Method for separating yttrium from yttrium enrichment

Abstract

The invention belongs to the field of rare earth hydrometallurgy, and particularly relates to a method for separating yttrium from yttrium enrichment, which comprises the following steps: a) mixing and reacting an organic phase to be saponified with a saponification reagent to obtain a saponified organic phase; the components of the organic phase to be saponified comprise 2-n-hexyldecanoic acid and a diluent; and b) extracting non-yttrium rare earth in the yttrium-containing rare earth water phase by using the saponified organic phase. According to the method provided by the invention, yttrium in the yttrium enrichment can be extracted and separated by utilizing a relatively short process flow, the phase separation time is short, the interface phenomenon is good, the cycling stability of an extraction system is good, recycling can be realized, and the economic benefit is greatly improved.

Description

Technical Field

[0001] The present invention belongs to the field of rare earth hydrometallurgy, and particularly relates to a method for separating yttrium from yttrium-rich substances. Background Art

[0002] Regardless of the past or the present, the importance of rare earths is self-evident. With the rapid development of technology, rare earths have been applied in various industries. From the initial fluorescent powders and fluorescent lamps to ceramics, laser instruments, catalysts, etc., and then to high-tech fields such as PET detectors, wires, gemstones, and X-ray tubes, it can be said without exaggeration that rare earths have penetrated into all aspects of our lives and play a crucial role in the military, medicine, and aerospace. However, the separation of rare earth elements has always been a very difficult task, especially for rare earths applied in high-tech fields, which require very high purity. In the market, the purity of rare earths is directly linked to their price. The higher the purity, the price increases exponentially. Therefore, it is extremely urgent to develop methods for separating and purifying high-purity rare earths.

[0003] Yttrium, due to its excellent optical, electrical, and magnetic properties, is widely used in special glasses, ceramics, catalysts, etc. As one of the most difficult rare earth elements to separate, its separation is highly favored in both industry and research. Correspondingly, many methods for separating yttrium have emerged. However, the truly reliable or practical industrial production methods are the most classic solvent extraction method, which can take on this important task. The solvent extraction method has the advantages of continuous production, large processing capacity, fast reaction speed, etc., and is widely used in the separation of various rare earth elements. When using the solvent extraction method to separate and purify yttrium, the extractant is the core. In recent years, there have been many reports on separating yttrium using the solvent extraction method. However, truly speaking, the extractants used are difficult to achieve large-scale production, that is, difficult to industrialize. Even if the extractants inside are slightly better than the traditional naphthenic acid (NA) in terms of effect, their synthesis process is relatively cumbersome and the cost is relatively high. Therefore, in such a background, it is very necessary to focus on extractants that can be industrialized or have been industrialized for separating and purifying yttrium. Summary of the Invention

[0004] In view of this, the purpose of the present invention is to provide a method for separating yttrium from yttrium-rich substances. The extraction system used in this method is easy to obtain, has good extraction effect, fast extraction time, and has good industrialization prospects.

[0005] The present invention provides a method for separating yttrium from yttrium-rich substances, including the following steps:

[0006] a) Mixing the organic phase to be saponified with a saponification reagent for reaction to obtain a saponified organic phase;

[0007] The components of the organic phase to be saponified include 2-n-hexyldecanoic acid and a diluent;

[0008] b) Using the saponified organic phase to extract non-yttrium rare earths from the yttrium-containing rare earth aqueous phase.

[0009] Preferably, the content of 2-n-hexyldecanoic acid in the organic phase to be saponified is 0.1 - 1.8 mol / L.

[0010] Preferably, the components of the organic phase to be saponified further include a phase modifier, and the phase modifier is one or more of isooctanol, isodecanol, and tributyl phosphate.

[0011] Preferably, the content of the phase modifier in the organic phase to be saponified is ≤ 30 vol%.

[0012] Preferably, the diluent is one or more of white oil, sulfonated kerosene, and C6 - C 13 hydrocarbons.

[0013] Preferably, the saponification degree of the saponified organic phase is 10 - 90%.

[0014] Preferably, the extraction method is single-stage extraction or fractional extraction.

[0015] Preferably, the specific process of the single-stage extraction includes: mixing the saponified organic phase with the yttrium-containing rare earth aqueous phase, so that the non-yttrium rare earths in the aqueous phase enter the organic phase, to obtain a loaded organic phase and a yttrium-containing raffinate.

