Electro-Decontamination of Spent Ion Exchange Resins Contaminated with Iron Oxide Deposits under Dynamic Conditions

Abstract

A method for the electro-decontamination of spent ion exchange resin contaminated with hematite under dynamic conditions using sulfuric acid solutions has been suggested. It has been shown that decontamination under dynamic conditions excludes the secondary adsorption of radionuclides on ion-exchanger sites. The efficiency of this approach has been compared to that of control experiments without direct current treatment. A positive effect of the introduction of Fe2+ on the rate of dissolution of hematite has been demonstrated. This allows for decreasing the concentration of the sulfuric acid solution without decreasing the decontamination efficiency.

1. Introduction

The steel elements of a nuclear power plant (NPP) continue to become partially corroded in the course of its service. As a result of this process and subsequent hydrolysis, iron oxide/hydroxide particles are formed in the condensation water [1,2]. Such particles, generally called “crud”, have a mixed chemical composition, which is mainly represented by iron and, to a lesser extent, chromium, nickel, cobalt, and zinc [3,4]. Crud particles tend to adsorb short-lived radionuclides of the corrosion group [3], which leads to the risk of receiving increased dose loads for maintenance personnel. The crud is removed from the NPP system water by means of mechanical filtration on columns with ion-exchange resins, followed by reverse washing. In the process of mechanical filtration, some parts of the crud bind irreversibly due to diffusion in the pore space of an ion-exchange resin grain [5], which complicates the regeneration and subsequent disposal of spent ion-exchange resins (SIER).

The utilization of SIER by direct immobilization into cement matrices and the use of thermal destruction methods (pyrolysis, combustion) demonstrate a number of substantial disadvantages, such as a decrease in the strength of cement matrices, as well as the formation of secondary gaseous products [6,7,8]. Liquid-phase oxidation based on the Fenton or electro-Fenton process, accompanied by the destruction of ion-exchanger due to depolymerization [9,10], is free of these disadvantages. Possible disadvantages of liquid-phase oxidation include the use of concentrated solutions of hydrogen peroxide, the incomplete dissolution of SIER, and the formation of secondary liquid waste containing ion-exchanger decomposition products.

The removal of iron oxide deposits without destroying the polymer matrix represents a promising approach to SIER decontamination. For example, SIER contaminated with crud are treated by HNO₃ and H₂SO₄ solutions at heating (80–120 °C) [11,12] or citrate solutions with the addition of ascorbic acid [13,14]. Upon decontamination, Co-60 can be removed from acidic solutions by electrodeposition on a cathode [11,12]. Thereafter, decontaminated SIER can be dumped at a domestic waste disposal site [15].

The efficiency of the SIER decontamination by methods not involved in the destruction of the polymer matrix depends on the degree of removal of iron oxide deposits, which, in its turn, is determined by the completeness of the dissolution of hematite formed by the oxidation of magnetite with dissolved oxygen [2] or due to the transformation of goethite [1]. A significant issue here lies in the fact that it is difficult to dissolve hematite in mineral acids and in the presence of chelating agents, such as EDTA, IDA, and NTA, compared to goethite and magnetite [16,17,18].

In our opinion, the optimal method for decontaminating SIER contaminated with iron oxide deposits consists of treatment in the near-cathode reduction space in solutions of mineral acids under static conditions without adding organic impurities. The potential of such an approach was demonstrated in [19]. The dissolution of hematite occurs in accordance with the following reactions:

• 2H⁺ + 2ē → 2H₂↑ (cathode),
• 2H₂O − 4ē → O₂↑ + 4H⁺ (anode),
• Fe₂O₃ + 6H⁺ + 2ē → 2Fe²⁺(aq) + 3H₂O [20].

Thus, the dissolution of hematite is intensified in the near-cathode space due to the reduction processes. It is worth mentioning that, after the hematite dissolution, the cobalt radionuclides enter the solution in an ionic form and can bind to the ion-exchanger exchange groups. In order to regenerate SIER and remove the radionuclide, it is necessary to additionally wash it with acid solutions containing an excess of sodium ions [19], which yields an increase in the volume of secondary waste. To solve this problem, the electro-decontamination of SIER can be carried out directly under dynamic conditions, which will prevent the secondary adsorption of cobalt radionuclide. Hence, the objective of the present work is to evaluate the efficiency of the SIER electro-decontamination process carried out under dynamic conditions.

