Reaction Rate Study of the Photocatalytic Degradation of Dichloroacetic Acid in a Black Body Reactor

: The light-induced degradation of dichloroacetic acid in aqueous suspensions containing the TiO 2 photocatalyst Hombikat UV 100 was investigated. The reactions were performed in a black body reactor in which the rate of conversion, deﬁned as the time derivative of the extent of conversion, is not a ﬀ ected by the light scattering properties of the photocatalysts. At su ﬃ ciently high concentrations of both the probe compound and the photocatalyst the rate of conversion was found to be unswayed by the initial concentration of the probe compound, the mass concentration of the photocatalyst, and the suspension volume. Thus, the chosen experimental conditions enable the determination of the rate of conversion and the quantum yield of the light induced degradation of dichloroacetic acid in aqueous photocatalyst suspension with su ﬃ ciently good reproducibility. The experimental procedure employed here seems to be generally applicable to determine rates of conversion and quantum yields that possibly allow a comparison of the activities of photocatalysts in aqueous suspensions.


Introduction
Heterogeneous photocatalysis in solid-liquid systems is considered as an effective method to harvest photons for the oxidative degradation of organic water pollutants, the generation of molecular hydrogen by water splitting or reforming of organic compounds, the fixation of carbon dioxide or molecular nitrogen, and the synthesis of organic compounds. Therefore, new photocatalysts and photocatalytically active composites are being synthesized and investigated with respect to possible applications in heterogeneous photocatalysis [1][2][3][4][5][6][7][8].
Technically applicable photocatalysts must meet a number of requirements. It is crucial that the photocatalytically active solid is stable under the conditions of the desired light-induced chemical reaction, and that it has a high photocatalytic activity. The latter condition inevitably requires the comparative assessment of the activities of semiconductors and composites intended as photocatalysts.
Several methods have been proposed for this comparative assessment of photocatalytic activities in suspensions. For details on the proposed methods, the curious reader is referred to the recently published papers of Kisch and Bahnemann [9], Qureshi and Takanabe [10], Hoque and Guzman [11], and the references given therein. Usually, the reaction rate at which a probe compound is photocatalytically converted, is used as the measure of the photocatalytic activity of the solid under consideration. The activities of different photocatalysts are then assessed by comparing the numerical values of the respective rates. Reaction rates are usually reported on a volume basis (converted amount of the probe compound per unit time and unit suspension volume), a mass basis (converted amount per unit time and unit mass of photocatalyst), or an area basis (converted amount per unit time and unit surface area of photocatalyst). A photocatalytic reaction, however, takes place only in the small volume inside the photoreactor that is located directly behind the light entrance. In this volume, the photon flux decreases as the distance from the entrance window increases. This, of course, is accompanied by a decrease in the reaction rate, which becomes zero in the more distant layers of the suspension, which are not penetrated by photons. A reported reaction rate is consequently always a volume averaged value. A prerequisite for the comparison of reaction rates is that the values were determined under identical reaction conditions [9]. Consequently, the comparison of published values is impeded due to the lack of detailed information on the geometry of the photoreactor, the size of the entrance window, and the characteristics of the irradiation conditions.
To avoid this draw-back, it has been proposed to calculate the ratio between the amounts of the probe compound reacted in a time interval and the photons impinging on the outer wall of the light entrance in this time interval. However, objections have been raised against this ratio, which is called the photonic efficiency (also known as quantum efficiency), as a measure of the photocatalytic activity of a material. In almost all published papers reporting comparative studies of photocatalysts in suspensions, experimental setups were used, in which the slurries are irradiated by an external light source through a window in the outer wall of the photoreactor. In such an arrangement of photoreactor and light source (positive irradiation geometry), a fraction of the photons entering the suspension is not absorbed, but back-scattered out of the slurry and the reactor [12][13][14][15]. This undesired loss of photons can vary between 13% and 76% of the incoming light [12]. The ratio between absorbed and out-scattered photons depends, inter alia, on the photocatalyst composition, its particle size, and its mass concentration [16][17][18]. A reaction rate determined with an experimental set-up having positive irradiation geometry and, consequently, the resulting photonic efficiency thus also reflects the optical properties of the suspension and is, therefore, not a measure of the intrinsic activity of the photocatalyst under consideration.
Recently, Emeline and co-authors have proposed a particular design of a reactor with negative irradiation geometry in which the light entrance is surrounded by the suspension in all three spatial directions (as far as technically feasible) [19]. The design of this photoreactor ensures that almost all out-scattered photons re-enter the suspension elsewhere. Provided that no photons are transmitted through the suspension, all the photons with appropriate energy to excite the photocatalyst are absorbed inside the suspension. Although the reactor filled with the suspension behaves like a black body only in a finite wavelength range, it was termed as a black body-like reactor by Emeline et al. [19].
Provided that the photocatalyst is the only light absorbing species and that the suspension is optically dense for photons having an energy greater than the bandgap energy of the photocatalyst (i.e., no photons are transmitted through the reactor), all the photons with appropriate energy emitted by the light source are absorbed by the photocatalyst. All photons emitted by the light source are therefore available to initiate a photocatalytic reaction. The rate of a photocatalytic reaction as a measure of the photocatalytic activity is thus diminished only by the recombination of the photogenerated charge carriers and is independent from the scattering properties of the photocatalyst. The amount of photons emitted by the light source and entering the black body-like photoreactor can easily be determined by chemical actinometry. When using a monochromatic light source, a quantum yield-as is usual for homogeneous photochemical reactions-can thus be calculated [19]. However, it must be emphasized that a quantum yield will only be meaningful if the photocatalyst is the only species that absorbs the photons entering the suspension. In order to determine the quantum yield of a light-induced reaction in a photocatalyst suspension, the probe compound must therefore be optically transparent. In addition, the photocatalytic conversion of the probe compound must not yield intermediates and products capable to absorb the incoming light. Dichloroacetic acid (DCA) is an organic compound that meets these requirements when irradiated with visible and UV(A) light. DCA presents some additional advantages for laboratory studies due to its low vapor pressure and high water solubility [20]. An additional advantageous reason to use DCA as the probe compound is given by the fact that the photocatalytic reaction according to can be monitored not only by measuring the DCA concentration [20][21][22][23][24], but also by measuring the concentration of organic carbon (TOC) [20,21,25], as well as the evolved amounts of CO 2 [26], Cl − [20,21,26,27], and H + (employing, e.g., a pH-stat technique [27][28][29][30]) to determine the photocatalytic reaction rate. However, for the direct comparison of the rates obtained by the measurements of these analytes, it is recommended that the rates of conversion as defined by the IUPAC are used [31]. The rate of conversion of a species i is defined as the time derivative of the extent of reaction ξ(i) where n(i) and C(i) are the amount and the amount concentration (molarity), respectively, of this species at any time t, ν(i) is its stoichiometric coefficient, and V is the volume of the suspension. If Equation (1) is valid, then the equality dξ(DCA)/dt = dξ(CO 2 )/dt = dξ(Cl − )/dt must be satisfied during the photocatalytic degradation of DCA. However, the evaluation of published data employing the rates of conversion suggests that the numerical values are slightly different for the different analytes [20,21,26]. Such differences in the rates of conversion would then have to be taken into account when comparing published data for one reactant but obtained with different analytes.
This article reports on the photocatalytic oxidation of dichloroacetic acid in acidic aqueous suspensions employing a black body-like reactor. The initial concentration of DCA, the mass concentration of the photocatalyst TiO 2 Hombikat UV 100, the volume of the suspension, and the photon flux were varied. The experimental conditions were chosen such that the DCA concentration decreases linearly with the irradiation time, with the result that the kinetics of the photocatalytic degradation of DCA is approximated by a zero-order rate law. This work was performed to answer two scientific questions: (i) How reproducible are the results of photocatalytic degradation experiments performed in a black body photoreactor? (ii) Are the rates of conversion for the reactant and the reaction product (here DCA and Cl − ) the same within the limits of experimental error? This paper thus complements our recent publications, in which we have used the black body photoreactor for the comparative assessment of heterogeneous photocatalysts and for the determination of the quantum yields of heterogeneous photocatalytic reactions [23,24].