[0016] Preferably, the following steps are further included: stripping and washing the loaded organic phase, and then returning to step a) for recycling.

[0017] Preferably, the fractional extraction includes an extraction section and a scrubbing section, and the number of extraction stages in the extraction section and the number of scrubbing stages in the scrubbing section are both obtained by calculation according to the countercurrent extraction theory.

[0018] Compared with the prior art, the present invention provides a method for separating yttrium from yttrium-rich substances, comprising the following steps: a) mixing a saponifiable organic phase with a saponification reagent for reaction to obtain a saponified organic phase; the components of the saponifiable organic phase include 2-n-hexyldecanoic acid and a diluent; b) using the saponified organic phase to extract non-yttrium rare earths from a yttrium-containing rare earth aqueous phase. The extraction system used in the present invention overcomes many disadvantages of traditional extractants. For example, naphthenic acid (NA) is a by-product of petroleum processing, with a complex composition structure, slow phase separation speed after saponification, poor fluidity, easy aging after long-term use, poor stability, and difficult treatment of waste organic phases. The secondary octylphenoxyacetic acid (CA-12) system is prone to esterification reaction with alcohol phase modifiers, and has a low separation coefficient between yttrium and heavy rare earth elements, resulting in a large number of separation stages, complex processes, and long process flows. The method provided by the present invention can extract and separate yttrium from yttrium-rich substances with a short process flow, fast phase separation time, good interfacial phenomenon, good cyclic stability of the extraction system, and can be recycled, greatly improving economic benefits. Detailed Embodiments

[0019] The technical solutions in the embodiments of the present invention will be clearly and completely described below. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all of the embodiments. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present invention without creative efforts shall fall within the protection scope of the present invention.

[0020] The present invention provides a method for separating yttrium from yttrium-rich substances, comprising the following steps:

[0021] a) Mixing a saponifiable organic phase with a saponification reagent for reaction to obtain a saponified organic phase;

[0022] b) Using the saponified organic phase to extract non-yttrium rare earths from a yttrium-containing rare earth aqueous phase, thereby realizing the separation of yttrium from non-yttrium rare earths.

[0023] In the method provided by the present invention, in step a), the components of the saponifiable organic phase include 2-n-hexyldecanoic acid and a diluent; wherein, the abbreviation of 2-n-hexyldecanoic acid is DY319, and its common name is isopalmitic acid; the diluent is preferably one or more of white oil, sulfonated kerosene, and C6-C 13 hydrocarbons, and the C6-C 13 hydrocarbons include but are not limited to n-hexane and / or cyclohexane; the content of 2-n-hexyldecanoic acid in the saponifiable organic phase is preferably 0.1-1.8 mol / L, specifically 0.1 mol / L, 0.3 mol / L, 0.5 mol / L, 0.8 mol / L, 1 mol / L, 1.3 mol / L, 1.5 mol / L, or 1.8 mol / L.

[0024] In the method provided by the present invention, in step a), the composition of the organic phase to be saponified preferably further includes a phase modifier, and the phase modifier is one or more of isooctanol, isodecanol, and tributyl phosphate (TBP); the content of the phase modifier in the organic phase to be saponified is preferably ≤ 30 vol%, and specifically can be 1 vol%, 5 vol%, 10 vol%, 15 vol%, 20 vol%, 25 vol%, or 30 vol%.

[0025] In the method provided by the present invention, in step a), the saponification reagent is preferably one or more of sodium hydroxide, potassium hydroxide, ammonia water, sodium carbonate, and ammonium carbonate.

[0026] In the method provided by the present invention, in step a), the temperature of the mixing reaction is preferably 10 - 40 °C, and specifically can be 10 °C, 15 °C, 20 °C, 25 °C (room temperature), 30 °C, 35 °C, or 40 °C; the rotation speed of the mixing reaction is preferably 100 - 500 rpm, and specifically can be 100 rpm, 150 rpm, 200 rpm, 250 rpm, 280 rpm, 300 rpm, 350 rpm, 400 rpm, 450 rpm, or 500 rpm; the time of the mixing reaction is preferably 5 - 60 min, and specifically can be 5 min, 10 min, 15 min, 20 min, 25 min, 30 min, 35 min, 40 min, 45 min, 50 min, 55 min, or 60 min.

[0027] In the method provided by the present invention, in step a), the saponification degree of the saponified organic phase is preferably 10 - 90%, and specifically can be 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, or 90%. In the present invention, "%" in the saponification degree refers to mole percentage.