2. Materials and Methods

Iron(III) chloride (FeCl₃ × 6H₂O), iron (II) sulfate (FeSO₄ × 7H₂O), ammonium hydroxide (NH₄OH), a solution of sulfuric acid at a concentration of 17.5 mol/L (H₂SO₄), and a solution of nitric acid at a concentration of 13.3 mol/L (HNO₃) of chemically pure grade were purchased from NevaReaktiv, Russia, and used without additional purification. The radionuclide Co-57 in 1 mL of 1 M HCl solution with an activity of 5 MBq (1.6 × 10⁻⁸ g of Co-57) was acquired from the Leypunskiy Institute of Physics and Power Engineering. The KU 2-8 cation-exchanger was purchased from TOKEM, Russia. Prior to the start of the experiment, the cation-exchanger was washed with a 1 M solution of HNO₃ under dynamic conditions; thereafter, it was washed free from the acid residues with distilled water and stored in a flask with a plug stopper.

Model SIER were prepared according to the method described in [21]. The ion exchange resin KU 2-8 was pre-saturated with the radionuclide Co-57. For this purpose, 50 mL of Na-form ion-exchanger was transferred to a glass column, and distilled water labeled with the Co-57 radionuclide was fed through it at a rate of 30 mL/h. The ion-exchanger containing the radionuclide Co-57 was transferred to a conical flask containing 250 mL of FeCl₃ solution of a concentration of 0.2 mol/L; then, the resulting pulp was stirred for 24 h. After the specified time, the pulp was alkalized with a NH₄OH solution at a concentration of 10 mol/L to a neutral reaction and held for 3–6 h. After acidification with HCl solution to pH 2, the pulp was transferred to a stainless steel autoclave with an inner Teflon chamber and hydrothermally treated for 24 h at a temperature of 175 °C. The hydrothermal treatment leads to the formation of a hematite phase (card number No. 00-210-8027) on the surface and in the bulk of the resin grains (Figure 1).

After the treatment, the model SIER was washed by decanting from the remains of hematite particles formed outside an ion-exchanger grain, then treated under dynamic conditions with a solution of the following composition: HNO₃—3 mol/L, NaNO₃—1 mol/L with a volume of 500 mL.

The experiments were performed using an electrochemical cell with a volume of 45 mL; the working volume was 30 mL (Figure 2). The cell consisted of two interconnected segments, where an anode in the form of a plate and a spiral cathode were placed. The near-cathode space was additionally contained by a glass cylinder of an internal diameter of 1.2 cm with a cross-linked bottom made of a chemically resistant polymer. For further treatment, 2 mL of the model SIER was placed in a glass cylinder.

The treatment of the model SIER under dynamic conditions was performed by feeding H₂SO₄ solution through the cell at a rate of 4 mL/h. It was then collected using a fraction collector, and the specific activity of Co-57 was measured. The electro-decontamination process was accompanied by the partial flaking-off of hematite from the surface of the model SIER and its delivery from the inner glass cell into the glass body. The flaked-off hematite residue was removed from the cell; then, the specific activity (RA) was measured. During the treatment, the cell was heated up; then, it was placed in a container with water to cool down to room temperature (22 ± 5 °C). The temperature inside the cell was continuously monitored using an electronic thermometer.

The total decontamination efficiency (sDE) was calculated using Equation (1):

$$sDE(\%)=\left(\frac{{\sum }_{V=0}^n\left(V\times A_i\right)}{A_0}\right)\times 100,$$

(1)

where V is the amount of solution passed through the cell at the time of measurement (mL), A_i is the activity of the passed solution (DPM/mL), and n is the total amount of the solution passed through the cell (mL).

