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Uranium, iron, thorium and rare earth extraction and separation process

A rare earth extraction, separation and process technology, which is applied in the field of uranium, iron, thorium and rare earth extraction and separation processes, can solve the problems of difficult separation from uranium and inability to meet commodity requirements, achieve comprehensive utilization, avoid ammonia nitrogen wastewater problems, reduce The effect of extraction separation stages and investment

Active Publication Date: 2017-02-15
永州市湘江稀土有限责任公司
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  • Abstract
  • Description
  • Claims
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Problems solved by technology

In the separation process of U and Fe, the iron in the loaded organic exists in the form of trivalent, and it is difficult to separate from uranium. Generally, increasing the number of stages and increasing the amount of washing is used to improve the separation efficiency of uranium and iron, but the obtained iron nitrate raffinate still contains Contains dozens or even hundreds of ppm of U, which cannot meet the requirements of the product

Method used

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  • Uranium, iron, thorium and rare earth extraction and separation process

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Effect test

Embodiment 1

[0033] Use 30% P in the hydrochloric acid system 350 ‐ Kerosene extraction system for UFe / ThRE separation, control the concentration of [RE+Th+U+Fe+Ti] in the feed liquid to 180g / L, [TiO 2 ]=3.5g / L, [H + ] = 2.0 mol / L, using countercurrent extraction, compared to organic phase: aqueous phase = 4: 1, the number of extraction stages is 15, and the organic phase loaded with U and Fe and the raffinate containing Th and RE are obtained. Using 2.0 mol / L HCl to countercurrent wash the organic phase loaded with U and Fe, the comparison is organic phase:water phase=6:1, and the number of stages is 18.

[0034] The organic phase is fed with loaded U and Fe, and the washing section uses 0.3mol / L HNO 3 (which contains 3wt.%H 2 o 2 ) solution to wash the loaded U and Fe organic phases, the extraction section uses a blank P350 organic phase feed, and separates U / Fe by fractional extraction to obtain an organic phase loaded with pure U and Fe(NO 3 ) 2 raffinate. Compared with blank or...

Embodiment 2

[0041] Use 35% P in the hydrochloric acid system 350 ‐ Kerosene extraction system for UFe / ThRE separation, control the concentration of [RE+Th+U+Fe+Ti] in the feed liquid to 250g / L, [TiO 2 ]=1g / L, [H + ]=2.5mol / L, using counter-current extraction, compared to organic phase:water phase=3:1, the number of extraction stages is 18, and the organic phase loaded with U and Fe and the raffinate containing Th and RE are obtained. 2.5 mol / L HCl is used for countercurrent washing of the organic phase loaded with U and Fe, compared to organic phase:water phase=6:1, and the number of stages is 18.

[0042] The organic phase is fed with loaded U and Fe, and the washing section uses 0.5mol / L HNO 3 (which contains 5wt.% Na 2 SO 3 ) solution to wash the loaded U and Fe organic phases, the extraction section uses a blank P350 organic phase feed, and separates U / Fe by fractional extraction to obtain an organic phase loaded with pure U and Fe(NO 3 ) 2 raffinate. Compared with blank organi...

Embodiment 3

[0045] Use 25% P in the hydrochloric acid system 350 ‐ Kerosene extraction system for UFe / ThRE separation, control the concentration of [RE+Th+U+Fe+Ti] in the feed liquid to 200g / L, [TiO 2 ]=2g / L, [H + ]=2.3mol / L, using counter-current extraction, compared to organic phase:water phase=4:1, extraction stage is 20, to obtain organic phase loaded with U and Fe and raffinate containing Th and RE. Use 2.2mol / L HCl to carry out the countercurrent washing of the organic phase loaded with U and Fe, and the comparison is organic phase:water phase=8:1, and the number of stages is 20.

[0046] The organic phase is fed with loaded U and Fe, and the washing section uses 0.5mol / L HNO 3 (Containing 1wt.% ascorbic acid) solution washes the loaded U and Fe organic phases, the extraction section uses a blank P350 organic phase feed, and U / Fe is separated by fractional extraction to obtain the organic phase loaded with pure U and Fe (NO 3 ) 2 raffinate. Compared with blank organic phase: l...

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Abstract

The invention relates to a uranium, iron, thorium and rare earth extraction and separation process, wherein a UFe / ThRE-containing solution is subjected to extraction and separation with P350 in a hydrochloric acid system, a reducing substance is added to the obtained U-Fe-supported organic phase, the organic phase is subjected to washing-iron with a nitric acid solution to obtain the pure-U-supported organic phase and the raffinate containing bivalent iron, and the pure-U-supported organic phase is subjected to back extraction with a Na2SO4-containing H2SO4 solution so as to obtain the UO2SO4 solution. According to the present invention, with the introduction of the reducing substance into the process, the difficultly-separated trivalent iron and the hexavalent uranium can be effectively separated; and the whole process achieves the comprehensive utilization of the whole element.

Description

technical field [0001] The invention is an extraction and separation process for uranium, iron, thorium and rare earth, specifically, UFe / ThRE is separated by using P350 in a hydrochloric acid system, and reducing substances are added in the U / Fe separation process to reduce ferric iron , to solve the effective separation of iron and uranium, to obtain uranium-containing substances and ferric nitrate products respectively, belonging to the field of rare earth hydrometallurgy. Background technique [0002] Monazite is one of the important rare earth ores. This kind of ore also contains a considerable amount of uranium, which is a nuclear fuel urgently needed by the country at present, and contains a high content of thorium, which is a valuable resource for important nuclear fuel in the future. After monazite concentrate is extracted by traditional alkali decomposition-hydrochloric acid solution, the remaining radioactive thorium uranium (rare earth) solution slag also contain...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C22B3/26C22B60/02C22B59/00
Inventor 俞正明李效平王凯严炳琛陈伯华李金叶徐学道
Owner 永州市湘江稀土有限责任公司
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