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Thorium and uranium separating and recovering method

A technology of separation and recovery, acid aqueous solution, applied in the field of separation and recovery of thorium and uranium, and can solve the problems of low thorium yield and the like

Active Publication Date: 2017-04-05
SHANGHAI INST OF APPLIED PHYSICS - CHINESE ACAD OF SCI
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0004] The technical problem to be solved by the present invention is that in order to overcome the low yield of thorium in the existing method for separating and recovering thorium and uranium from thorium-based spent fuel, it is necessary to adopt higher feed acidity, organic phase / water phase flow ratio and more fractional distillation extraction stages and other defects, and a method for separation and recovery of thorium and uranium is provided

Method used

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  • Thorium and uranium separating and recovering method
  • Thorium and uranium separating and recovering method
  • Thorium and uranium separating and recovering method

Examples

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Embodiment 1

[0032] 1) Using kerosene as an organic solvent, prepare an organic solution with a volume concentration of 25% of methylphosphonic acid bis(1-methyl)heptyl, as an extractant, prepare a Th 4+ , UO 2 2+ 、Zr 4+ , Nb 5+ , Ru(RuNO 3+ ), Rh 3+ 、Sr 2+ 、Cs + 、Ce 3+ 、Ce 4+ 、Gd 3+ 、Dy 3+ 1M aqueous nitric acid solution, where Th 4+ , UO 2 2+The concentration is 200g / L, 2g / L, and the concentration of other metal ions is 20ppm. As the feed liquid, a 0.2M aqueous solution of nitric acid is prepared, and as the washing liquid, the above solution is subjected to fractional extraction. The extraction stages are 10, and the washing stages are Level 8, the flow ratio of feed liquid, extractant, and washing liquid is 1:5:0.5, thorium and uranium are extracted into the organic phase, while impurity metal ions remain in the water phase, the concentration of thorium and uranium in the organic phase and water phase at all levels distributed as figure 2 shown;

[0033] figure 2 The...

Embodiment 2

[0039] 1) Using n-dodecane as an organic solvent, prepare an organic solution with a volume concentration of 15% of methylphosphonic acid bis(1-methyl)heptyl, as an extractant, prepare a Th 4+ , UO 2 2+ 、Zr 4+ , Nb 5+ , Ru(RuNO 3+ ), Rh 3+ 、Sr 2+ 、Cs + 、Ce 3+ 、Ce 4+ 、Gd 3+ 、Dy 3+ 2M aqueous nitric acid solution, where Th 4+ , UO 2 2+ The concentration is 200g / L, 2g / L, and the concentration of other metal ions is 20ppm. As the feed liquid, a 0.2M aqueous solution of nitric acid is prepared, and as the washing liquid, the extraction agent, feed liquid and washing liquid are subjected to fractional distillation extraction, and the number of extraction stages is 10. Level, the number of washing stages is 6, the flow ratio of feed liquid, extractant, and washing liquid is 1:7:1, thorium and uranium are extracted into the organic phase, while impurity metal ions remain in the water phase;

[0040] 2) Using kerosene as an organic solvent, prepare an organic solution wit...

Embodiment 3

[0044] 1) Using n-dodecane as an organic solvent, prepare an organic solution with a volume concentration of 20% of methylphosphonic acid bis(1-methyl)heptyl, as an extractant, prepare a Th 4+ , UO 2 2+ 、Zr 4+ , Nb 5+ , Ru(RuNO 3+ ), Rh 3+ 、Sr 2+ 、Cs + 、Ce 3+ 、Ce 4+ Gd 3+ 、Dy 3+ 0.6M aqueous nitric acid solution, where Th 4+ , UO 2 2+ The concentration is 200g / L, 2g / L, and the concentration of other metal ions is 20ppm. As the feed liquid, a 1.0M aqueous solution of nitric acid is prepared, and as the washing liquid, the extraction agent, feed liquid and washing liquid are subjected to fractional distillation and extraction, and the number of extraction stages is 9. level, the number of washing stages is 7, the flow ratio of feed liquid, extractant, and washing liquid is 1:4:0.8, thorium and uranium are extracted into the organic phase, while impurity metal ions remain in the water phase;

[0045] 2) Using kerosene as an organic solvent, prepare an organic soluti...

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Abstract

The invention discloses a thorium and uranium separating and recovering method. The method comprises the following steps: 1) taking aqueous acid containing thorium and uranium as material liquid, taking an organic solvent containing methylphosphonic acid di(1-methyl) heptyl ester, taking the aqueous acid as washing liquid for fractionation and extraction; 2) taking the organic solvent containing methylphosphonic acid di(1-methyl) heptyl ester as an extraction supplement agent, taking the aqueous acid as the washing liquid, and performing fractionation and extraction on an organic extract phase containing thorium and uranium, the extraction supplement agent, and the washing liquid; and 3) performing back extraction on the organic extract phase containing uranium and strip liquor in a multistage counter current mode. Under conditions of low feeding acidity, organic phase / water phase flow ratio and less extracting stage number, separating and recovery of thorium and uranium are realized, high thorium and uranium recovery rate can be obtained, and the impurity metal ion decontamination coefficient is obtained.

Description

technical field [0001] The invention relates to a method for separating and recovering thorium and uranium. Background technique [0002] Thorium is one of the important elements in the research and development of nuclear energy. It can absorb neutrons and transform into fissionable nuclide U-233 for nuclear fission reaction. Therefore, thorium is a very promising nuclear fuel. For the reprocessing of thorium-based nuclear fuel, it is necessary to recover and separate the unburned thorium and uranium in order to realize the full utilization of resources. [0003] So far, the recovery and separation of thorium and uranium are usually carried out by using TBP as the extraction agent and the Thorex process. However, in practical applications, TBP has deficiencies and defects. For example, the extraction performance of TBP to thorium is relatively low. In order to ensure the yield of thorium, it is necessary to add 12-13mol / L of concentrated nitric acid as the salting-out acid,...

Claims

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Application Information

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IPC IPC(8): C22B7/00C22B60/02
CPCC22B7/006C22B60/026C22B60/0291Y02P10/20
Inventor 张岚李峥李瑞芬刘春霞何淑华赵皓贵李晴暖于婷
Owner SHANGHAI INST OF APPLIED PHYSICS - CHINESE ACAD OF SCI
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