CN109207724B - Extraction solvent and extraction method for simultaneously extracting and separating vanadium and chromium from vanadium and chromium-containing solution - Google Patents
Extraction solvent and extraction method for simultaneously extracting and separating vanadium and chromium from vanadium and chromium-containing solution Download PDFInfo
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- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
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- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
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- C22B34/00—Obtaining refractory metals
- C22B34/20—Obtaining niobium, tantalum or vanadium
- C22B34/22—Obtaining vanadium
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- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B34/00—Obtaining refractory metals
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- C22B34/32—Obtaining chromium
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Abstract
The invention relates to the technical field of hydrometallurgy, in particular to an extraction solvent and an extraction method for simultaneously extracting and separating vanadium and chromium from a vanadium and chromium-containing solution, which are characterized in that the extraction solvent is formed by mixing an extraction agent and a diluent, the extraction agent is water-soluble amide with the solubility lower than 0.5g/L, the diluent is an inert organic solvent, the extraction agent is one or more of N-alkylamide, N, N, N-tetraalkyl diamide or low-water-soluble amide containing a plurality of amide groups and the like, the diluent is one or more of sulfonated kerosene, white oil, halogenated hydrocarbon compounds and other inert organic solvents which are liquid at normal temperature, and the high-purity vanadium solution or vanadium-containing precipitate and chromium-containing solution is obtained by the process steps of preparing the extraction solvent, extracting, washing, back extracting chromium and back extracting vanadium, and has simple process, Strong extraction capacity, fast balance, good separation selectivity, easy back extraction, economy, environmental protection and the like.
Description
Technical Field
The invention relates to the technical field of hydrometallurgy, in particular to an extraction solvent and an extraction method for simultaneously extracting and separating vanadium and chromium from a vanadium and chromium-containing solution, which have the advantages of simple process, strong extraction capacity, fast balance, good selectivity, easy back extraction and separation, economy and environmental protection.
Background
It is well known that vanadium and chromium are important strategic resources, which are widely used in various industries. However, the properties of vanadium and chromium are very similar, and the vanadium and chromium are generally symbiotic in vanadium-titanium magnetite, and the separation and purification of vanadium and chromium in the water leaching solution of roasted vanadium-chromium slag is a problem which is difficult to solve at present.
In order to solve the above problems, patent publication No. CN1073414 discloses a chemical method for treating waste liquid of vanadium and chromium, which comprises the steps of firstly forming a precipitate from a weak acidic solution of ferric chloride and pentavalent vanadium, and then extracting chromium from the precipitate by using sulfuric acid and ammonium sulfate, but the process avoids simultaneous precipitation of vanadium and chromium, and only has a good effect on low-concentration vanadium and chromium liquid. Chinese patent CN101121962A discloses a method for separating vanadium and chromium by extracting primary and secondary compound amines, which has good effect on separating vanadium and chromium, but has complex process and more energy consumption. Chinese patent CN102127654 adopts a hypofused salt method to extract vanadium and chromium, and sodium vanadate and sodium chromate are obtained by fractional crystallization.
Disclosure of Invention
The invention aims to solve the defects of the prior art and provide the method for simultaneously extracting and separating vanadium and chromium from the vanadium and chromium-containing solution, which has the advantages of simple process, strong extraction capability, quick balance, good selectivity, easy back extraction and separation, economy and environmental protection.
The technical scheme adopted by the invention for solving the technical problems is as follows:
an extraction solvent for simultaneously extracting and separating vanadium and chromium from a vanadium and chromium-containing solution is characterized in that the extraction solvent is formed by mixing an extraction agent and a diluent, wherein the extraction agent is a water-soluble amide with the solubility of less than 0.5g/L, and the diluent is an inert organic solvent.
The extracting agent is one or more of N-alkyl amide and N, N, N, N-tetraalkyl diamide or water-soluble amide containing a plurality of amide groups and having the solubility of less than 0.5g/L, and the diluent is one or more of sulfonated kerosene, white oil and inert organic solvent of halogenated hydrocarbon compounds which are liquid at normal temperature.
When one of the extracting agent and the diluent is solid at 25 ℃ or both are solid at 25 ℃, the mass ratio of the extracting agent in the extracting solvent is 2-100%, the mass ratio of the diluent is 0-98%, and when both the extracting agent and the diluent are liquid at 25 ℃; the volume of the extracting agent in the extracting solvent accounts for 5-100%, and the volume of the diluent accounts for 0-95%.