[0028] In the method provided by the present invention, in step b), the yttrium-containing rare earth aqueous phase further contains ions of other rare earth elements, and the other rare earth elements include, but are not limited to, one or more of holmium (Ho), erbium (Er), thulium (Tm), ytterbium (Yb), and lutetium (Lu).

[0029] In the method provided by the present invention, in step b), the pH value of the yttrium-containing rare earth aqueous phase is preferably 3 - 5, and specifically can be 3, 3.1, 3.2, 3.3, 3.4, 3.5, 3.6, 3.7, 3.8, 3.9, 4, 4.1, 4.2, 4.3, 4.4, 4.5, 4.6, 4.7, 4.8, 4.9, or 5.

[0030] In the method provided by the present invention, in step b), the extraction method is preferably single-stage extraction or fractional extraction.

[0031] In the method provided by the present invention, in step b), the specific process of the single-stage extraction preferably includes: mixing the saponified organic phase with the yttrium-containing rare earth aqueous phase, so that the rare earths other than yttrium in the aqueous phase enter the organic phase, to obtain a loaded organic phase and a yttrium-containing raffinate. Among them, the volume ratio of the saponified organic phase to the yttrium-containing rare earth aqueous phase is preferably 1:(0.25-4), and specifically can be 1:0.25, 1:0.5, 1:0.75, 1:1, 1:1.25, 1:1.5, 1:1.75, 1:2, 1:2.25, 1:2.5, 1:2.75, 1:3, 1:3.25, 1:3.5, 1:3.75 or 1:4; the temperature of the mixing is preferably 10-40°C, and specifically can be 10°C, 15°C, 20°C, 25°C (room temperature), 30°C, 35°C or 40°C; the rotation speed of the mixing is preferably 100-500 rpm, and specifically can be 100 rpm, 150 rpm, 200 rpm, 250 rpm, 280 rpm, 300 rpm, 350 rpm, 400 rpm, 450 rpm or 500 rpm; the mixing time is preferably 5-60 min, and specifically can be 5 min, 10 min, 15 min, 20 min, 25 min, 30 min, 35 min, 40 min, 45 min, 50 min, 55 min or 60 min; after the mixing is completed, standing for phase separation is carried out to obtain a loaded organic phase and a rare earth raffinate.

[0032] In the method provided by the present invention, in step b), for the single-stage extraction scheme, it preferably further includes the following steps: stripping and water washing the loaded organic phase, and then returning to step a) for recycling.

[0033] In the method provided by the present invention, in step b), the fractional extraction preferably includes an extraction section and a scrubbing section, and the number of stages and the flow ratio are determined by the countercurrent extraction theory. The scrubbing agent used in the scrubbing section is preferably hydrochloric acid, and the concentration of the hydrochloric acid is preferably 1 to 3 mol / L, specifically 1 mol / L, 1.5 mol / L, 2 mol / L, 2.5 mol / L or 3 mol / L; the temperature of the fractional extraction is preferably 10 to 40 °C, specifically 10 °C, 15 °C, 20 °C, 25 °C (room temperature), 30 °C, 35 °C or 40 °C; the oscillation rate of the fractional extraction is preferably 200 to 300 rpm, specifically 200 rpm, 210 rpm, 220 rpm, 230 rpm, 240 rpm, 250 rpm, 260 rpm, 270 rpm, 280 rpm, 290 rpm or 300 rpm; the oscillation time of the fractional extraction is preferably 5 to 60 min, specifically 5 min, 10 min, 15 min, 20 min, 25 min, 30 min, 35 min, 40 min, 45 min, 50 min, 55 min or 60 min; after the oscillation is completed, it is allowed to stand for phase separation to obtain the feed liquid after fractional extraction.

[0034] The extraction system used in the method provided by the present invention overcomes many disadvantages of traditional extractants. For example, naphthenic acid (NA) is a by-product of petroleum processing, with a complex composition and structure. After saponification, the phase separation speed is slow, the fluidity is poor, it is easy to age after long-term use, the stability is poor, and the treatment of waste organic phase is difficult. The 2-ethylhexyl phenylphosphonic acid mono-2-ethylhexyl ester (CA-12) system is prone to esterification reaction with alcohol phase modifiers, and the separation coefficient between yttrium and heavy rare earth elements is low, resulting in a large number of separation stages, complex process and long process flow. The method provided by the present invention can extract and separate yttrium in yttrium concentrate by using a shorter process flow, with fast phase separation time, good interfacial phenomenon, good cyclic stability of the extraction system, and can be recycled, greatly improving the economic benefits.

