The Experimental Study of Innovative Methods Regarding the Removal of Sm(III)

: The modern development of the construction materials sector determines the use of rare earth metals (REM) for various purposes. In particular, REM are added as basic alloying elements into magnesium alloys to increase alloy durability and strength. The complex systematic study of structural components and REM interaction are the basis for the phase state monitoring of multicomponent oxide polyfunctional materials. In addition, on the preparatory stage, layers with speciﬁed construction material coatings are formed. The paper presents experimental and theoretical results of studies of adsorptive bubble methods in the systems containing Samarium cations and surfactants, namely sodium dodecyl sulphate (NaDS). To identify the process mechanisms and prediction of optimal conditions of metal cations’ removal and separation by extraction, ﬂotation, and ion ﬂotation methods, one should know the pH of metal hydroxo-complexes and pH of the hydrate formation. The possibility of lanthanide ions’ removal (by the example of Samarium ions) by the solvent sublation method with NaDS as a collector and isooctyl alcohol as an extractant was studied. From the obtained experimental data, it was clear that the Sm 3+ removal in acidic mediums is practically non-existent. The results obtained in this paper are topical in the production of electrode coating components, welding ﬂuxes, sorbents for nuclear wastewater burial, wastewater treatment, highly porous heat-insulating and ﬁre-resistant materials, cement, and concrete with improved frost resistance.


Introduction
Russia has no less than 20% of world's REE (rare earth elements) reserves but the volume of the extraction of raw materials is only 2% of the world's extraction volume [1,2]. The production of products with REM in Russia is less than 1% of world's production volume [3][4][5].
Current Russian and foreign REM production techniques are rated for small-scale production. A special feature of available Russian raw material sources is the REM low content and complex chemicomineralogical composition. On the achieved technological level, processing of this type of raw materials is unprofitable [6][7][8]. The complex systematic study of the interaction of structural components in nitrate systems of lanthanides of the cerium family and the representatives of the Li, Na, and K chemical group established the formation of the representative class of Ln alkali coordination nitrates [9][10][11]. The findings form the basis for revealing and controlling the phase state of processing facilities in preparatory stages when forming construction material coating layers, as well as the determination of process and functional dependences for changing the composite material properties [12][13][14]. In addition, the studies conducted at Kola Peninsula, one of the most Current Russian and foreign REM production techniques are rated for small-scale production. A special feature of available Russian raw material sources is the REM low content and complex chemicomineralogical composition. On the achieved technological level, processing of this type of raw materials is unprofitable [6][7][8]. The complex systematic study of the interaction of structural components in nitrate systems of lanthanides of the cerium family and the representatives of the Li, Na, and K chemical group established the formation of the representative class of Ln alkali coordination nitrates [9][10][11]. The findings form the basis for revealing and controlling the phase state of processing facilities in preparatory stages when forming construction material coating layers, as well as the determination of process and functional dependences for changing the composite material properties [12][13][14]. In addition, the studies conducted at Kola Peninsula, one of the most developed Arctic regions in Russia, are of interest. Ores mined at the existing deposits may be used for the production of up to 30 different concentrates. Materials produced from local mineral deposits include metallic nickel; cobal; copper; titanium; niobium; rare earth metals; steel; sealants; electrode coating components and welding fluxes; sorbents for burial of nuclear wastes and wastewaters containing heavy non-ferrous metals and other pollutants; highly porous heat-insulating and fire-resistant materials; cement; and concrete with improved frost resistance [15,16].
The three methods of lanthanide cations removal are studied, namely ion flotation, solvent sublation, and extraction.
The work objective is an experimental and thermodynamic study of the possibility of selective REE removal (by the example of Sm +3 ) by adsorptive bubble methods.

Ion Flotation
According to data by foreign researchers, an increase of effectiveness in current technologies at the expense of accompanying extraction of valuable components from production wastes [7,8] is possible when using ion flotation methods [17] in the mining industry. The consequence of the decrease of REE toxicity and risk of damaging the environment is presumed. In papers [5][6][7], the ion flotation method is proposed for REE removal from apatite sulphuric acid processing products by different anion surfactants. At the production scale, the ion flotation process permits the preventing of sediment formation, REE loss, and usage of expensive extractants.
