Synergistic Effect of Dielectric Barrier Discharge Plasma and TiO 2 -Pillared Montmorillonite on the Degradation of Rhodamine B in an Aqueous Solution

: Photocatalytic, plasma and combined plasma – photocatalytic processes were applied for the destruction of a model pollutant, Rhodamine B dye, in an aqueous solution (concentration of 40 mg/L). For this purpose TiO 2 -pillared montmorillonite was used as a photocatalyst (characterized by X-ray analysis and low-temperature nitrogen adsorption/desorption). It was prepared by the method of intercalation of titanium hydroxocomplexes, including hydrothermal activation of the process and preliminary mechanical treatment of the layered substrate. The dielectric barrier discharge (DBD) plasma in the presence of photocatalysts increases the efficiency of dye degradation (100%, 8 s) compared to plasmolysis (94%) and UV photolysis (92%, 100 min of UV irradiation); in contrast to photolysis, destructive processes are more profound and lead to the formation of simple organic compounds such as carboxylic acids. The plasma – catalytic method enhances by 20% the energetic efficiency of the destruction of Rhodamine B compared to DBD plasma. The efficiency of dye destruction with the plasma – catalytic method increases with the improvement of the textural properties of the photocatalyst. weak peaks of both anatase (at 2θ = 25.3° , 47.8° and 54.4°) and rutile (at 2θ = 27.7°), whereas in the case of the TiO 2 -PMMH and TiO 2 -PAMMH samples these peaks were significantly sharper and more intense; moreover the anatase peak at 2θ = 37.7° bec ame visible as well. These results demonstrated that in the preparations of photocatalysts by the methods II and III the TiO 2 pillars crystallized in the anatase and rutile phases much more readily; the TiO 2 crystallite sizes were evaluated as 7 nm and 11 nm, respectively. The montmorillonite peaks in the TiO 2 PAMMH case nearly disappeared. This fact indicates amorphization of the montmorillonite structure as a result of mechanical treatment.


Introduction
Purification of natural water resources from organic dyes due to their resistance to decomposition processes [1] is a problem of topical interest [2][3][4][5]. Conventional treatment technologies such as biological, physical and chemical methods [6][7][8][9][10] are neither cheap nor provide the required efficiency. Recently, special attention has been paid to advanced oxidative process (AOP) technologies, the use of which allows for the decomposition of pollutants into less toxic products with the processes of destruction occurring at high rates, which is a significant advantage [11][12][13].
One of the possible ways to intensify wastewater treatment processes is the dielectric barrier discharge (DBD), which has already found wide application in environmental protection systems [14][15][16]. High purification efficiency can be achieved by combining plasma-chemical and photocatalytic purification methods with the observation of a synergistic effect [17][18][19] while source: https://doi.org/10.7892/boris.144772 | downloaded: 4.11.2020 reducing energy costs [20]. In this case, radiation quanta enhance the oxidation processes due to the formation of additional active particles, such as, for example, those in the TiO2 photocatalyst-plasma system [21,22]:  (8) where e − + h + are the electron-hole pairs formed on the surface of the catalyst. Moreover, a synergistic effect may arise due to the promotion of the photocatalyst, which consists in assumed inhibition of the recombination of e -+ h + pairs on the surface of TiO2 and continuous photocatalyst regeneration under DBD [23].
The presence of an intense UV component of the DBD plasma [24] simplifies the approaches to the selection of effective photocatalysts. In particular, for the most common TiO2 photocatalysts, in this case, it is not urgent to reduce the width of the forbidden zone by doping to shift the working radiation range to the visible region, which is essential when using only the photocatalytic purification method. Therefore, the best choice for the plasma-catalytic purification method is applying the advanced catalytic systems based on titanium oxide [25,26], in particular, its nanoscale forms [27].