In the N-alkyl amide, the N, N, N-tetraalkyl diamide or the water-soluble amide containing a plurality of amide groups and having a solubility of less than 0.5g/L, the number of carbon atoms of the alkyl group in the acyl group is 1 to 18, and the acyl group may be a straight-chain alkyl group or a branched-chain alkyl group.
The number of carbon atoms in an alkyl directly connected with a nitrogen atom in the N-alkylamide is 1-18, two alkyls directly connected with the nitrogen atom in the N, N, N, N-tetraalkyldiamide are the same alkyl or different alkyls, the number of carbon atoms in the two alkyls directly connected with the nitrogen atom is 1-18 respectively, and the two alkyls can be a straight-chain alkyl or a branched-chain alkyl.
The carbon number of the sulfonated kerosene is 11-17, the type of the white oil is 1-7, and the halogenated hydrocarbon compound which is liquid at normal temperature is one or more of inert organic solvents of chlorohydrocarbon, bromohydrocarbon or iodohydrocarbon.
A method for simultaneously extracting and separating vanadium and chromium from a vanadium and chromium-containing solution is characterized by comprising the following process steps:
(1) preparing an extraction solvent: the extraction solvent is formed by mixing an extraction agent and a diluent, wherein the extraction agent is water-soluble amide with the solubility lower than 0.5g/L, the diluent is an inert organic solvent, and the extraction solvent is prepared by mixing the extraction agent and the diluent to be an organic phase;
(2) extraction: extracting the vanadium-chromium-containing solution by using the extraction solvent in the step (1), wherein the pH of the vanadium-chromium-containing solution is 1.3-10, the extraction temperature is 10-90 ℃, the extraction time is 1-10 min compared with the time when the O/A = 0.4-4.0, the extraction mode is countercurrent extraction, fractional extraction or cross-flow extraction, and the extraction stage number is 1-35, so as to obtain a loaded organic phase;
(3) washing: washing the loaded organic phase obtained in the step (2) with a solution, wherein the pH of the solution is 1.2-9.0, the temperature is 10-90 ℃, and the time is 1-10 min compared with the time that O/A = 0.4-40, so as to obtain a washed organic phase;
(4) stripping chromium: taking the washed organic phase obtained in the alkaline solution back-extraction step (3), extracting at the temperature of 10-60 ℃ for 1-8 min compared with the time of 1-20O/A, wherein the pH of the alkaline solution is 7.2-10.0, the back-extraction mode is countercurrent extraction or cross-flow extraction, and the extraction stages are 1-10 stages, so as to obtain high-purity chromium solution and the vanadium-loaded organic phase;
(5) stripping vanadium: and (3) carrying out back extraction on the vanadium-loaded organic phase obtained in the step (4) by using an alkaline solution, wherein the extraction temperature is 10-60 ℃, the extraction time is 1-10 min compared with the time of O/A = 1-10, the pH of the alkaline solution is 7.5-13.5, the back extraction mode is countercurrent extraction or cross-flow extraction, and the extraction stage number is 1-10, so that the high-purity vanadium liquid is obtained.
The vanadium-chromium-containing solution comprises a vanadium titano-magnetite smelting waste residue leaching solution and a mixed solution of two or more than two vanadium-or chromium-containing polymetallic sulfuric acid media, wherein the solution contains vanadium and chromium at the same time or only contains vanadium or chromium; the valence of vanadium is tetravalent or pentavalent, or a mixture of tetravalent and pentavalent vanadium; the valence state of chromium is trivalent or hexavalent, or a mixture of trivalent and hexavalent.
In the step (4) and the step (5), the alkaline substance is one or a mixture of ammonia water, sodium hydroxide, potassium hydroxide, calcium hydroxide, sodium carbonate, ammonium carbonate, potassium carbonate, ammonium chloride and ammonium sulfate.
The solution in the step (3) is an acidic solution, and the acidic solution comprises inorganic acid which is not easy to oxidize, such as sulfuric acid or nitric acid, or one or two mixtures containing the inorganic acid.