In particular, the ion flotation method is commercially used for the removal of non-ferrous, rare-earth, and radioactive metal cations from industrial and residential wastewaters [11]. In addition, when using different types of flocculants and coagulants, The three methods of lanthanide cations removal are studied, namely ion flotation, solvent sublation, and extraction.
The work objective is an experimental and thermodynamic study of the possibility of selective REE removal (by the example of Sm +3 ) by adsorptive bubble methods.

Ion Flotation
According to data by foreign researchers, an increase of effectiveness in current technologies at the expense of accompanying extraction of valuable components from production wastes [7,8] is possible when using ion flotation methods [17] in the mining industry. The consequence of the decrease of REE toxicity and risk of damaging the environment is presumed. In papers [5][6][7], the ion flotation method is proposed for REE removal from apatite sulphuric acid processing products by different anion surfactants. At the production scale, the ion flotation process permits the preventing of sediment formation, REE loss, and usage of expensive extractants.
In particular, the ion flotation method is commercially used for the removal of nonferrous, rare-earth, and radioactive metal cations from industrial and residential wastewaters [11]. In addition, when using different types of flocculants and coagulants, wastewater treatment for petroleum and oil impurities by the ion flotation method is possible [12]. When reaching certain conditions, the ion flotation process provides almost a 100% recovery of precious metals from solutions [18,19].
This work studies the distribution of Sm +3 ions in "water phase"-"froth phase" systems formed by standardized test solutions containing Sm 3+ ions and a surfactantsodium dodecyl sulphate. A diagram of the lanthanide flotation machine is shown in Figure 2. NaDS is used as one of the most common and well-studied surfactants. (CCM) is 8 × 10 −3 mol·kg −1 at 20 • C [1]. It is evident that this permits using solutions with a concentration below this value.
This work studies the distribution of Sm +3 ions in "water phase"-"froth phase" systems formed by standardized test solutions containing Sm 3+ ions and a surfactant-sodium dodecyl sulphate. A diagram of the lanthanide flotation machine is shown in Figure 2. NaDS is used as one of the most common and well-studied surfactants. (CCM) is 8•10 −3 mol•kg −1 at 20 °C [1]. It is evident that this permits using solutions with a concentration below this value. For reasons of the surfactant economy and achievement of the concentration effect, it is reasonable to use a minimum amount of collector, close to its stoichiometric consumption in accordance with the reaction: The chemically pure grade samarium nitrate hexahydrate was used. The initial concentration of samarium nitrate solution was 0.001 mol/L and the sodium dodecyl sulphate concentration was three times higher: 0.003 mol•L −1 or 0.864 g/L (DS -, dodecyl sulphate ion). The pH value of the solution was monitored by the "Anion 7010" ion meter with a glass electrode [18]. To find out the pH value of the solution, the nitric acid solution or sodium hydroxide solution were used.
The ion flotation process was conducted on the flotation machine ( Figure 2) [19]. In total, 200 mL of samarium nitrate solution with the concentration of 0.001 mol/L and dry NaDS were added to the cuvette. The process continued for no more than 5 min. The picked-out froth was broken by 5 mL sulphuric acid solution with the concentration of 1 mol•l −1 . The obtained solution (froth pulp) and the solution remained in the cuvette after flotation (chamber residue) and were analyzed for REE content by using the method in [20] and for dodecyl sulphate ion content by the potentiometer method [21,22].

Solvent Sublation
Solvent sublation is a method of surface separation combining the flotation of ions or molecules and a method of liquid extraction. The organic phase (in-out case that is isooctyl alcohol) was above the aqueous phase [17]. The process was implemented with small gas consumption. The method was used for wastewater treatment from organic impurities and for quantitative determination of trace metals and surfactants [23][24][25].
The feature of solvent sublation regarding the possibility of the concentration of multiple metal ions in a small volume of organic solvent shows the potential of this method for wastewater treatment containing metal ions for their subsequent recovery. It should be noted that currently available data regarding the organic phase nature, which are very limited [26,27], indicate that the organic phase ("trap") should have some polarity and should comply with basic requirements for an organic phase in solvent subla- For reasons of the surfactant economy and achievement of the concentration effect, it is reasonable to use a minimum amount of collector, close to its stoichiometric consumption in accordance with the reaction: The chemically pure grade samarium nitrate hexahydrate was used. The initial concentration of samarium nitrate solution was 0.001 mol/L and the sodium dodecyl sulphate concentration was three times higher: 0.003 mol·L −1 or 0.864 g/L (DS − , dodecyl sulphate ion). The pH value of the solution was monitored by the "Anion 7010" ion meter with a glass electrode [18]. To find out the pH value of the solution, the nitric acid solution or sodium hydroxide solution were used.