However, the use of nanoparticles of pure TiO2 is hindered by some limitations such as low adsorption capacity and the possibility of particle agglomeration, which reduce its photocatalytic efficiency for the processes of purifying water from pollutants of organic origin. To overcome these limitations, titanium dioxide nanoparticles are distributed on mineral carriers such as natural clay minerals [28], particularly montmorillonite (MM) [29]. The TiO2-pillared montmorillonite possesses a highly developed specific surface area and exhibits high activity in various photocatalytic processes, including photolysis of organic dyes [30]. Recently we proposed and successfully applied a new approach to the synthesis of TiO2-pillared montmorillonite with a high degree of crystallinity for the TiO2 pillars (nanocrystals) representing a mixture of the anatase and rutile phases, and with improved adsorption and photocatalytic activities as a result of hydrothermally activated intercalation of titanium polyhydroxocomplexes [31]. Moreover, when obtaining TiO2-pillared MM, along with hydrothermal activation of the intercalation of titanium polyhydroxocomplexes we have used preliminary mechanical treatment of the original substrate [32]. This allowed for a significant improvement of the textural characteristics, in particular, a specific surface area and porosity of pillared materials due to a decrease in the size of MM particles during mechanical processing, and, therefore, an increase in the area of the interphase boundary through which ion exchange occurs.
Among the various dyes used in various fields of business activity, Rhodamine B has found wide application in the textile and food industries [33], in laser technology [34], and also used as a biomarker and molecular probe [35,36], electrochemical luminescent sensitizer [37], and also it is a sensitizer in combination with metal oxides in solar panels [38]. Rhodamine B refers to toxic compounds that have an irritating effect on the mucous membranes and skin. This dye has carcinogenic properties, exhibits neurotoxic effects and has a chronic toxic effect on aquatic organisms and humans [39]. Thus, the purification of water bodies from Rhodamine B is an urgent task to protect the environment and human health. This paper presents the results of studying the destruction of Rhodamine B in a combined plasma-photocatalytic process using TiO2-pillared montmorillonite as a photocatalyst. The effects of various factors, such as discharge characteristics (current power and frequency), processing time and textural properties of the photocatalyst, on the purification process are assessed.

X-ray Diffraction, Textural Characterization and Particle Size Distribution
The characterization of the photocatalysts is discussed in the following. The photocatalysts were prepared as detailed below in Section 3.2.1. Throughout the text the following nomenclature for the samples was used: montmorillonite-MM; activated montmorillonite-AMM; TiO2-pillared montmorillonite-TiO2-PMM (method I); TiO2-pillared hydrothermally treated montmorillonite-TiO2-PMMH (method II) and TiO2-pillared hydrothermally treated and activated montmorillonite-TiO2-PAMMH (method III).
The original matrices and pillared materials were characterized by X-ray diffraction (XRD), see Figure 1. X-ray analysis was performed using an X-ray diffractometer Bruker D8 Advance (Bruker AXS GmbH, Karlsruhe, Germany). The average crystallite size of the TiO2 photoactive phase, anatase, was evaluated using the Scherrer's method [40]. The pillared samples were characterized by peaks corresponding to the montmorillonite (2θ = 19.8° and 35.6°) and cristobalite (2θ = 21.7°) phases. The latter was a secondary product, which was formed in synthetic conditions with a low pH value of the medium. The diffractogram of the TiO2-PMM samples shows broad and weak peaks of both anatase (at 2θ = 25.3°, 47.8° and 54.4°) and rutile (at 2θ = 27.7°), whereas in the case of the TiO2-PMMH and TiO2-PAMMH samples these peaks were significantly sharper and more intense; moreover the anatase peak at 2θ = 37.7° became visible as well. These results demonstrated that in the preparations of photocatalysts by the methods II and III the TiO2 pillars crystallized in the anatase and rutile phases much more readily; the TiO2 crystallite sizes were evaluated as 7 nm and 11 nm, respectively. The montmorillonite peaks in the TiO2-PAMMH case nearly disappeared. This fact indicates amorphization of the montmorillonite structure as a result of mechanical treatment.