[0035] For the sake of clarity, the following will be described in detail through the following examples and comparative examples.

[0036] Example 1

[0037] 1. Prepare the organic phase: Dilute 2-n-hexyldecanoic acid with white oil to 0.45 mol / L, and add 20 vol% of isooctanol as a phase modifier.

[0038] 2. Saponify the organic phase: Take 20 mL of the above organic phase, add a certain volume of 6 mol / L sodium hydroxide solution, and oscillate at room temperature and 280 rpm for 20 min to make the saponification degree reach 80% to obtain the saponified organic phase.

[0039] 3. Extraction: In this example, single-stage extraction is used. The aqueous phase is a mixed solution of chlorides of 15 rare earth elements (excluding scandium and promethium), with the same concentration for each rare earth element and a total rare earth element concentration of 0.1764 mol / L, and pH = 4. The above saponified organic phase and the aqueous phase are mixed at a volume ratio of organic phase:aqueous phase = 1:1, oscillated for 20 min at room temperature and 280 rpm, and then allowed to stand for phase separation to obtain the loaded organic phase and the raffinate.

[0040] Comparative Example 1

[0041] Replace 2-n-hexyldecanoic acid in Example 1 with CA-12 and NA respectively, and keep other conditions unchanged for the same treatment. The separation coefficients between yttrium and heavy rare earth elements can be obtained as shown in the following table.

[0042] <![CDATA[β Ln / Y > 2-n-Hexyldecanoic acid CA-12 NA Ho / Y 2.37 1.79 2.14 Er / Y 2.46 1.33 2.01 Tm / Y 3.05 1.30 2.48 Yb / Y 4.05 1.28 3.14 Lu / Y 4.12 1.14 3.18

[0043] It can be found from the table that the separation coefficient of 2-n-hexyldecanoic acid for Y and heavy rare earth elements is larger than that of NA and CA-12, and better separation effect can be achieved.

[0044] Example 2

[0045] 1. Preparation of organic phase: Dilute 2-n-hexyldecanoic acid with white oil to 0.6 mol / L and add 20 vol% of isooctanol as a phase modifier.

[0046] 2. Saponification of organic phase: Take 20 mL of the above organic phase, add a certain volume of 6 mol / L sodium hydroxide solution, oscillate for 20 min at room temperature and 280 rpm to make its saponification degree reach 60% to obtain the saponified organic phase.

[0047] 3. Extraction: In this example, single-stage extraction is used. The aqueous phase is a mixed solution of chlorides of 15 rare earth elements (excluding scandium and promethium), with the same concentration for each rare earth element and a total rare earth element concentration of 0.1764 mol / L, and pH = 4. The above saponified organic phase and the aqueous phase are mixed at a volume ratio of organic phase:aqueous phase = 1:1, oscillated for 20 min at room temperature and 280 rpm, and then allowed to stand for phase separation to obtain the loaded organic phase and the raffinate. The extraction rate of Y is 52.66%.

[0048] Comparative Example 2

[0049] Referring to Example 2, the difference is that no sodium hydroxide is added for saponification in step 2, that is, the saponification degree is 0%. As a result, the extraction rate of Y is less than 5%. If the saponification degree is increased to 80%, the extraction rate of Y can reach 85.81%.

[0050] Comparative Example 3

[0051] Referring to Example 2, the difference is that no isooctanol is added in step 1. As a result, the extraction rate of Y is 51.97%.

[0052] Comparative Example 4

[0053] Referring to Example 2, the difference is that isooctanol is not added in the first step, and the saponification degree in the second step is increased to 65%, 70%, and 80%. The results show that emulsification occurs at the phase interface after standing phase separation, and the degree of emulsification increases with the increase of the saponification degree.

[0054] Example 3

[0055] 1. Prepare the organic phase: Dilute 2-n-hexyldecanoic acid with white oil to 0.75 mol / L, and add 20 vol% of isooctanol as a phase modifier.

[0056] 2. Saponify the organic phase: Take 20 mL of the above organic phase, add a certain volume of 6 mol / L sodium hydroxide solution, and shake it at room temperature and 280 rpm for 20 min to make the saponification degree reach 80% to obtain the saponified organic phase.