The ion flotation process was conducted on the flotation machine ( Figure 2) [19]. In total, 200 mL of samarium nitrate solution with the concentration of 0.001 mol/L and dry NaDS were added to the cuvette. The process continued for no more than 5 min. The picked-out froth was broken by 5 mL sulphuric acid solution with the concentration of 1 mol·L −1 . The obtained solution (froth pulp) and the solution remained in the cuvette after flotation (chamber residue) and were analyzed for REE content by using the method in [20] and for dodecyl sulphate ion content by the potentiometer method [21,22].

Solvent Sublation
Solvent sublation is a method of surface separation combining the flotation of ions or molecules and a method of liquid extraction. The organic phase (in-out case that is isooctyl alcohol) was above the aqueous phase [17]. The process was implemented with small gas consumption. The method was used for wastewater treatment from organic impurities and for quantitative determination of trace metals and surfactants [23][24][25].
The feature of solvent sublation regarding the possibility of the concentration of multiple metal ions in a small volume of organic solvent shows the potential of this method for wastewater treatment containing metal ions for their subsequent recovery. It should be noted that currently available data regarding the organic phase nature, which are very limited [26,27], indicate that the organic phase ("trap") should have some polarity and should comply with basic requirements for an organic phase in solvent sublation including: being less dense than water; minimum water solubility; and maximum capacity of sublate accumulation. Nowadays, many authors of conducted studies showed that during solvent sublation, the substance distribution is determined by its ability to adsorb on bubble walls, passing through the solution, and it does not depend on the phase volume relationship. Thereby, the sublate adsorption process is the determining factor of the process.
Compared to the foam separation method, the process of solvent sublation is poorly studied. Originally, solvent sublation was proposed for ion removal by the surfactant and afterwards the process was realized for dissolved substance removal based on their surface activity and sediment flotation [19,28,29].
Additionally, there is a carrier agent for the colligand in solvent sublation surfactants. An important property of this method is its high selectivity. In the flotation method, most dissolved impurities go into the froth, while in solvent sublation, one can achieve such a separation, at which the substance partially goes into the organic phase and partially returns. It should be noted that with foam separation, water is also removed from the solution together with the isolated substance. First, this reduces the concentration ratio of the substance. Second, in the foam separation method, water removal results in rapid floating solution consumption and in the end, prevents from making a total curve during the experiment with one initial solution. In solvent sublation, this is not the case, as water always returns to the aqueous phase. Despite all advantages, the solvent sublation method has disadvantages: (1) it is not always possible to select a solvent that could dissolve the formed sublate and (2) both the formation of aqueous emulsion in the organic phase is possible and the contamination of this organic phase by undesirable ingredients from the aqueous solution is possible [1].
In the solvent sublation process, a glass column was used [1]. In total, 100 mL of Sm(NO 3 ) 3 (chemically pure grade samarium nitrate hexahydrate) and 5 mL of 2-octanol were added into the column. Nitrogen was fed through the glass filter at the base of the column. The process time was 2 h.

Extraction
Extraction processes are currently the basic practice in REM separation. In industry practice, tributyl phosphate, DEHPA, carboxylic acids, and ammonium base salts are mainly used for lanthanide separation [30].
Separation is based on the regular change in distribution coefficient (D) values in the lanthanide series ( Figure 3). tion including: being less dense than water; minimum water solubility; and maximum capacity of sublate accumulation. Nowadays, many authors of conducted studies showed that during solvent sublation, the substance distribution is determined by its ability to adsorb on bubble walls, passing through the solution, and it does not depend on the phase volume relationship. Thereby, the sublate adsorption process is the determining factor of the process.
Compared to the foam separation method, the process of solvent sublation is poorly studied. Originally, solvent sublation was proposed for ion removal by the surfactant and afterwards the process was realized for dissolved substance removal based on their surface activity and sediment flotation [19,28,29].
