Technology for reprocessing mother liquor and washing solution from crystalization purification of HTGR SNF

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Abstract

The extractants diphenyl-N,N-dioctylcarbamoylmethylphosphine oxide and diphenyl-N,N-diisobutylcarbamoylmethylphosphine oxide for the processing of spent fuel were tested. The conditions for extraction and separation of uranium and TPE–REE were determined. A technological scheme was proposed for processing spent nuclear fuel from high-temperature gas-cooled reactors. During dynamic testing, at least 99.9% of uranium and plutonium and at least 99.5% of americium and rare earth elements were extracted. The TPE + REE and U+Pu fractions were isolated. The U+Pu fraction contained approximately 5% Am, while the TPE + REE fraction had less than 0.1% U and Pu.

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About the authors

L. I. Tkachenko

Khlopin Radium Institute

Email: vlvidanov@bochvar.ru
Russian Federation, 2-i Murinskii pr. 28, St. Petersburg, 194021

V. L. Vidanov

Bochvar High-Technology Research Institute of Inorganic Materials

Author for correspondence.
Email: vlvidanov@bochvar.ru
Russian Federation, ul. Rogova 5a, Moscow, 123098

E. V. Kenf

Khlopin Radium Institute

Email: vlvidanov@bochvar.ru
Russian Federation, 2-i Murinskii pr. 28, St. Petersburg, 194021

N. Yu. Volodina

Khlopin Radium Institute

Email: vlvidanov@bochvar.ru
Russian Federation, 2-i Murinskii pr. 28, St. Petersburg, 194021

Ya. O. Pleshakov

Khlopin Radium Institute

Email: vlvidanov@bochvar.ru
Russian Federation, 2-i Murinskii pr. 28, St. Petersburg, 194021

A. Yu. Shadrin

Science and Innovations Private Enterprise for Nuclear Industry Scientific Development

Email: vlvidanov@bochvar.ru
Russian Federation, ul. Bol’shaya Ordynka 44, str. 3, Moscow, 119017

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2. Fig. 1. Structural formulas of carbamoylmethylphosphine oxides.

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3. Fig. 2. Isotherm of uranium extraction from 3 mol/l HNO3 using the extraction system 0.2 mol/l CMFO-1 + 30 vol% TBP in F-3.

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4. Fig. 3. Values ​​of distribution coefficients during extraction from HNO3 solutions in the presence of 25 g/l U using the extraction system 0.25 mol/l CMFO-1 + 30 vol% TBP in F-3.

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5. Fig. 4. Schematic diagram of the processing of VGTR MPR using the extraction system 0.25 mol/l CMFO-1 + 30 vol% TBP + F-3.

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