[0057] 3. Extraction: In this example, single-stage extraction is used. The aqueous phase is a feed solution with a YCl3 concentration of 0.24 mol / L and pH = 4; mix the above saponified organic phase and the aqueous phase according to a volume ratio of organic phase:aqueous phase = 1:1, shake it at room temperature and 280 rpm for 20 min, and stand for phase separation to obtain the loaded organic phase and the raffinate. The loaded organic phase contains 0.1695 mol / L of Y.

[0058] 4. Recycling and regeneration of the extractant: First, strip the loaded organic phase with acid, then wash it with deionized water until it is weakly acidic, repeat the steps of saponification, extraction, stripping, and deionized water washing, and measure the concentration of 2-n-hexyldecanoic acid in the organic phase after each cycle. In ten cycles, the concentration of 2-n-hexyldecanoic acid fluctuates around 0.75 mol / L, indicating that 2-n-hexyldecanoic acid has good recycling stability.

[0059] Comparative Example 5

[0060] Referring to Example 3, the difference is that 2-n-hexyldecanoic acid in the first step is replaced with NA, and the others remain unchanged. As a result, the loaded organic phase contains 0.1726 mol / L of Y, indicating that the loading capacities of 2-n-hexyldecanoic acid and NA are comparable.

[0061] Example 4

[0062] 1. Prepare the organic phase: Dilute 2-n-hexyldecanoic acid with white oil to 0.75 mol / L, and add 20 vol% of isooctanol as a phase modifier.

[0063] 2. Saponified organic phase: Take a certain volume of the above-mentioned organic phase, add a certain volume of 6 mol / L sodium hydroxide solution, and shake it at room temperature and 280 rpm for 20 min to make the saponification degree reach 80%, obtaining the saponified organic phase.

[0064] 3. Extraction: In this example, fractional extraction is used. The aqueous phase is the feed solution of high-yttrium enriched material (holmium-erbium-thulium-ytterbium-lutetium-yttrium enriched material) dissolved in hydrochloric acid, the total concentration of rare earth elements is 1.0 mol / L, and pH = 4. The fractional extraction process consists of 16 extraction stages and 4 washing stages. The saponified organic phase is fed into the first stage, the feed solution is fed into the 16th stage, and the acid for washing is fed into the 20th stage. The acid for washing is 3 mol / L hydrochloric acid, and the volume flow ratio is organic phase:feed solution:acid for washing = 8.8:1:1.4. After shaking at room temperature and 280 rpm for 20 min, it is allowed to stand for phase separation.

[0065] The compositions of the feed solution before fractional extraction and the product after fractional extraction are shown in the following table (unit: mass fraction, wt%) in terms of the oxides corresponding to each rare earth element. It should be noted that the rare earth elements in the feed solution and the product do not exist in the form of oxides, but in the form of ions. The following table is only converted to the oxide content for the convenience of calculation.

[0066] Composition <![CDATA[La2O3~D y2 O3]]> <![CDATA[Ho2O3]]> <![CDATA[Er2O3]]> <![CDATA[Tm2O3]]> <![CDATA[Yb2O3]]> <![CDATA[Lu2O3]]> <![CDATA[Y2O3]]> Feed solution <0.19 4.33 7.8 0.81 3.60 0.53 >82.74 Product <0.0033 0.0121 0.0048 <0.003 <0.003 <0.003 >99.971

[0067] As shown in the table, after fractional extraction, the purity of Y2O3 increased from 82.74 wt% to 99.97 wt%, realizing the separation and purification of Y from the high-yttrium enriched material.

[0068] Example 5

[0069] 1. Preparation of organic phase: Dilute 2-n-hexyldecanoic acid with white oil to 0.75 mol / L, and add 20 vol% isooctanol as a phase modifier.

[0070] 2. Saponified organic phase: Take a certain volume of the above-mentioned organic phase, add a certain volume of 6 mol / L sodium hydroxide solution, and shake it at room temperature and 280 rpm for 20 min to make the saponification degree reach 80%, obtaining the saponified organic phase.