Additionally, there is a carrier agent for the colligand in solvent sublation surfactants. An important property of this method is its high selectivity. In the flotation method, most dissolved impurities go into the froth, while in solvent sublation, one can achieve such a separation, at which the substance partially goes into the organic phase and partially returns. It should be noted that with foam separation, water is also removed from the solution together with the isolated substance. First, this reduces the concentration ratio of the substance. Second, in the foam separation method, water removal results in rapid floating solution consumption and in the end, prevents from making a total curve during the experiment with one initial solution. In solvent sublation, this is not the case, as water always returns to the aqueous phase. Despite all advantages, the solvent sublation method has disadvantages: (1) it is not always possible to select a solvent that could dissolve the formed sublate and (2) both the formation of aqueous emulsion in the organic phase is possible and the contamination of this organic phase by undesirable ingredients from the aqueous solution is possible [1].
In the solvent sublation process, a glass column was used [1]. In total, 100 mL of Sm(NO3)3 (chemically pure grade samarium nitrate hexahydrate) and 5 mL of 2-octanol were added into the column. Nitrogen was fed through the glass filter at the base of the column. The process time was 2 h.

Extraction
Extraction processes are currently the basic practice in REM separation. In industry practice, tributyl phosphate, DEHPA, carboxylic acids, and ammonium base salts are mainly used for lanthanide separation [30].
Separation is based on the regular change in distribution coefficient (D) values in the lanthanide series ( Figure 3). It was discovered that extraction removal was conducted at the expense of samarium (III) cations and Sm(OH) 2+ moving into the organic phase. A shortcoming of this method is that the process does not flow at pH < 4, though in practice valuable compo- It was discovered that extraction removal was conducted at the expense of samarium (III) cations and Sm(OH) 2+ moving into the organic phase. A shortcoming of this method is that the process does not flow at pH < 4, though in practice valuable components need to be recovered from acid mediums. Thus, the extraction process in solutions containing samarium ions with NaDS at pH = 3.0-6.0 was studied. Dry sodium dodecyl sulphate and chemically pure grade samarium nitrate hexahydrate were used. The studied metal cation solution in the volume of 200 mL was placed into the 250 mL beaker. Next, dry sodium dodecyl sulphate was added up to the concentration of 0.003 M.
By partial addition of the NaOH 0.95 N solution or H 2 SO 4diluted , the pH value was adjusted to the required value. Then, 5 mL of isooctyl alcohol was added. The obtained solution was stirred by the agitator ES-8300 D at approximately 700 RPM.

Results of the Ion Flotation Method
The results of the ion flotation study of the solutions containing Sm +3 иDS − are shown in Table 1. From the obtained experimental data, it is evident that the Sm 3+ removal in acidic mediums is practically non-existent. With the increase of the pH value from 3.5 to 6.0, the distribution coefficient was approximately 16. Not surprisingly, in this pH range, neutral and basic dodecyl sulphates of samarium Sm(C 12 H 25 OSO 3 ) 3 иSm(OH)(C 12 H 25 OSO 3 ) 2 floats. From the obtained experimental data, it is evident that at a pH exceeding 6.0, the distribution coefficient (K p ) increases rapidly. This value is lower than that previously determined by us through the pH of the hydrate formation (Formula (3). On this basis, it may be considered that in the pH range satisfying the maximum removal, samarium floats mainly in the hydroxide form, with which DS − anions form hydrogen bonds with the admixture of neutral and basic dodecyl sulphate.