The extraction solvent is formed by mixing an extraction agent and a diluent, wherein the extraction agent is water-soluble amide with the solubility lower than 0.5g/L, the diluent is an inert organic solvent, the extraction agent is one or more of N-alkyl amide and N, N, N, N-tetraalkyl diamide with the solubility lower than 0.5g/L, and the diluent is one or more of inert organic solvents such as sulfonated kerosene, white oil, halogenated hydrocarbon compounds which are liquid at normal temperature and the like; an organic phase washing procedure is added, so that other impurities possibly contained in the loaded organic phase are effectively removed; the organic phase can be regenerated circularly, is beneficial to reducing the cost by carrying out extraction reaction for many times, and has the advantages of simple process, strong extraction capability, quick balance, good selectivity, easy back extraction and separation, economy, environmental protection and the like.
Detailed Description
An extraction solvent for simultaneously extracting and separating vanadium and chromium from a vanadium and chromium-containing solution, which is characterized in that the extraction solvent is formed by mixing an extraction agent and a diluent, wherein the extraction agent is a water-soluble amide with the solubility lower than 0.5g/L, the diluent is an inert organic solvent, the extraction agent is one or more of N-alkyl amide and water-soluble amide with the solubility lower than 0.5g/L of N, N, N, N-tetraalkyl diamide, preferably the mono-substituted amide, wherein the number of carbon atoms in an alkyl R is 6-10, preferably the di-substituted amide, wherein two alkyl Rs can be the same or different; the carbon number of the alkyl R is 6-10, the diluent is one or more of inert organic solvents such as sulfonated kerosene, white oil and halogenated hydrocarbon compounds which are liquid at normal temperature, when one of the extracting agent and the diluent is solid at 25 ℃ or both of the extracting agent and the diluent are solid at 25 ℃, the mass ratio of the extracting agent in the extracting solvent is 2-100%, the mass ratio of the diluent is 0-98%, and when both the extracting agent and the diluent are liquid at 25 ℃; the volume of the extracting agent in the extracting solvent is 5-100%, the volume of the diluting agent is 0-95%, the solubility of the N-alkylamide and the N, N, N, N-tetraalkyl diamide is lower than 0.5g/L, the carbon atom number of the alkyl in the acyl is 1-18, the alkyl can be straight chain alkyl or branched chain alkyl, the carbon atom number of the alkyl directly connected with the nitrogen atom in the N-alkylamide is 1-18, the alkyl can be straight chain alkyl or branched chain alkyl, the two alkyl directly connected with the nitrogen atom in the N, N, N, N-tetraalkyl diamide are the same alkyl or different alkyls, the carbon atom number of the two alkyl directly connected with the nitrogen atom is 1-18 respectively, the two alkyl can be straight chain alkyl or branched chain alkyl, and the carbon number of the sulfonated kerosene is 11-17, the white oil is 1# to 7#, the halogenated hydrocarbon compound which is liquid at normal temperature is one or more of inert organic solvents such as chlorohydrocarbon, bromohydrocarbon or iodohydrocarbon, and the extraction separation method comprises the following process steps: (1) preparing an extraction solvent: the extraction solvent is formed by mixing an extraction agent and a diluent, wherein the extraction agent is water-soluble amide with the solubility lower than 0.5g/L, the diluent is an inert organic solvent, and the extraction solvent is prepared by mixing the extraction agent and the diluent to be an organic phase; (2) extraction: extracting a vanadium-chromium-containing solution by using the extraction solvent in the step (1), preferably an acidic solution, wherein the pH of the vanadium-chromium-containing solution is 1.3-5, the extraction temperature is 10-70 ℃, the time is 1-8 min compared with the time when the O/A = 0.4-3, so as to obtain a loaded organic phase, the extraction mode is countercurrent extraction, fractional extraction or cross-flow extraction, and the extraction stage number is 1-10, so as to obtain the loaded organic phase; (3) washing: washing the loaded organic phase obtained in the step (2) with an acidic solution, wherein the pH of the acidic solution is 1.2-5, the temperature is 10-70 ℃, and the time is 1-8 min compared with the time that O/A = 0.4-2, so as to obtain a washed organic phase; (4) stripping chromium: taking the washed organic phase obtained in the alkaline solution