Low-temperature nitrogen adsorption-desorption isotherms and pore size distributions of the samples are shown in Figure 2. Samples were investigated on a specific surface and porosity analyzer ASAP 2020 (Micromeritics Instrument Corp., Norcross, GA, U.S.A.). Prior to the measurements, the samples were degassed at 180 °C and a reduced pressure of 5-10 Pa for 3.5 h. All the isotherms were characterized by the presence of capillary condensation hysteresis loops and belonged to type IV according to International Union of Pure and Applied Chemistry (IUPAC) classification [41], which is typical for materials with a mesoporous structure. Furthermore, the shape of the hysteresis loop for these isotherms is of type H3 according to IUPAC [42], indicating the presence of long slit-shaped and plane-parallel pores in the obtained pillared materials.
The values of specific surface area according to Brunauer-Emmett-Teller (BET) theory (SBET) and total pore volume (ΣVpore; by the Barrett-Joyner-Halenda (BJH) method) are shown in Table 1, revealing that the process of pillaring led to significant increases in a specific surface area and total pore volume compared to the pristine MM. SBET, BET specific surface area; ∑Vpore, total pore volume; Dav, BJH adsorption average pore diameter.
As seen from Table 1, the treatment by methods II and III caused a decrease in a specific surface area and an increase in the total pore volume compared to the treatment by method I.
Pore size distribution curves are shown in Figure 2b. The distribution pattern for the TiO2-PMM sample was narrow and unimodal. The TiO2-PMMH and TiO2-PAMMH samples featured a shift of the distribution curve to larger pore sizes and the broadening of its shape. Furthermore, as seen in Figure 2b, the TiO2-PMMH and TiO2-PAMMH samples already demonstrated two peaks. This is due to aggregation processes in the interlayer space of MM activated under hydrothermal conditions. The growth of pillars can also be explained by Ostwald ripening, i.e., relatively small TiO2 pillars dissolve in water followed by reprecipitation at large pillars.
The particle size distribution in an aqueous suspension was measured by static light scattering using an Analysette 22 Compact laser diffraction analyzer (FRITSCH GmbH, Idar-Oberstein, Germany), see Figure 3. The mechanical pretreatment of pristine montmorillonite allows one (i) to enhance textural characteristics, in particular, to substantially increase the specific surface area (Table  1) and (ii) causes a significant change in its particle size in an aqueous suspension. According to the dynamic light scattering data of pristine MM (Figure 3a), there are three particle fractions: 0.1-0.2 μm, 0.4-0.6 μm (most abundant) and 3-4 μm. Mechanical treatment (Figure 3b) results in a practically monofractional composition with an average particle size of about 0.1 μm. The overall decrease in the AMM particle size plays presumably a key role in increasing its cation exchange capacity, which is especially important during the intercalation and further formation of the pillared structure.

Photolytic and Plasmolytic Characterization
Kinetics and efficiency of the RhB destruction in the photolysis and plasmolysis processes are shown in Figures 4 and 5, respectively. From these figures, it can be seen that the destruction of Rhodamine B was significantly more efficient when using the combined plasma-catalytic process. Note that both in photocatalytic and combined plasma-catalytic processes the dye destruction efficiency increased successively in the series of photocatalysts TiO2-PMM, TiO2-PMMH and TiO2-PAMMH. This is primarily due to an increase in the total pore volume and the size of the TiO2 crystallites (Table 1), which determines the e -+ h + pair regeneration rate [43].   (2), TiO2-PMMH (3) and TiO2-PAMMH (4). Processing conditions: carrier gas flow rate is 0.5 L/min, the discharge current is 3.2 mA, and discharge current frequency is 500 Hz; discharge power is 20 W/cm 3.