According to the literature data, in the process of the ion flotation of metal cations, the increase in removal ratio occurs in the pH range of the hydrate formation [29] and notable cations go into the froth in the form of hydroxides. It is assumed that ion flotation non-ferrous metals flow with the formation of their basic salts with anion surfactants. A hypothesis was put forward based on a thermodynamic analysis of ion-molecular equilibriums that cerium (3+) is extracted at pH = 5 by oleic and naphthenic acid solutions in diluents in the form of basic oleates and naphthenates, and yttrium in the form of neutral salts [30]. To identify the process mechanisms and predictions of optimal conditions of metal cations removal and separation by extraction, flotation, and ion flotation methods, one should know the pH of metal hydroxo-complexes and pH of the hydrate formation that can be calculated based on the Gibbs energies of hydroxo-complexes and metal hydroxides formation. The pH value of the Sm(OH) 2+ hydroxo-complexes formation can be calculated based on the expression for instability constants: Appl. Sci. 2021, 11, 7726 6 of 12 The pH value of hydrate formation is calculated by the formula: where L is the product of hydroxide solubility; C is the samarium cation concentration; and γ ± is the salt average ion activity coefficient. Although the Gibbs energy value for Sm(OH) 3 formation is −1281.56 ± 3.77 kJ/mol, in [32,33], this value is missing. The Gibbs energy value of Sm(OH) 2+ hydrate formation is −859.95 kJ/mol, available in [32], which disagrees with the value of −848.10 ± 3.35 kJ/mol as specified in [33]. Due to the poor accuracy of values available in the literature data, the pH evaluation of complex formation and hydrate formation by the conductometric titration method was attempted with subsequent calculation of thermodynamic quantities.
Conductometric titration was carried out as follows: 10 mL aliquots of Sm(NO) 3 solution with the concentration of 0.001 mol·kg −1 , acidified by nitric acid down to pH = 3 (approximately), were titrated with 0.002 N solution of NaOH. After the addition of each portion of 1-2 mL alkali solution, the solution was agitated until the establishment of the constant value of specific electrical conductivity, measured by the "Anion 4100" conductometer. At the same time, the pH value was measured by the "Anion 7010" ion meter. After the results, the titration curve was plotted as shown in Figure 4.
Appl. Sci. 2021, 11, x FOR PEER REVIEW 6 of 12 droxides formation. The pH value of the Sm(OH) 2+ hydroxo-complexes formation can be calculated based on the expression for instability constants: The pH value of hydrate formation is calculated by the formula: where L is the product of hydroxide solubility; C is the samarium cation concentration; and γ± is the salt average ion activity coefficient. Although the Gibbs energy value for Sm(OH)3 formation is −1281.56 ± 3.77 kJ/mol, in [32,33], this value is missing. The Gibbs energy value of Sm(OH) 2+ hydrate formation is −859.95 kJ/mol, available in [32], which disagrees with the value of −848.10 ± 3.35 kJ/mol as specified in [33]. Due to the poor accuracy of values available in the literature data, the pH evaluation of complex formation and hydrate formation by the conductometric titration method was attempted with subsequent calculation of thermodynamic quantities.
Conductometric titration was carried out as follows: 10 mL aliquots of Sm(NO)3 solution with the concentration of 0.001 mol•kg −1 , acidified by nitric acid down to pH = 3 (approximately), were titrated with 0.002 N solution of NaOH. After the addition of each portion of 1-2 mL alkali solution, the solution was agitated until the establishment of the constant value of specific electrical conductivity, measured by the "Anion 4100" conductometer. At the same time, the pH value was measured by the "Anion 7010" ion meter. After the results, the titration curve was plotted as shown in Figure 4. By analyzing these relationships, we see that at pH = 5.3, there was a break in the curve of the specific electrical conductivity as a function of the added alkali with a transition to an almost horizontal part, which shows the added hydroxyl anions' fixation into poorly dissociated compounds. As the formation of hydroxides was not observed (optical density of solutions did not change), this part was responsible for the formation of hydroxo-complexes. By the quantity of milliequivalents of alkali used here, one can determine that the process flows until the formation of Sm(OH) 2+ monohydroxo-complexes. The specified pH value was taken as the pH of the complex formation onset of pHcompl. Upon the completion of the complex formation, a near-linear growth of electrical conductivity with the addition of alkali was observed. At pH = 6.49, the growth of electrical conductivity stops. This part of the titration curve corresponds to the hydroxide sedimentation. The latter was observed visually and confirmed by an increase in the optical density of solutions. By analyzing these relationships, we see that at pH = 5.3, there was a break in the curve of the specific electrical conductivity as a function of the added alkali with a transition to an almost horizontal part, which shows the added hydroxyl anions' fixation into poorly dissociated compounds. As the formation of hydroxides was not observed (optical density of solutions did not change), this part was responsible for the formation of hydroxocomplexes. By the quantity of milliequivalents of alkali used here, one can determine that the process flows until the formation of Sm(OH) 2+ monohydroxo-complexes. The specified pH value was taken as the pH of the complex formation onset of pH compl . Upon the completion of the complex formation, a near-linear growth of electrical conductivity with the addition of alkali was observed. At pH = 6.49, the growth of electrical conductivity stops. This part of the titration curve corresponds to the hydroxide sedimentation. The latter was observed visually and confirmed by an increase in the optical density of solutions.