To describe the decontamination process of the model SIER under dynamic conditions, the logistic equation (2) was used to describe the experimental values in the coordinates A/A₀ = f(V):

$$\frac{A}{A_0}=\frac{G}{1+e^{-\frac{V-A}{B}}},$$

(2)

where A₀ is the total activity of the model SIER (DPM), A is the activity of the fraction of the fed solution (DPM), G is the maximum expected desorption efficiency (unit fraction), V is the volume of the passed solution (mL), A is the volume of the H₂SO₄ solution required to be fed through the resin to achieve a decontamination efficiency of 50 % (mL), B is the dimensionless coefficient inverse to the exponential growth value.

The control experiment without electro-decontamination was carried out as follows: a model SIER of a volume of 2 mL was placed in a glass column with an internal diameter of 1.2 cm. The H₂SO₄ solution was fed through the column at a rate of 2 mL/h. The filtrate was collected using a fraction collector, and the activity of Co-57 was measured.

The accuracy of the measurement of the activity of model SIER and solution fed through the cell was estimated through the determination of the confidence interval (CI_0.95) with the confidence level of 0.95 (p < 0.05) as a standard deviation of ×1.96 in accordance with Equation (3):

$$C{I}_{0.95}=\frac{\sqrt{n}}{t}\times 1.96,$$

(3)

where n is the quantity of registered impulses and t is the measurement time (min).

The specific activity of Co-57 (photopeak energy: 122 keV) was determined by the direct radiometric method using an RKG-AT1320 gamma-radiometer equipped with a NaI(Tl) detector measuring 63 × 63 mm (RPE Atomtech, Republic of Belarus). The X-ray phase analysis was performed using a D8 ADVANCE diffractometer, X-ray images of the samples were recorded in the range of angles 2θ 3–85° with a step of 0.02° at the count point of 0.6 s. The phase composition was identified using the Qualx2. 0 software. The results were processed using the SciDAVis software (ver 1.23).

3. Results

Figure 3 shows decontamination curves without electro-decontamination, which was carried out by feeding the H₂SO₄ solution through a fixed layer of the model SIER placed in the column. The experimental parameters and the logistic equation coefficients are summarized in

Table 1. Decontamination efficiency and coefficients obtained by approximating the experimental data using the logistic equation without electro-decontamination.

Experiment	FeSO4 (mol/L)	H2SO4 (mol/L)	G	A	B	R2	sDE
1	-	1	1.0 ± 0.02	54.6 ± 0.8	14.3 ± 0.5	0.9971	96.6
2	-	2	1.02 ± 0.01	50.4 ± 0.7	13.9 ± 0.6	0.9972	97.5
3	0.1	1	1.02 ± 0.01	46.7 ± 0.6	11.7 ± 0.5	0.9971	98.8
4	0.1	2	1.0 ± 0.02	40.0 ± 0.6	8.8 ± 0.4	0.9967	98.9

.

The experimental data are adequately described by an S-type logistic curve (R² > 0.95).

Figure 4 shows the results of the electro-decontamination of the model SIER in the presence of H₂SO₄ solutions: the experimental conditions and the calculated values of the logistic equation are provided in

Table 2. Decontamination efficiency and coefficients obtained by approximating the experimental data using the logistic equation.

Experiment	H2SO4 (mol/L)	Current (A)	G	A	B	R2	RA	sDE
5	1	1.0	0.70 ± 0.02	19.7 ± 0.5	5.2 ± 0.4	0.9940	22	91.5
6	1	1.5	0.78 ± 0.05	18.0 ± 1.3	5.7 ± 1.0	0.9861	14	92.2
7	1	2.0	0.82 ± 0.04	17.0 ± 1.0	6.0 ± 0.8	0.9799	10	92.5
8	2	1.0	0.80 ± 0.01	10.0 ± 0.2	3.2 ± 0.1	0.9981	17	97.4
9	2	1.5	0.82 ± 0.01	8.5 ± 0.2	3.6 ± 0.2	0.9980	16	98.4
10	2	2.0	0.84 ± 0.01	7.2 ± 0.1	3.4 ± 0.1	0.9993	14	98.4

.

The experimental data obtained using electro-decontamination are also adequately described by the logistic equation; however, the curve shape is different, which indicates changes in the rate and character of hematite dissolution.