The photocatalytic experimental data are processed using the first-order kinetic model [44]. In order to accurately compare the rate constants with the plasmolysis processes, we proceeded from the following suppositions. Experimental data describing the kinetic regularities in DBD plasma in the most common form can be expressed in terms of cylindrical coordinates: where z and r are the longitudinal and radial coordinates, respectively; ni is the initial, the concentration of RhB, V is the linear flow rate, Di is the diffusion coefficient and W is the rate of RhBrelated chemical processes. The characteristic value of the diffusion coefficient (D) for organic compounds in water was 10 −5 cm 2 /s [45]. Characteristic processing times were 10 s for DBD and 6000 s for photocatalytic processes, whereas for diffusion processes they amounted to 10 7 s. Therefore, diffusion processes could be neglected in the considered systems. Assuming that RhB in the processes under study was subject to destruction, the change in the concentration of the dye in the solution could be described by the equation: where na and Wa are the average concentration and the average RhB decomposition rate, respectively.   (12) where r1 and r2 are the external and internal radii of the fluid layer.
For boundary conditions na = nin(z = 0) and the assumption that the RhB decomposition rate is described by a first-order kinetic equation and is an irreversible process, Equation (10)  where nin is the initial concentration of the dye in the solution, µmol/L, K is the rate constant, s -1 , and t is the processing time, s. Effective rate constants for the three studied processes are presented in Table 2. *-in energetic efficiency calculations the power expended in the process of RhB destruction was assumed to be 0.25 kW and 0.02 kW for the photocatalytic and plasma-catalytic processes, respectively. **-efficiency of RhB destruction is less than 50%.
From Table 2 it can be seen that the RhB degradation rate constant was significantly smaller in the photocatalytic process compared to DBD plasma. Comparison of the effect of photocatalysts on the rate of destruction shows that for both purely photocatalytic process and combined plasmacatalytic process, the catalytic effect increased in the series TiO2-PMM, TiO2-PMMH and TiO2-PAMMH. Note that rate constants for the photocatalytic processes of RhB decomposition with our catalytic materials were significantly larger than those known in the literature: (0.8-1.6)·10 -3 s -1 [46].
Evaluation of the energy cost of RhB destruction (Y50%, g/(kW·h), Table 2) was carried out according to the following equation [47]: 50 % , 100 where Ci is the initial concentration of the dye in the solution, g/L; V is the volume of the treated solution, L; P is the power expended in the process of destruction, kW, and t is the processing time, h. Table 2 shows that the energetic efficiency decreased with an increasing degree of RhB degradation ( Figure 6), which was associated with a decrease in the concentration of the dye, and also the reduced probability of an interaction of active particles formed in the solution and UV photons with RhB and intermediate products of its decomposition. The obtained results suggest a possible reduction in energy consumption when using a combined plasma-photocatalytic effect. To this end, we studied the effect of the discharge current frequency on the expended power in the discharge and the efficiency of the RhB decomposition, as shown in Figure 7. As can be seen from the data presented in Figure 7, at current frequencies above 1500 Hz the discharge burning conditions were met, allowing for the complete removal of the dye from aqueous solutions. It should be noted that the presence of photocatalysts in the system greatly reduced the energy consumption while maintaining the high degrees of degradation. Thus, under the same treatment conditions (the expended power in the discharge was 3 W/cm 3 and the current frequency was 500 Hz), the efficiency of the purification process in the presence of photocatalysts was 20% higher compared to DBD.