back-extraction step (3), extracting at the temperature of 10-60 ℃ for 1-8 min compared with the time of O/A = 1-15, wherein the pH of the alkaline solution is 7.2-9.0, the back-extraction mode is countercurrent extraction or cross-flow extraction, and the number of extraction stages is 1-10, so as to obtain high-purity chromium solution and the vanadium-loaded organic phase; (5) stripping vanadium: extracting the vanadium-loaded organic phase obtained in the step (4) with an alkaline solution at 10-60 ℃ for 1-10 min compared with O/A = 1-8, wherein the pH of the alkaline solution is 7.5-13.5, the back extraction mode is countercurrent extraction or cross-flow extraction, and the extraction stage number is 1-10, so as to obtain a high-purity vanadium solution, and the vanadium-chromium-containing solution comprises a vanadium-titanium magnetite smelting waste residue leachate and a mixed solution of two or more vanadium-or chromium-containing polymetallic sulfuric acid media, wherein the solution contains vanadium and chromium at the same time or only contains vanadium or chromium; the valence of vanadium is tetravalent or pentavalent, or a mixture of tetravalent and pentavalent vanadium; the valence state of the chromium is trivalent or hexavalent or a mixture of trivalent and hexavalent, the alkaline substance in the step (4) and the step (5) is one or a mixture of more of ammonia water, sodium hydroxide, potassium hydroxide, calcium hydroxide, sodium carbonate, ammonium carbonate, potassium carbonate, ammonium chloride and ammonium sulfate, and the acidic solution in the step (3) comprises inorganic acid which is not easy to oxidize, such as sulfuric acid or nitric acid, or one or a mixture of two of the inorganic acid.
The N-alkylamides (structural formula) are as follows:
the N, N, N, N-tetraalkyldiamide (structural formula) is as follows:
the N, N, N, N-tetraalkylbisamides have the following formal structural formula:
example 1
(1) Preparing an extraction solvent: the weight percentage is 10 percent
+90% of sulfonated kerosene is mixed to prepare an extraction solvent as an organic phase;
(2) extraction: taking the extraction solvent in the step (1), performing 4-stage countercurrent extraction on the vanadium-chromium slag leachate subjected to sodium salt roasting and with the pH value of 1.9, wherein the temperature is 60 ℃, and the time is 1 min compared with the time when the O/A =0.4, so as to obtain a loaded organic phase;
(3) washing: washing the loaded organic phase of step (2) with a sulfuric acid solution at a pH of 1.4, a temperature of 60 ℃, for 5 min compared to O/a =3, to obtain a washed organic phase;
(4) stripping chromium: carrying out 8-stage cross-flow back extraction on the organic phase in the step (3) by using an ammonia water solution with the pH of 7.5 at the temperature of 40 ℃, and obtaining a chromium solution with the purity of 99.25% and an organic phase loaded with vanadium, wherein the time is 6 min compared with that of O/A = 2;
(5) stripping vanadium: and (3) carrying out 9-stage countercurrent stripping on the vanadium-loaded organic phase in the step (4) by using an ammonia water solution with the pH of 12.5, wherein the temperature is 30 ℃, the phase ratio of O/A =2, and the time is 8min, so that a vanadium solution with the purity of 99.87% is obtained.
Example 2
(1) Preparing an extraction solvent: the mass percentage is 20 percent
+80% of sulfonated kerosene is mixed to prepare an extraction solvent as an organic phase;
(2) extraction: taking the extraction solvent in the step (1), performing 3-stage countercurrent extraction on the sodium-treated roasted vanadium-chromium slag leaching solution with the pH of 1.7 at the temperature of 50 ℃, and obtaining a loaded organic phase in 3min compared with the condition that O/A = 0.5;
(3) washing: washing the organic phase of step (2) with a sulfuric acid solution at a pH of 1.6 and a temperature of 40 ℃ for 1 min compared to O/a =2 to obtain a washed organic phase;
(4) stripping chromium: carrying out 7-stage cross-flow back extraction on the organic phase in the step (3) by using an ammonia water solution with the pH of 7.7 at the temperature of 20 ℃, and obtaining a chromium solution with the purity of 99.37% and an organic phase loaded with vanadium, wherein the time is 4 min compared with that of O/A = 1;
(5) stripping vanadium: and (3) carrying out 7-stage counter-current back extraction on the organic phase in the step (4) by using an ammonia water solution with the pH of 12.9 at the temperature of 20 ℃ for 9 min compared with the O/A =5 to obtain a vanadium solution with the purity of 99.82%.