The quantity of milliequivalents of alkali used here meets the following reaction: Sm(OH) 2+ + OH -= Sm(OH) 3 .
The pH value corresponding to the horizontal part of the titration curve was taken as the pH of hydrate formation pH hydr . Furthermore, on the titration curve, the near-linear growth of the specific electrical conductivity was observed because of the excess alkali.
The obtained calculated values are shown in Table 2. The obtained Gibbs energy value of the Sm(OH) 3 formation agrees well with the database [32], in which the value of −1281.56 ± 3.77 kJ/mol is specified ( Table 2). The Gibbs energy value of samarium hydroxo-complex differs greatly from literature data, namely from −848.10 ± 3.35 [32] and −859.95 [33]. We calculated the values of Sm(OH) 2+ hydroxo-complex instability constants according to data from [32,34] and calculated the values 8.4 × 10 −6 and 3.47 × 10 −7 , corresponding to the pH of the complex formation onset by Formula (2), equal to 8.0 and 6.7. These values, however, were higher than the pH values of the hydrate formation that we determined and calculated based on ∆ f G 0 298 Sm(OH) 3 from the reference book [34]. This is contradictory as the formation of hydroxocomplexes should carry at a pH below the pH of the hydrate formation and precede the hydroxide precipitation.

Solvent Sublation Results
The Sm +3 ions' content in the organic phase was determined from the concentration difference between the initial solution and aqueous phase [26].
The samarium ions' distribution coefficient during solvent sublation was calculated by the formula: K p = C org /C aq [1]. The results of the experimental study of the diluted aqueous solutions containing Sm(NO 3 ) 3 Tables 3 and 4.  Table 4. Recovery ratio α and distribution coefficient of samarium (III) (process duration was 120 min and C 0 = 0.001 mol/L). From the obtained data, it is evident that when the process time lies between 5 and 10 min, the Sm +3 removal is more intense than by further floating. As a result, one can find an optimal solvent sublation process time in the REE nitrate solutions with the initial concentration of 0.001 mol/L. Depending on the solution pH, it is 10 min and higher.

and a surfactant are shown in
In time, the concentration of the studied REE ions asymptotically approaches some finite value, which is typical for the system moving into the stationary state, in which the equilibrium between the processes of lanthanide adsorption and desorption is established.
At pH = 5.0-6.0, the process of solvent sublation removal moves into a stationary mode with high equilibrium concentrations. The maximum recovery ratio was approximately 25%. In this pH range, the formation of monohydroxyo-complexes begins.
At pH = 6.8-8.0, the equilibrium concentration lowers and the recovery ratio increases, and an upward trend in the process rate was observed. The K p value and α reach maximum values. An explanation of the observed patterns is possible based on the consideration of diffusing particle forms at different pH values. In the aqueous solution at the pH range from 4.8 to 6.1, the formation of lanthanide monohydroxo-complexes occurs; at pH = 6.1-6.5, dihydroxo-complexes are formed; and at the pH range from 6.5 to 7.5, the formation of hydroxides occurs. At a pH exceeding 7.4, lanthanides in the aqueous phase are in the form of Ln(OH) 2 (C 12 H 25 OSO 3 ) organic complexes because otherwise the settling of the hydroxide sediment would occur, which was not observed. The limiting stage of the lanthanide and yttrium removal process is the diffusion of organic complexes and because of their large size, it flows slowly, the rate constant decreased by an order.
Thus, depending on the pH of the aqueous phase, the forms of dodecyl sulphate and samarium present in the aqueous phase change.

Extraction Results
In this paper, the possibility of using sodium dodecyl sulfate for the removal of Sm3+ by extraction with isooctyl alcohol is studied ( Figure 5). The 0.001 M standard test solutions of Sm 3+ nitrates were used.
find an optimal solvent sublation process time in the REE nitrate solutions with the initial concentration of 0.001 mol/L. Depending on the solution pH, it is 10 min and higher.