Apart from reducing energy costs, the plasma-catalytic method allows for more profound destruction of the dye compared to UV photolysis. Figure 8 shows the evolution of UV-Vis absorption spectra for RhB which, being a chromophore, is characterized by three major absorption bands in an aqueous solution at 554, 340 and 259 nm [48]; a decrease in the latter indicates degradation of the aromatic part of the dye. The most important observation when comparing spectra in Figure 8 is the emergence of intense bands around 200 nm in the DBD spectrum as the processing time increased. These bands were characteristic for carboxylic acids (n→π* transition at λmax = 204 nm) [49], which indicates destructive oxidative processes leading to the rupture of the aromatic rings of the dye and the formation of simpler organic compounds such as carboxylic acids. To quantify the destruction of the studied pollutant, experiments were carried out to assess changes of the total organic carbon (TOC) content and the concentration of carbon oxides (CO and CO2). Aqueous solutions of Rhodamine B were studied with an initial concentration of 40 mg/L. The solutions were processed in DBD with a TiO2-PAMMH catalyst at optimal processing parameters. These conditions were chosen because the TiO2-PAMMH catalyst in DBD shows the maximum dye decomposition efficiency at the minimum energy cost. As can be seen from Figure 9, the maximum degree of decomposition under these experimental conditions was 91% and the degree of mineralization was 80%. The decomposition process initially formed intermediate organic compounds with a lower molecular weight (such as alcohols and carboxylic acids), which were subsequently oxidized to CO, CO2 and H2O, which confirmed a high degree of mineralization. The measurement of the content of carbon oxides in the system made it possible to assess the convergence of the carbon balance (i.e., the completeness of the determination of intermediate compounds), which was determined by the formula: where Ypr is the carbon content in the system after the processing (decomposition products in the liquid and gas phases), taking into account the incompleteness of RhB destruction, and Yin is the carbon content in the RhB stock solution. Carbon oxides were detected only in the gas phase, which could be explained by the low pH < 4 of the solutions after DBD treatment. The CO and CO2 concentrations were around 16.6 mmol/m 3 and 21.2 mmol/m 3 for a carrier gas flow rate of 0.5 L/min (8.3·10 −6 m 3 /s), which corresponded to 1.43·10 −7 mol/s and 1.82·10 −7 mol/s, respectively. The assessment of the carbon balance showed that the total yield of carbon oxides was at least 90% of the TOC in the system, which confirmed the experimental TOC results.
The results allowed us to suggest a possible mechanism for the decomposition of RhB, which proceeded through a series of intermediate stages. It included the breaking of aromatic rings with the formation of aldehydes, alcohols, and carboxylic acids, which were easily oxidized and were converted into CO and CO2 by the action of active particles ( Figure 10). Ozone is one of the main oxidizing agents formed in the barrier discharge [50], which is also reflected in the proposed destruction mechanism in Figure 10. The maximum dye destruction efficiencies were observed at high DBD powers. This suggests that the optimal conditions for the formation of ozone were precisely fulfilled for these parameters. To assess the contribution of ozone to the RhB degradation, the ozone concentration in the DBD process was measured in model aqueous solutions with and without RhB and a photocatalyst, see Figure 11. The ozone concentration increased with the discharge power, as measured for the reference sample 1. For a higher discharge power a part of the ozone was consumed for the RhB destruction. The contribution of ozone to the RhB oxidation process can be quantified according to the equation: Hence, about 24 moles of O3 are needed for the complete oxidation of 1 mol of RhB. According to the data presented in Figure 11, the maximum decrease in ozone concentration during dye oxidation was 0.12 × 10 18 cm −3 , which corresponded at a liquid flow rate of 0.5 mL/s to 100 μmol/s. When the dye content in the system was equal to 43 μmol/s, its total oxidation required 1032 μmol O3. Therefore, other active particles formed in the discharge zone of the reactor made a significant contribution to the decomposition of the dye besides the ozone. It should also be noted that the introduction of a catalyst into the DBD reactor did not affect the ozone formation and destruction processes in the discharge power range of 1.1-2.1 W/cm 3 ( Figure 11). Only at high values of the discharge power, the ozone concentration in the liquid decreased by approximately 10% in the presence of a catalyst.

Materials
Rhodamine B (RhB, C28H31ClN2O3, M = 479.02 g/mol; Figure 12), which belongs to the group of fluorescent dyes [51], was chosen as a model pollutant. RhB is highly soluble in water and is highly stable towards light [52].