Example 3
(1) Preparing an extraction solvent: the weight percentage is 30 percent
+70% of No. 3 white oil is mixed to prepare an extraction solvent as an organic phase;
(2) extraction: taking the extraction solvent in the step (1), carrying out 3-level countercurrent extraction on calcified burnt vanadium-chromium slag with acidity of 1.6 at 40 ℃, comparing with O/A =0.7, and carrying out 1 min to obtain a loaded organic phase;
(3) washing: washing the organic phase of step (2) with a sulfuric acid solution at a pH of 1.5 and a temperature of 30 ℃ for 4 min compared to O/a =1 to obtain a washed organic phase;
(4) stripping chromium: performing 7-stage counter-current back extraction on the organic phase in the step (3) by using an ammonia water solution with the pH of 7.9 at the temperature of 30 ℃ for 8min compared with the O/A =4 to obtain a chromium solution with the purity of 99.41% and an organic phase loaded with vanadium;
(5) stripping vanadium: and (3) carrying out 8-stage counter-current back extraction on the organic phase in the step (4) by using an ammonia water solution with the pH of 12.7 at the temperature of 50 ℃ for 5 min compared with the O/A =4 to obtain a vanadium solution with the purity of 99.79%.
Example 4
(1) Preparing an extraction solvent: the mass ratio is 40%
+60% of No. 5 white oil is mixed to prepare an extraction solvent as an organic phase;
(2) extraction: taking the extraction solvent in the step (1), carrying out 2-stage cross-flow extraction on the calcified burnt vanadium-chromium slag leaching solution with the pH of 1.5 at the temperature of 30 ℃, comparing with O/A =1, and carrying out the extraction for 3min to obtain a loaded organic phase;
(3) washing: washing the organic phase of step (1) with a sulfuric acid solution at a pH of 1.8 and a temperature of 50 ℃ for 2min compared to O/a =4 to obtain a washed organic phase;
(4) stripping chromium: 5-stage cross-flow back extraction of the organic phase in the step (2) by using an ammonia water solution with the pH of 8.0 at the temperature of 10 ℃, wherein the time is 7 min compared with the time when the O/A =5, so that a chromium solution with the purity of 99.19% and an organic phase loaded with vanadium are obtained;
(5) stripping vanadium: and (3) carrying out 5-stage countercurrent back extraction on the organic phase in the step (3) by using an ammonia water solution with the pH of 13.0 at the temperature of 10 ℃, comparing with O/A =6, and carrying out 2min to obtain a vanadium solution with the purity of 99.90%.
Example 5
(1) Preparing an extraction solvent: the weight percentage is 50 percent
+50% of chloro-heptane to prepare an extraction solvent as an organic phase;
(2) extraction: taking the extraction solvent in the step (1), carrying out 1-stage cross-flow extraction on the calcified roasted vanadium-chromium slag leaching solution with the pH value of 1.4 at the temperature of 20 ℃, and obtaining a loaded organic phase in 4 min in comparison with the condition that O/A = 1.1;
(3) washing: washing the organic phase of step (2) with a sulfuric acid solution at a pH of 1.7 and a temperature of 10 ℃ for 4 min compared to O/a =2.5 to obtain a washed organic phase;
(4) stripping chromium: performing 4-stage countercurrent back extraction on the organic phase in the step (3) by using an ammonia water solution with the pH of 8.3 at the temperature of 60 ℃ for 2min compared with the O/A =3 to obtain a chromium solution with the purity of 99.35% and an organic phase loaded with vanadium;
(5) stripping vanadium: and (3) carrying out 3-stage counter-current stripping on the organic phase in the step (4) by using an ammonia water solution with the pH value of 13.1, wherein the temperature is 40 ℃, the phase ratio of O/A =1, and the time is 7 min, so that a vanadium solution with the purity of 99.83% is obtained.
