, using lauryl alcohol as a Nb extractant can achieve better synergy between the ultrasonic and magnetic field composite fields, which helps to further enhance the extraction effect of niobium. For example, it can achieve a better niobium extraction rate with a lower reagent dosage.

[0071] Example 4

[0072] Compared to Example 1, the only difference is that in step 2, the ultrasonic intensity is 0.8 W / cm² and the magnetic field strength is 4500 Oe during the extraction process. In step 5, the second stage of extraction also uses an ultrasonic intensity of 0.8 W / cm² and a magnetic field strength of 4500 Oe.

[0073] The results showed that the scandium extraction rate was 91.63% in step 3, and the niobium extraction rate was 90.31% in step 6.

[0074] Example 5

[0075] Compared with Example 1, the only difference is that in step 1, 10v% hydrochloric acid is added to the leachate in advance at a volume ratio of 1:0.1; all other operations and parameters are the same as in Example 1.

[0076] The results were as follows: In step 3, the scandium extraction rate was 92.54%. In step 6, the niobium extraction rate was 90.65%.

[0077] Example 6

[0078] Compared with Example 1, the only difference is that in the first extraction (step 1), the first organic phase contains 35% TBP and 65% kerosene, and the ratio of aqueous phase to organic phase is 1:1;

[0079] In the second extraction (step 4), the second organic phase contains 65% TBP and 35% kerosene; before extraction, 10v% hydrochloric acid is added to the extract residue (the volume ratio of extract residue to hydrochloric acid is 1:0.15); the ratio of aqueous phase to organic phase is 1:2. Other operations and parameters are the same as in Example 1.

[0080] The results showed that the scandium extraction rate was 88.64% in step 3 and the niobium extraction rate was 82.63% in step 6.

[0081] Comparative Example 1

[0082] Compared with Example 1, the only difference is that there is no ultrasonic field and magnetic field treatment in the extraction process of steps 2 and 5. All other operations and parameters are the same as in Example 1.

[0083] The results were as follows: in step 3, the scandium extraction rate was 42.35%, and in step 6, the niobium extraction rate was 31.27%.

[0084] Comparative Example 2

[0085] Compared with Example 1, the only difference is that the extraction process in steps 2 and 5 is carried out only under ultrasound, and the ultrasound time is extended to 20 minutes; all other operations and parameters are the same as in Example 1.

[0086] The results were as follows: in step 3, the scandium extraction rate was 52.63%, and in step 6, the niobium extraction rate was 42.85%.

[0087] Comparative Example 3

[0088] Compared with Example 1, the only difference is that the extraction process in steps 2 and 5 is carried out only under a magnetic field, and the magnetic field time is extended to 20 minutes; all other operations and parameters are the same as in Example 1.

[0089] The results were as follows: in step 3, the scandium extraction rate was 53.49%, and in step 6, the niobium extraction rate was 41.87%.

[0090] Comparative Example 4

[0091] Compared with Example 1, the only difference is that the extraction process in steps 2 and 5 is not carried out under a combined field of ultrasound and magnetic field. Instead, it is pre-extracted by ultrasound for 10 minutes and then extracted under magnetic field for 10 minutes. All other operations and parameters are the same as in Example 1.

[0092] The results were as follows: in step 3, the scandium extraction rate was 51.56%, and in step 6, the niobium extraction rate was 40.87%.

[0093] This invention innovatively demonstrates that the extraction performed under a combined ultrasonic-magnetic field unexpectedly adapts to the final physicochemical characteristics of niobium-scandium in phosphoric acid solution, resulting in unexpectedly excellent extraction capabilities. In particular, in a complex phosphoric acid system containing niobium and scandium, excellent scandium-niobium separation selectivity can also be obtained.

Claims

1. A method for extracting niobium and / or scandium from a phosphoric acid solution system, characterized in that, The loaded organic phase was obtained by extracting a phosphoric acid solution system containing niobium and / or scandium and the extracting organic phase under a combined ultrasonic-magnetic field.

2. The extraction method for niobium and / or scandium in a phosphoric acid solution system as described in claim 1, characterized in that, The phosphoric acid solution system is a leachate obtained by leaching materials containing niobium and / or scandium with a phosphoric acid solution; Preferably, in the phosphoric acid solution system, the concentration of phosphoric acid is 4~12 mol / L; Preferably, the phosphoric acid solution system is pretreated with acid, wherein the acid is at least one of hydrochloric acid and sulfuric acid.

3. The extraction method for niobium and / or scandium in a phosphoric acid solution system as described in claim 1, characterized in that, When the phosphoric acid solution system is a scandium-containing phosphoric acid solution, it is subjected to the aforementioned auxiliary extraction to obtain a scandium-loaded organic phase; When the phosphoric acid solution system is a niobium-containing phosphoric acid solution, it is subjected to the aforementioned auxiliary extraction to obtain a niobium-loaded organic phase; When the phosphoric acid solution system is a phosphoric acid solution containing scandium and niobium, it is first subjected to a first-stage auxiliary extraction to obtain a scandium-loaded organic phase and a niobium-containing raffinate; then the niobium-containing raffinate is subjected to a second-stage auxiliary extraction to obtain a niobium-loaded organic phase.

4. The extraction method for niobium and / or scandium in a phosphoric acid solution system as described in any one of claims 1 to 3, characterized in that, The extractant organic phase for scandium extraction comprises extractant A, which includes C6~C6. 20 Phosphate ester, C6~C 20 Tertiary carbonic acid, C2~C 10 Acylated oxime acids, C6~C 20 At least one of alkyl tertiary amines and trialkylphosphine oxides.

5. The extraction method for niobium and / or scandium in a phosphoric acid solution system as described in claim 4, characterized in that, The organic phase extracted also contains a hydrophobic diluent, wherein the content of extractant A is 2-50% vol%. Preferably, during the scandium extraction process, the O / A volume ratio is 1:5 to 3:

1. Preferably, the extraction temperature is 15℃~50℃; Preferably, the extraction time is 5 min to 20 min.

6. The extraction method for niobium and / or scandium in a phosphoric acid solution system as described in any one of claims 1 to 3, characterized in that, The extractant organic phase for niobium extraction comprises extractant B, which includes C6~C6. 20 Phosphate ester, C4~C 10 Alkyl ketones, C5~C 10 Cycloalkanes, C6~C 20 Alkylamine, C6~C 20 Alkyl alcohols, C2~C 10 At least one of the amides.

7. The extraction method for niobium and / or scandium in a phosphoric acid solution system as described in claim 6, characterized in that, The extractant B is C8~C 16 Alkyl alcohols.

8. The extraction method for niobium and / or scandium in a phosphoric acid solution system as described in claim 6, characterized in that, In the organic phase extraction, the content of extractant B is 10%~70%; Preferably, during the niobium extraction process, the O / A volume ratio is 1~3:1; Preferably, the extraction temperature is 15℃~50℃; Preferably, the extraction time is 5 min to 20 min.

9. The extraction method for niobium and / or scandium in a phosphoric acid solution system as described in any one of claims 1 to 8, characterized in that, The ultrasonic intensity is 0.1 W / cm² to 1 W / cm².

10. The extraction method for niobium and / or scandium in a phosphoric acid solution system according to any one of claims 1 to 8, characterized in that, The magnetic field strength is 500~5000 Oe.

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