In time, the concentration of the studied REE ions asymptotically approaches some finite value, which is typical for the system moving into the stationary state, in which the equilibrium between the processes of lanthanide adsorption and desorption is established.
At pH = 5.0-6.0, the process of solvent sublation removal moves into a stationary mode with high equilibrium concentrations. The maximum recovery ratio was approximately 25%. In this pH range, the formation of monohydroxyo-complexes begins.
At pH = 6.8-8.0, the equilibrium concentration lowers and the recovery ratio increases, and an upward trend in the process rate was observed. The Kp value and α reach maximum values. An explanation of the observed patterns is possible based on the consideration of diffusing particle forms at different pH values. In the aqueous solution at the pH range from 4.8 to 6.1, the formation of lanthanide monohydroxo-complexes occurs; at pH = 6.1-6.5, dihydroxo-complexes are formed; and at the pH range from 6.5 to 7.5, the formation of hydroxides occurs. At a pH exceeding 7.4, lanthanides in the aqueous phase are in the form of Ln(OH)2(C12H25OSO3) organic complexes because otherwise the settling of the hydroxide sediment would occur, which was not observed. The limiting stage of the lanthanide and yttrium removal process is the diffusion of organic complexes and because of their large size, it flows slowly, the rate constant decreased by an order.
Thus, depending on the pH of the aqueous phase, the forms of dodecyl sulphate and samarium present in the aqueous phase change.

Extraction Results
In this paper, the possibility of using sodium dodecyl sulfate for the removal of Sm3+ by extraction with isooctyl alcohol is studied ( Figure 5). The 0.001 M standard test solutions of Sm 3+ nitrates were used. The extraction was conducted for 30 min. Aqueous and organic phases were separated in separate funnels of 0.25 or 0.5 L in capacity. Phase separation occurred over 3 to 5 days. The aqueous phase was analyzed by a photometric method for REE cations content. The form of salts extracted to the organic phase was determined by the IR spectroscopy method [35].  The extraction was conducted for 30 min. Aqueous and organic phases were separated in separate funnels of 0.25 or 0.5 L in capacity. Phase separation occurred over 3 to 5 days. The aqueous phase was analyzed by a photometric method for REE cations content. The form of salts extracted to the organic phase was determined by the IR spectroscopy method [35].
Sodium dodecyl sulphate (NaDS) is insoluble in non-polar solvents and, moreover, it is practically insoluble in alcohols. In this study, sodium dodecyl sulphate was added to the aqueous phase and isooctyl alcohol (C 8 H 18 O, 2-ethyl-1-hexanol) was used as an extractant.
During the experiment, it was discovered that NaDS goes to into the organic phase in the form of Ln(C 12 H 25 OSO 3 ) 3 solvates. Solubility can be explained by the polar group orientation towards the cation and solvate screening from the outer side by non-polar radicals. Apparently, alcohol molecules interact with REE cations as well, which confirms the stretching frequency ν o-н shift and the lack of lanthanide dodecyl sulphate dissolution in non-polar solvents [35].
Certain experiments showed that rare earth elements are poorly extracted by alcohol in the absence of NaDS. When extracting holmium (III) cations at pH = 6.0, K distr was 4.46, whereas in the presence of sodium dodecyl sulphate, it was 360. Thus, isooctyl alcohol is an extractant, while NaDS acts as a carrier agent. Thus, the proposed extraction technique in the system, namely sodium dodecyl sulphate-lanthanide salt aqueous solution-isooctyl alcohol, significantly increases K distr in the studied solutions. Figure 6 shows the results of the experimental study of samarium (III) extraction. The initial concentration of REE was 0.001 M and the sodium dodecyl sulphate concentration corresponded to the chemical reaction (1) stoichiometry and was 0.003 M. The organic phase volume (V org ) was 5 mL and aqueous phase volume (V aq ) was 200 mL, i.e., the ratio V org :V aq = 1:40.
During the experiment, it was discovered that NaDS goes to into the organic phase in the form of Ln(C12H25OSO3)3 solvates. Solubility can be explained by the polar group orientation towards the cation and solvate screening from the outer side by non-polar radicals. Apparently, alcohol molecules interact with REE cations as well, which confirms the stretching frequency νо-н shift and the lack of lanthanide dodecyl sulphate dissolution in non-polar solvents [35].