The effect of Fe²⁺ (FeSO₄) on the efficiency and rate of the decontamination of the model SIER under dynamic conditions was evaluated. The results are shown in Figure 5; the experimental conditions and the calculated values of the logistic equation are provided in

Table 3. Decontamination efficiency and coefficients obtained by approximating the experimental data using the logistic equation.

Experiment	FeSO4 (mol/L)	H2SO4 (mol/L)	Current (A)	G	A	B	R2	RA	sDE
11	0.1	1	1.5	0.82 ± 0.03	18.1 ± 0.4	3.8 ± 0.3	0.9942	12	94.4
12	0.1	2	1.5	0.95 ± 0.03	12.8 ± 0.4	3.2 ± 0.3	0.9931	3	97.9
13	0.2	1	1.5	0.94 ± 0.03	15.2 ± 0.4	4.0 ± 0.3	0.9955	5	98.4
14	0.2	2	1.5	0.94 ± 0.02	9.7 ± 0.3	2.7 ± 0.2	0.9918	4	98.5

.

Figure 6 shows the gamma spectra of the model SIER before the treatment and after electro-decontamination under dynamic conditions (experiment 12) in comparison with the background spectrum.

4. Discussion

The experimental data obtained using H₂SO₄ solutions without electrochemical treatment are adequately described by the logistic curve with a high determination coefficient (Figure 3, Table 1). The G values reach one whereas the actual decontamination efficiency exceeds 96%, which indicates that H₂SO₄ solutions can be used for the effective removal of crud in the form of hematite deposits. By increasing the concentration of the H₂SO₄ solution, the decontamination efficiency increases insignificantly.

The introduction of Fe(II) to the H₂SO₄ solution can intensify the hematite dissolution process. This assumption is based on the fact that, in neutral media, Fe(II) is adsorbed on the surface of hematite with subsequent oxidation until Fe(III) and electron transfer to Fe(III), which forms a part of the crystal lattice. The electron density redistribution between Fe(II) and Fe(III) is accompanied by the formation of a new mineral phase in the form of magnetite [22]. P. Larese-Casanova et al. [23] also provided data on the adsorption of Fe(II) on hematite with the formation of the Fe(OH)₂ phase. A. J. Frierdich [24] indicated that, along with a decrease of the size of hematite particles, the efficiency of Fe(II) adsorption increases due to the special features of the exchange. Here, on small particles, iron exchange occurs in their bulk, whereas, on large particles, adsorption occurs only in the surface layer [24]. J. G. Catalano et al. [25] stated that the oxidative adsorption of Fe(II) on hematite and the redistribution of electron density occur in acidic media as well. Here, the adsorption process is accompanied by structural changes in hematite. The possibility of the adsorption of Fe(II) from acidic media by hematite was confirmed by the results provided by B-H Jeon et al. [26].

To sum up, the preliminary introduction of Fe(II) to the H₂SO₄ solution can result in structural changes in hematite due to the adsorption and redistribution of electron density with subsequent formation of more soluble new phases, which, in its turn, can increase the solubility of iron oxide deposits on SIER. Indeed, it was found that the introduction of Fe(II) to the H₂SO₄ solution led to an increase in the intensity and completeness of the dissolution of hematite on the model SIER under dynamic conditions (Figure 3, lines 3, 4). It is worth mentioning that, despite satisfactory results, the disadvantage of this approach consists in the excessive consumption of the H₂SO₄ solution. To solve this problem, the intensity of dissolution of hematite deposits can be increased with the use of electro-decontamination of SIER.

In the course of electro-decontamination of SIER, the following features and regularities have been revealed. According to the values of the parameter G of the logistic equation, an increase of the concentration of the H₂SO₄ solution from 1 to 2 mol/L is accompanied by an increase in the efficiency of decontamination of the model SIER. It is worth mentioning, however, that the value of the G parameter cannot reach 100% because a part of hematite is mechanically flaked off from the model SIER without dissolution, which leads to a decrease in the total activity of the solution fed through the cell. An increase of the concentration of the H₂SO₄ solution enables one to half the total volume of the solution (parameter A) required for 50% decontamination of the model SIER, as well as to double the rate of dissolution of hematite deposits—a decrease of the parameter B. A similar effect was observed with a growth of the DC current, which increases the efficiency and rate of the SIER decontamination with smaller volumes of acid solution. The G value calculated using the logistic equation correlates to the actual residual activity of the model SIER, taking into account the residue of the undissolved hematite, whose weight and activity also depend on the treatment conditions. From the point of view of the actual efficiency of decontamination of the model SIER and the reduction in the cost for the direct current treatment, the most attractive treatment modes are No. 6 and No. 9. Therefore, further studies were performed at a DC power of 1.5 A.