Example 6
(1) Preparing an extraction solvent: the weight percentage is 60 percent
+40% of bromohexane is mixed to prepare an extraction solvent as an organic phase;
(2) extraction: taking the extraction solvent in the step (1), performing 1-stage countercurrent extraction on the vanadium-chromium mixed acidic solution with acidity of 1.3, wherein the temperature is 10 ℃, and the time is 5 min compared with the time with O/A =1.2 to obtain a loaded organic phase;
(3) washing: washing the organic phase of step (2) with a sulfuric acid solution at a pH of 1.6 and a temperature of 35 ℃ for 3min compared to O/a =3.5 to obtain a washed organic phase;
(4) stripping chromium: 2-stage countercurrent back extraction of the organic phase in the step (3) by using an ammonia water solution with the pH of 8.5 at the temperature of 55 ℃ for 5 min compared with the O/A =2.5 to obtain a chromium solution with the purity of 99.36% and an organic phase loaded with vanadium;
(5) stripping vanadium: and (3) carrying out 2-stage countercurrent back extraction on the organic phase in the step (4) by using an ammonia water solution with the pH of 13.2 at the temperature of 55 ℃, comparing with the O/A =6 for 3min, and obtaining a vanadium solution with the purity of 99.91%.
Example 7
(1) Preparing an extraction solvent: the mass percentage is 20 percent
+80% of sulfonated kerosene is mixed to prepare an extraction solvent as an organic phase;
(2) extraction: taking the extraction solvent in the step (1), performing 3-stage countercurrent extraction on the mixed acid solution of vanadium and chromium with acidity of 1.6, wherein the temperature is 30 ℃, and the time is 6 min compared with the time with O/A =1.8 to obtain a loaded organic phase;
(3) washing: washing the organic phase of step (2) with a sulfuric acid solution at a pH of 1.5 and a temperature of 55 ℃, for 6 min compared to O/a =3.0, to obtain a washed organic phase;
(4) stripping chromium: 2-stage countercurrent back extraction of the organic phase in the step (3) by using an ammonia water solution with the pH of 8.0 at the temperature of 45 ℃ for 6 min compared with the O/A =2.0 to obtain a chromium solution with the purity of 99.46% and an organic phase loaded with vanadium;
(5) stripping vanadium: and (3) carrying out 4-stage countercurrent back extraction on the organic phase in the step (4) by using an ammonia water solution with the pH of 13.0, wherein the temperature is 45 ℃, the phase ratio of O/A =5, and the time is 4 min, so that a vanadium solution with the purity of 99.93% is obtained.
Example 8
(1) Preparing an extraction solvent: the weight percentage is 30 percent
+70% of No. 4 white oil is mixed to prepare an extraction solvent as an organic phase;
(2) extraction: taking the extraction solvent in the step (1), carrying out 4-stage countercurrent extraction on the vanadium-chromium mixed acidic solution with acidity PH of 1.9, wherein the temperature is 40 ℃, and the time is 2min compared with O/A =1.8 to obtain a loaded organic phase;
(3) washing: washing the organic phase of step (2) with a sulfuric acid solution at a pH of 1.5 and a temperature of 40 ℃ for 3min compared to O/a =2.5 to obtain a washed organic phase;
(4) stripping chromium: 2-stage countercurrent back extraction of the organic phase in the step (3) by using an ammonia water solution with the pH of 8.0 at the temperature of 35 ℃ for 2min compared with the O/A =3.0 to obtain a chromium solution with the purity of 99.46% and an organic phase loaded with vanadium;
(5) stripping vanadium: and (3) carrying out 6-stage countercurrent back extraction on the organic phase in the step (4) by using an ammonia water solution with the pH of 12.8 at the temperature of 25 ℃, comparing with the O/A =4 for 1 min, and obtaining a vanadium solution with the purity of 99.93%.
In conclusion, the high-purity vanadium liquid and chromium liquid can be obtained by the process method.
