Separation of actinides and REEs using TODGA in meta-nitrobenzotrifluoride: development and demonstration of flowsheet

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Abstract

A process was developed for the extraction and separation of actinides and REEs from PUREX process raffinates using TODGA in meta-nitrobenzotrifluoride (F-3). The proposed flowsheet was tested under dynamic conditions using simulated raffinates of the PUREX process. The scheme includes joint extraction of actinides and REE, nitric acid stripping, actinide stripping, and REE stripping. The conditions of selective MA stripping by DTPA solution in the presence of a salting-out agent were determined.

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About the authors

L. I. Tkachenko

Khlopin Radium Institute

Author for correspondence.
Email: mikkaly@gmail.com
Russian Federation, 2-i Murinskii pr. 28, St. Petersburg, 194021

E. V. Kenf

Khlopin Radium Institute

Email: mikkaly@gmail.com
Russian Federation, 2-i Murinskii pr. 28, St. Petersburg, 194021

V. A. Babain

Khlopin Radium Institute

Email: mikkaly@gmail.com
Russian Federation, 2-i Murinskii pr. 28, St. Petersburg, 194021

M. Yu. Alyapyshev

AO Polymetal Engineering

Email: mikkaly@gmail.com
Russian Federation, pr. Narodnogo Opolcheniya 2, St. Petersburg, 198216

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Supplementary files

Supplementary Files
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2. Fig. 1. Values of metal distribution coefficients during extraction from 3 M HNO3; 0.001 M of each metal, indicator amounts of 241Am. Extraction agent – 0.1 M TODGA in F-3

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3. Fig. 2. Distribution coefficients of Pd and Zr during extraction from 3 M HNO3 in the presence of complexones. Extraction agent – 0.1 M TODGA in F-3

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4. Fig. 3. Isotherm of REE extraction from model solution No. 1, diluted with 3 M nitric acid to the required REE concentrations. Extractant – 0.1 M TODGA in F-3

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5. Fig. 4. Structural formulas of the studied water-soluble complexones

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6. Fig. 5. Dependence of the distribution coefficients of Am (solid line) and Eu (dashed line) on the concentration of nitric acid. Extraction agent – 0.1 M TODGA in F-3. Aqueous phase – nitric acid + 0.1 M complexone (DEMGA or TEDGA) + 10–5 M Eu(NO3)3 + indicator amounts of 241Am or 152Eu

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7. Fig. 6. Dependence of the distribution coefficients of Am and REE on the pH of the aqueous phase. Extractant – 0.1 M TODGA in F-3. Aqueous phase – 10 g/L DTPA + 120 g/L NH4NO3 + 1×10–3 M ∑REE + indicator amounts of 241Am

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8. Fig. 7. Separation coefficients of DREE/DAm depending on the pH of the aqueous phase. Extraction agent – 0.1 M TODGA in F-3. Aqueous phase – 10 g/L DTPA + 120 g/L NH4NO3 + 1×10–3 M ∑REE + indicator amounts of 241Am

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9. Fig. 8. Isotherm of nitric acid extraction. Extractant – 0.1 M TODGA in F-3

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10. Fig. 9. Dependence of the pH value on the amount of glycine in the re-extractant (10 g/l DTPA + 120 g/l NH4NO3) after adding 0.15 M HNO3 to it

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11. Fig. 10. Dependence of the pH value of the re-extractant (10 g/l DTPA + 120 g/l NH4NO3) on the concentration of Nd (pHin 2.02)

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12. Fig. 11. Dependence of metal distribution coefficients on the pH of the stripping agent at different concentrations of REE. Extraction agent – 0.1 M TODGA in F-3. Stripping agent – 10 g/l DTPA + 120 g/l NH4NO3 + REE + indicator amounts of 241Am

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13. Fig. 12. Dependence of the equilibrium pH value of the stripping agent on the Nd concentration. Stripping agent – 10 g/l DTPA + 120 g/l NH4NO3 + 0.1 M buffer (pНinc 2.05)

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14. Fig. 13. Distribution coefficient values of metals and nitric acid. Organic phase – 0.1 M TODGA in F-3. Aqueous phase – 180 g/l NH4NO3

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15. Fig. 14. Flow chart for separation of TPE and REE

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