[0071] 3. Extraction: In this example, fractional extraction is used. The aqueous phase is the feed solution of high-yttrium enriched material (holmium-erbium-yttrium enriched material) dissolved in hydrochloric acid, the total concentration of rare earth elements is 1.0 mol / L, and pH = 4. The fractional extraction process consists of 16 extraction stages and 6 washing stages. The saponified organic phase is fed into the first stage, the feed solution is fed into the 16th stage, and the acid for washing is fed into the 22nd stage. The acid for washing is 3 mol / L hydrochloric acid. The volume flow ratio is organic phase:feed solution:acid for washing = 7.95:1:1.36. After shaking at room temperature and 280 rpm for 20 min, it is allowed to stand for phase separation.

[0072] The compositions of the feed solution before fractional extraction and the product after fractional extraction are shown in the following table (unit: mass fraction, wt%). It should be noted that the rare earth elements in the feed solution and the product do not exist in the form of oxides, but in the form of ions. In the following table, the contents are converted to oxide contents only for the convenience of calculation.

[0073] Composition <![CDATA[Ho2O3]]> <![CDATA[Er2O3]]> <![CDATA[Y2O3]]> Feed solution 2.39 7.61 90.00 Product <0.021 0.0198 >99.959

[0074] As shown in the table, after fractional extraction, the purity of Y2O3 increased from 90.00 wt% to 99.96 wt%, realizing the separation and purification of Y from the high-yttrium concentrate.

[0075] Example 6

[0076] 1. Prepare the organic phase: Dilute 2-n-hexyldecanoic acid with white oil to 0.75 mol / L, and add 20 vol% of isooctanol as a phase modifier.

[0077] 2. Saponify the organic phase: Take a certain volume of the above organic phase, add a certain volume of 6 mol / L sodium hydroxide solution, and oscillate at room temperature and 280 rpm for 20 min to make the saponification degree reach 80% to obtain the saponified organic phase.

[0078] 3. Extraction: In this example, fractional extraction is used. The aqueous phase is a yttrium-containing feed solution with a purity of 99.9 wt%, the total concentration of rare earth elements is 1.0 mol / L, and pH = 4; the fractional extraction process consists of 20 extraction stages and 10 washing stages. The saponified organic phase is fed into the first stage, the feed solution is fed into the 20th stage, and the acid wash is fed into the 30th stage; the acid wash is 3 mol / L hydrochloric acid; the volume flow ratio is organic phase:feed solution:acid wash = 8.00:1:1.47; after oscillating at room temperature and 280 rpm for 20 min, let it stand for phase separation.

[0079] After fractional extraction, the purity of yttrium can reach 99.999 wt%.

[0080] The above are only the preferred embodiments of the present invention. It should be pointed out that for those of ordinary skill in the art, without departing from the principle of the present invention, several improvements and refinements can be made, and these improvements and refinements should also be regarded as the protection scope of the present invention.

Claims

1. A method for separating yttrium from yttrium-enriched materials, characterized in that: The following steps are involved: a) mixing the organic phase to be saponified with a saponifying agent to react to obtain a saponified organic phase; The components of the organic phase to be saponified include 2-n-hexyldecanoic acid and a diluent; b) using the saponified organic phase to extract non-yttrium rare earth in the yttrium rare earth-containing aqueous phase.

2. The method according to claim 1, characterized in that The content of the 2-n-hexyldecanoic acid in the organic phase to be saponified is 0.1-1.8 mol / L.

3. The method according to claim 1, characterized in that The components of the organic phase to be saponified also include a phase modifier, and the phase modifier is one or more of isooctyl alcohol, isodecanol and tributyl phosphate.

4. The method according to claim 3, characterized in that The content of the phase modifier in the organic phase to be saponified is ≤30 vol%.

5. The method according to claim 1, characterized in that The diluent is white oil, sulfonated kerosene and C6~C 13 One or more hydrocarbons.

6. The method according to claim 1, characterized in that The saponification degree of the saponified organic phase is 10 to 90%.

7. The method according to claim 1, characterized in that The extraction method is single-stage extraction or fractional extraction.

8. The method according to claim 7, characterized in that The specific process of the single-stage extraction comprises: The saponified organic phase is mixed with the yttrium rare earth-containing aqueous phase, so that the non-yttrium rare earth in the aqueous phase enters the organic phase, thereby obtaining a loaded organic phase and a yttrium-containing raffinate.

9. The method according to claim 8, characterized in that The following steps are also included: The loaded organic phase is stripped and washed with water, and then returned to step a) for recycling.

10. The method according to claim 7, characterized in that The fractional extraction comprises an extraction section and a washing section, and the extraction stages of the extraction section and the washing stages of the washing section are calculated by cascade extraction theory.