Claims (5)
1. An extraction solvent for simultaneously extracting and separating vanadium and chromium from a vanadium and chromium-containing solution, which is characterized in that the extraction solvent is formed by mixing an extraction agent and a diluent, the extraction agent is water-soluble amide with the solubility lower than 0.5g/L, the diluent is an inert organic solvent, the extraction agent is one or more of N-alkyl amide and N, N, N, N-tetraalkyl diamide or water-soluble amide containing a plurality of amide groups and the solubility of which is lower than 0.5g/L, the alkyl is straight-chain alkyl or branched-chain alkyl, the diluent is one or more of sulfonated kerosene, white oil and an inert organic solvent of halogenated hydrocarbon compounds which are liquid at normal temperature, one of the extraction agent and the diluent is solid at 25 ℃ or when both are solid at 25 ℃, the mass ratio of the extraction agent in the extraction solvent is 2% -100%, the mass percentage of the diluent is 0-98%, and when the extracting agent and the diluent are both liquid at 25 ℃; the volume of an extracting agent in an extracting solvent is 5-100%, the volume of a diluent is 0-95%, the carbon number of alkyl in acyl is 1-18 in N-alkylamide and N, N, N, N-tetraalkyl diamide or water-soluble amide containing a plurality of amide groups and having the solubility lower than 0.5g/L, the carbon number of alkyl in the N-alkylamide is 1-18, the carbon number of alkyl in the N-alkylamide directly connected with a nitrogen atom is 1-18, the carbon number of N, N, N, N-tetraalkyl diamide or alkyl in the amide groups directly connected with the nitrogen atom is the same alkyl or different alkyls, the carbon number of the two alkyls directly connected with the nitrogen atom is 1-18 respectively, the carbon number of the sulfonated kerosene is 11-17, the white oil type is 1-7 #, the halogenated hydrocarbon compound which is liquid at normal temperature is chlorohydrocarbon, or chlorinated hydrocarbon, One or more of brominated hydrocarbon or iodocarbon inert organic solvents.
2. A method for simultaneously extracting and separating vanadium and chromium from a vanadium and chromium-containing solution is characterized by comprising the following process steps:
(1) preparing an extraction solvent: the extraction solvent is formed by mixing an extraction agent and a diluent, wherein the extraction agent is water-soluble amide with the solubility lower than 0.5g/L, the diluent is an inert organic solvent, and the extraction solvent is prepared by mixing the extraction agent and the diluent to be an organic phase;
(2) extraction: extracting the vanadium-chromium-containing solution by using the extraction solvent in the step (1), wherein the pH of the vanadium-chromium-containing solution is 1.3-10, the extraction temperature is 10-90 ℃, the extraction time is 1-10 min compared with the time when the O/A = 0.4-4.0, the extraction mode is countercurrent extraction, fractional extraction or cross-flow extraction, and the extraction stage number is 1-35, so as to obtain a loaded organic phase;
(3) washing: washing the loaded organic phase obtained in the step (2) with a solution, wherein the pH of the solution is 1.2-9.0, the temperature is 10-90 ℃, and the time is 1-10 min compared with the time that O/A = 0.4-40, so as to obtain a washed organic phase;
(4) stripping chromium: taking the washed organic phase obtained in the alkaline solution back-extraction step (3), extracting at the temperature of 10-60 ℃ for 1-8 min compared with the time of 1-20O/A, wherein the pH of the alkaline solution is 7.2-10.0, the back-extraction mode is countercurrent extraction or cross-flow extraction, and the extraction stages are 1-10 stages, so as to obtain high-purity chromium solution and the vanadium-loaded organic phase;
(5) stripping vanadium: and (3) carrying out back extraction on the vanadium-loaded organic phase obtained in the step (4) by using an alkaline solution, wherein the extraction temperature is 10-60 ℃, the extraction time is 1-10 min compared with the time of O/A = 1-10, the pH of the alkaline solution is 7.5-13.5, the back extraction mode is countercurrent extraction or cross-flow extraction, and the extraction stage number is 1-10, so that the high-purity vanadium liquid is obtained.
3. The method of claim 2, wherein the vanadium-chromium-containing solution comprises a leaching solution of vanadium titano-magnetite smelting waste residue, a mixed solution of two or more vanadium-or chromium-containing polymetallic sulfuric acid media, wherein the solution contains both vanadium and chromium; the valence of vanadium is tetravalent or pentavalent, or a mixture of tetravalent and pentavalent vanadium; the valence state of chromium is trivalent or hexavalent, or a mixture of trivalent and hexavalent.
4. The method for simultaneously extracting and separating vanadium and chromium from a vanadium and chromium containing solution according to claim 2, characterized in that in the step (4) and the step (5), the alkaline substance is one or a mixture of ammonia, sodium hydroxide, potassium hydroxide, calcium hydroxide, sodium carbonate, ammonium carbonate, potassium carbonate, ammonium chloride and ammonium sulfate.
5. The method for simultaneously extracting and separating vanadium and chromium from a vanadium and chromium containing solution as claimed in claim 2, characterized in that the solution in the step (3) is an acidic solution, and the acidic solution comprises a mineral acid which is not easily oxidized by sulfuric acid or nitric acid, or a mixture containing one or two of the mineral acids.
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