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A lithium extraction system

An extraction and system technology, applied to the improvement of process efficiency, etc., can solve the problems of large-scale industrial production, strong corrosion of extraction equipment, high solubility of brine, etc., and achieve easy industrial production, easy equipment selection, and simple production operation Effect

Active Publication Date: 2019-04-26
青海柴达木兴华锂盐有限公司
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  • Abstract
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Problems solved by technology

Lithium resources exist in the form of solid ore and salt lake brine. my country's salt lake lithium resources are rich, especially in the Qaidam Basin in Qinghai, with reserves of 24.47 million tons (LiCl). Due to the high content of associated magnesium, magnesium in brine The / lithium ratio (mass ratio) is as high as 40-1200, making it very difficult to separate and extract lithium
Extraction method is one of the most promising methods for extracting lithium from brine. The system with better effect is tributyl phosphate-ferric chloride-kerosene system. In 1979, Qinghai Salt Lake Research Institute of Chinese Academy of Sciences used this system to extract brine from Dachaidan Salt Lake. In the expansion test of lithium extraction, due to the high concentration of tributyl phosphate in the system, it is extremely corrosive to the extraction equipment, and the solubility of brine in the organic phase is relatively high, and the product purity is only about 98.5%, which has not been used in large-scale industrial production. Production

Method used

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Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0021] The ionic liquid is N-methyl-N-(N’-2-ethylcarbonyl) ethylpyrrole hexafluorophosphate, and its structural formula is:

[0022]

[0023] The co-extraction agent is a mixture of diisobutyl ketone and TBP, the ratio of the two is 4:1; the diluent is sulfonated kerosene. Add 1 volume of salt lake brine shown in Table 1 into a separatory funnel, add 1 volume of organic phase (compared to O / A=1), wherein the volume ratio of ionic liquid, co-extractant and diluent is 1 : 4: 5, after shaking for 10 minutes, rest and layer. Determination of Li in the equilibrium aqueous phase + content, the single extraction rate of lithium is calculated to be 76.84%.

[0024] As a comparison, similar to the conditions in Example 1, except that no N-methyl-N-(N'-2-ethylcarbonyl) ethylpyrrole hexafluorophosphate ionic liquid was added, the single extraction rate of lithium was 57.38 %.

Embodiment 2

[0026] The ionic liquid is N-ethyl-N-(N’-2-ethylcarbonyl) ethylpyrrole hexafluorophosphate, and its structural formula is:

[0027]

[0028] The co-extraction agent is TBP (tributyl phosphate), and the diluent is solvent gasoline. In a separating funnel, add 1 volume of salt lake brine as shown in Table 1, and add 2 volumes of the organic phase (compared to O / A = 2), wherein the volume ratio of ionic liquid, co-extraction agent and diluent is 2:4:4, shake for 10 minutes and then static layering. Determination of Li in the equilibrium aqueous phase + content, the single extraction rate of lithium is calculated to be 80.34%.

[0029] As a comparison, similar to the conditions in Example 2, except that no N-methyl-N-(N'-2-ethylcarbonyl) ethylpyrrole hexafluorophosphate ionic liquid was added, the single extraction rate of lithium was 61.35 %.

Embodiment 3

[0031] The ionic liquid is N-ethyl-N-[N'-(2-ethylhexyl)carbonyl]ethylpyrrole hexafluorophosphate, and its structural formula is:

[0032]

[0033] The extractant is amide compound N503, the diluent is petroleum ether, and 1 volume of salt lake brine shown in Table 1 and 3 volumes of organic phase (compared to O / A=3) are added to a separatory funnel, wherein the ion The volume ratio of liquid, co-extraction agent and diluent is 1:3:6, shake for 10 minutes and then static layer. Determination of Li in the equilibrium aqueous phase + content, the single extraction rate of lithium is calculated to be 70.15%.

[0034] As a comparison, similar to the conditions in Example 3, except that no N-methyl-N-(N'-2-ethylcarbonyl) ethylpyrrole hexafluorophosphate ionic liquid was added, the single extraction rate of lithium was 58.87 %.

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Abstract

The invention provides a system capable of extracting lithium from salt lake brine, including an ionic liquid, a co-extraction agent and a diluent, the ionic liquid is a pyrrole-type hexafluorophosphate ionic liquid containing functional groups for extracting lithium, and the diluent For solvent gasoline, sulfonated kerosene, petroleum ether. The extraction system used in the present invention can avoid the use of the co-extractant ferric chloride, so there is no need to adjust the pH of the brine. For every ton of lithium chloride produced, at least 5 tons of industrial hydrochloric acid and 2 tons of sodium hydroxide can be saved, greatly reducing The production cost is reduced; the process reduces the saponification process, acid washing process and iron removal process, so it is easier to industrialize large-scale production.

Description

technical field [0001] The invention relates to an extraction system for extracting lithium from salt lake brine with a high magnesium-lithium ratio by using a solvent extraction method. Background technique [0002] As a new strategic energy source, lithium is mainly used in fields such as batteries, nuclear power generation, aerospace, and medicine. Lithium resources exist in the form of solid ore and salt lake brine. my country's salt lake lithium resources are rich, especially in the Qaidam Basin in Qinghai, with reserves of 24.47 million tons (LiCl). Due to the high content of associated magnesium, magnesium in brine The / lithium ratio (mass ratio) is as high as 40-1200, which makes it very difficult to separate and extract lithium. Extraction method is one of the most promising methods for extracting lithium from brine. The system with better effect is tributyl phosphate-ferric chloride-kerosene system. In 1979, Qinghai Salt Lake Research Institute of Chinese Academy o...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C22B26/12C22B3/40
CPCC22B26/12C22B3/409Y02P10/20B01D11/0492B01D11/0419
Inventor 孟庆芬赵朋龙秦超王伟伟李亚鹏
Owner 青海柴达木兴华锂盐有限公司
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