During electro-decontamination, the addition of Fe²⁺ led to inconclusive results. In particular, in the case of using the H₂SO₄ solution of a concentration of 2 mol/L, only an increase of the G parameter was observed, whereas the values of A and B remained practically unchanged. This fact is related to the more complete dissolution of hematite deposits, which is corroborated by a decrease of the activity and, accordingly, the weight of the sediment remaining after the particles flaking-off. The residual activity of the model SIER, which is the most important indicator of the decontamination, also does not virtually change after the introduction of Fe²⁺.

A different picture is observed using the solution of H₂SO₄ of a concentration of 1 mol/L. The introduction of Fe²⁺ is accompanied by a decrease of the parameters A and B, as well as by an increase of G and the efficiency of decontamination of the resin. These results are compatible with those obtained using the solution of H₂SO₄ of a concentration of 2 mol/L. To sum up, the addition of Fe²⁺ allows the use of more dilute solutions of H₂SO₄, which firstly reduces economic costs and secondly decreases the potential corrosion of equipment. After the treatment, the gamma spectrum of the treated model SIERRA almost coincides with the background spectrum, which corroborates the efficiency of this decontamination method. In theory, decontaminated resins can be disposed of as non-radioactive waste.

It is worth mentioning that the introduction of Fe(II) allows for the complete disposal of secondary liquid radioactive waste. Here, the alkalization of the solution that was used for the decontamination of the model SIER with NH₄OHsolution of a concentration of 3 mol/L allows the complete deposition of Co-57 on the iron hydroxide sediment. The resulting sediment can be easily immobilized into a cement matrix, and the non-radioactive solution can be disposed of as sanitary waste.

Table 4. Comparison of the volume of the solutions formed during decontamination of the model SIER under different conditions.

Electro-Decontamination Conditions	Solution		The Solution/SIER Ratio (mL/mL)
	H2SO4 (1 mol/L)	NaNO3 (2 mol/L), HNO3 (1 mol/L)
Static	90 ± 9	30 ± 3	33
Dynamic	30 ± 10	0	15

shows the results of the comparison of the electro-decontamination of the model SIER under static and dynamic conditions. One can see that the decontamination under dynamic conditions eliminates the stage of additional washing of the resin, as well as reduces the volume of secondary liquid radioactive waste. The latter allows the process simplification as well as a reduction in the cost of decontamination of SIER with the use of electro-decontamination.

5. Conclusions

The possibility of the decontamination of SIER contaminated with hematite deposits using H₂SO₄ solutions under dynamic conditions has been evaluated. Increasing the concentration of the H₂SO₄ solution and introducing Fe²⁺ (FeSO₄) allows for improving the decontamination efficiency, which exceeds 96%. The disadvantage of this approach consists of the excessive consumption of the H₂SO₄ solution. As a result, the ratio of the volume of acid to the volume of swollen SIER exceeds 80, which can reduce the economic efficiency of this approach. The direct electric current treatment reduces the consumption of the H₂SO₄ solution more than twofold at a comparable efficiency to the SIER decontamination under dynamic conditions. For this purpose, the two-section electrochemical cell has been suggested. The introduction of Fe²⁺ in the form of FeSO₄ to the H₂SO₄ solution of a concentration of 1 mol/L during the electrochemical treatment increases the rate and efficiency of decontamination of the resin, which attains 98.4%. These results are comparable to those obtained using the H₂SO₄ solution of a concentration of 2 mol/L. The latter, in theory, will allow the use of solutions of H₂SO₄ of a lower concentration, which will reduce the economic expense and decrease the corrosion of equipment. The results obtained can serve as a basis for creating a technology for the decontamination of actual SIER polluted with iron oxide deposits.