Preparation of TiO2-pillared montmorillonite was carried out in accordance with the three following methods: I) intercalation of titanium hydroxocomplexes [54]; II) hydrothermal activation of the intercalation of titanium hydroxocomplexes [55]; III) both the preliminary mechanical treatment of the layered substrate [51] and hydrothermal activation of the intercalation of titanium hydroxocomplexes.
Intercalating solutions containing titanium polycations were prepared at room temperature by hydrolysis of titanium chloride according to Ref. [54]. In detail, 6 M solution of HCl was treated with TiCl4 (Sigma-Aldrich Rus, Moscow, Russia) drop by drop to obtain solutions with a Ti 4+ concentration of 4.92 M (a concentration of 4.92 M was the upper limit of sol formation). For further intercalation, the solutions were diluted by slow addition of deionized water to obtain solutions with a residual Ti 4+ concentration of 0.56 M. Prior to use, intercalating solutions were subjected to aging for 3 h at 20 °C, resulting in the formation of titanium polyhydroxocomplexes.
According to method I, the intercalation of montmorillonite by titanium hydroxocomplexes was carried out using ion exchange in a 1% aqueous suspension with a drop-by-drop addition of an intercalating solution (10 mmol of Ti 4+ /g MM) and vigorous stirring with a magnetic stirrer for 3 h at 20 °C. According to method II, the suspension of MM and the intercalating solution was subjected to hydrothermal treatment for 5 h at a temperature of 115 °C and a pressure of 170 kPa using a pressurized reactor made from fluoroplastic glass. After 12 h of coagulation at room temperature, the suspension was washed from Cl − ions, centrifuged and dried in a drying cabinet at 60 °C. According to method III, the original MM was treated in an energy-stressed planetary centrifugal mill AGO-2C (Novice, Novosibirsk, Russia). The mechanically activated MM is denoted as AMM. High-strength zirconium grinding bodies were used at a constant rotor speed of 1500 rpm; the mass ratio of MM to grinding bodies was 7.5:1. The milling improves textural properties [32]. Intercalated materials were prepared according to method II. Pillared materials were obtained by annealing intercalated samples in a furnace at a temperature of 500 °C for 3 h.

Description of Experimental Installations
A scheme of the DBD reactor is shown in Figure 13 [16]. The reactor is a coaxial system consisting of an outer Pyrex tube, 12 mm in diameter, which is the dielectric barrier of the discharge, and an inner aluminum-alloy electrode with a diameter of 8 mm. The outer electrode is an aluminum foil, uniformly deposited on the outer surface of the glass tube. The discharge zone was 12 cm long. The solution flows along the outer side of the electrode, in the volume where the gas flows. A hydrophobic glass fabric with a thickness of 1 mm was applied to the inner electrode, providing a film flow mode of the model solution in the system.
where D is the thickness of the hydrophilic material, h is the thickness of the solution film, Q is the volumetric flow rate of the solution and L is the length of the discharge zone. The film thickness of the fluid was calculated assuming a smooth laminar flow in the field of gravity [56]: (18) where n is the kinematic viscosity of the fluid and g is the gravitational constant. The discharge was excited by a high-voltage transformer. The voltage was monitored using a high-voltage probe, and the discharge current was determined by the voltage drop across the resistor (100 Ohm) connected in series to the ground circuit. Both signals were simultaneously controlled by a two-channel digital oscilloscope GW Instek GDS-2072 (Good Will Instrument CO. LTD, New Taipei City, Taiwan). The voltage in the system was changed from 6 to 13 kV. The discharge current in the experiments was 0.1-0.8 mA. The frequency of the discharge current varied in the range 500-2000 Hz, and the discharge power in the studied frequency range was 20-180 W. Voltage-current characteristics and discharge power, as well as the effect of the frequency of the discharge current on the physical characteristics of the plasma, are given in [15].