Certain experiments showed that rare earth elements are poorly extracted by alcohol in the absence of NaDS. When extracting holmium (III) cations at pH = 6.0, Kdistr was 4.46, whereas in the presence of sodium dodecyl sulphate, it was 360. Thus, isooctyl alcohol is an extractant, while NaDS acts as a carrier agent. Thus, the proposed extraction technique in the system, namely sodium dodecyl sulphate-lanthanide salt aqueous solution-isooctyl alcohol, significantly increases Kdistr in the studied solutions. Figure 6 shows the results of the experimental study of samarium (III) extraction. The initial concentration of REE was 0.001 M and the sodium dodecyl sulphate concentration corresponded to the chemical reaction (1) stoichiometry and was 0.003 M. The organic phase volume (Vorg) was 5 mL and aqueous phase volume (Vaq) was 200 mL, i.e., the ratio Vorg: Vaq = 1: 40. During the extraction, the dependence of Kdistr from pH was weak and Sm 3+ has the maximum Kdistr at pH = 5.0. The distribution coefficient is significantly higher than when extracting by carboxylic acids. Removal from acidic mediums is possible. Table 5 shows the results of the Sm 3+ extraction with different initial concentrations at pH = 4.0. According to the extractant efficiency series, as shown in Table 6, one can come to the conclusion that sodium dodecyl sulphate has the most negative Gibbs energy of solvation ΔSG о 298 and correspondingly the maximum Kdistr. In addition, it was discovered During the extraction, the dependence of K distr from pH was weak and Sm 3+ has the maximum K distr at pH = 5.0. The distribution coefficient is significantly higher than when extracting by carboxylic acids. Removal from acidic mediums is possible. Table 5 shows the results of the Sm 3+ extraction with different initial concentrations at pH = 4.0. According to the extractant efficiency series, as shown in Table 6, one can come to the conclusion that sodium dodecyl sulphate has the most negative Gibbs energy of solvation ∆ S G o 298 and correspondingly the maximum K distr . In addition, it was discovered that when saturating isooctyl alcohol with sodium dodecyl sulphate, the spectrum remained unchanged, which demonstrates NaDS insolubility in alcohol [35].

Conclusions
It is well known that rare earth elements are scattered in nature and do not manifest themselves in elementary states or even in the form of individual rare earth compounds.
They usually exist in rocks such as basalt, granite, gneiss, shale, and silicates in the form of mixed rare earth compounds forming various types of rare earth minerals. In general, most of these elements are mainly found in each type of rare earth mineral, but the distribution differs significantly between different minerals (Kanazawa and Kamitani, 2006). Therefore, to date, about 250 rare earth minerals have been found in more than 30 countries and regions. As a result of the low concentration, rare earth elements are formed as a by-product during the processing of various ores or are extracted from processed tailings or residues [36][37][38][39][40][41].
Considering the indispensable role of rare earth elements in the field of modern high technology, the efficient exploitation and utilization of rare earth resources is of great importance.
It should be noted that the removal of samarium ions from aqueous standard test solutions are by adsorption bubble methods, namely ion flotation, extraction, and solvent sublation.
In the processes under consideration, in our opinion, an interesting result is that the forms of the extracted components, namely Sm (OH) 2 (C 12 H 25 OSO 3 ) and Sm (OH)(C 12 H 25 OSO 3 ) 2 , were found at different pH values of the researched solutions.
The experimental results obtained during the conducted studies show that in the process of ion flotation, the maximum extraction of Sm (+3) occurs at pH = 6.7. In the SS-max method, extraction can be achieved at pH = 8.0 and in the extraction method at pH = 5.0.
In addition, it was experimentally proven that Sm +3 distribution coefficients for ion flotation and solvent sublation with sodium dodecyl sulphate are significantly higher than for the extraction process.
Thus, we believe that, depending on the studied samples obtained during a certain treatment of minerals containing samarium cations, it is possible to use various adsorptionbubble methods for extracting REE.
The results obtained in this paper could be topical in the production of welding fluxes, sorbents for nuclear waste burial, wastewater treatment, highly porous heat-insulating and fire-resistant materials, cement, and concrete.