The plasma-forming gas was oxygen (technical grade, 99.7%), which was fed into the system against the fluid flow with a volume flow rate of 1-3 cm 3 /s.
The photocatalytic reactor is shown in Figure 14. The photocatalytic activity of the TiO2-pillared MM samples was derived from the RhB destruction rate in an aqueous solution. The source of UV radiation was a high-pressure 250 W mercury lamp (Royal Philips Electronics, Amsterdam, The Netherlands) with maximum emission at 365 nm. The lamp was located in a water-cooled quartz vessel and placed in the center of the reactor with a volume of 800 mL. A magnetic stirrer provided an effective mixing of the reaction volume. The solution was purged with a constant air flow to ensure a steady concentration of dissolved oxygen. In each experiment, the synthesized photocatalyst (1 g/L) was added to 500 mL of the RhB solution (40 mg/L). A homogeneous reaction mixture was obtained after stirring up to 100 min at 25 °C.
The RhB concentration in the solution was determined photometrically before and during the process in the photocatalytic reactor or the DBD reactor. The optical density at the absorption maximum of RhB at λmax = 554 nm was measured on a Hitachi U-2001 spectrophotometer (wavelength range 200-800 nm). The RhB absorption maximum was determined from UV-Vis spectra of an aqueous solution ( Figure 8) and corresponds to n→π* transitions of the C=N and C=O groups [57].
To eliminate any effect of sorption processes, the photocatalytic reactor and the DBD reactor were equilibrated for 30 min [31] and 5 min, respectively, before starting the process. The reactor vessels were thoroughly cleaned between experiments.
The destruction (α) of RhB was evaluated from the discoloration of the solution: where A0 and A are the initial and final absorption, respectively, of the Rhodamine B solution at λmax = 554 nm. The ozone concentration was measured in an external cell from absorption measurements at 253.7 nm, close to the maximum of the Hartley ozone absorption band. An AvaSpec-2048FT-2 monochromator (Avantes BV, Apeldoorn, The Netherlands) with digital spectrum recording and a low-pressure Hg lamp were used. The ozone concentration was calculated from the absorption cross section 1.418 × 10 −18 cm 2 [58].
The CO and CO2 content in the gas phase at the outlet of the reactor were estimated by gas chromatography (Chromatech-5000 gas chromatograph, Chromatek, Yoshkar-Ola, Mariy El, Russia) with a methanator and a plasma ionization detector [59].

Conclusions
In this study, the degradation of the water-soluble dye Rhodamine B was investigated using photocatalytic, plasma and combined plasma-photocatalytic processes with the use of TiO2-pillared montmorillonite as a nanoscale photocatalyst. The catalysts were prepared by intercalation of titanium hydroxocomplexes, including hydrothermal activation of the process and preliminary mechanical treatment of the layered substrate. A 100% degradation of Rhodamine B was achieved in 8 s using a DBD plasma treatment in the presence of photocatalysts with a process energetic efficiency of 2.27 g/kWh. Over the same time, conventional plasmolysis removed 94% of the dye (1.21 g/kWh). UV photocatalytic degradation allowed for the removal of 92% RhB after 100 min of irradiation (0.24 g/kWh). Thus, a synergistic effect was observed (both in terms of energetic efficiency and process rate) for the combined use of the plasma and photocatalytic processes. The reaction of the dye destruction was described by a first order kinetic equation and the largest observed rate constant for the reaction of destruction was 0.6910 s -1 . In addition, in terms of complete purification of aqueous solutions from organic pollutants, the advantage of combined DBD plasma and TiO2-pillared montmorillonite treatment was based on more profound destructive processes leading to the formation of simple organic compounds such as carboxylic acids as compared with UV photolysis. It is shown that improved textural properties of the nanophotocatalyst (specific surface area and total pore volume) and an increase in the size of the TiO2 crystallites upon hydrothermal treatment allows for more efficient removal of the dye from aqueous solutions regardless of the type of the external influence.