Results
The light induced degradation of dichloroacetic acid (DCA) in the presence of Hombikat UV 100 as the photocatalyst was studied by varying the initial concentration of the probe compound (2 mmol L −1 ≤ C s ≤ 20 mmol L −1 ), the mass concentration of the photocatalyst (1 g L −1 ≤ γ ≤ 10 g L −1 ), the suspension volume (80 mL ≤ V ≤ 900 mL), and the photon flux into the suspension (0.54 µmol min −1 ≤ dn p /dt ≤ 10.7 µmol min −1 ). The temperature, the concentration of dissolved oxygen, the pH, and the ionic strength were kept almost constant. After adding the photocatalyst to the aqueous DCA solution and pH adjustment, the suspensions were stirred in the dark for two hours prior to irradiation. In all experimental runs the DCA concentration was found to decrease during this dark period, i.e., the DCA concentration C 0 at the time when the light source was switched on (t = 0) was always found to be lower than the DCA concentration C s of the stock solution. The monochromatic light was directed by means of a wave guide into the center of the suspension. The light inlet was thus surrounded by the suspension in all spatial directions. Therefore, it can be assumed that the condition for a blackbody reactor, i.e., all incident photons are absorbed in the suspension, is satisfied.
In a first set of experimental runs, the impact of the amount concentration of DCA on the reaction rate was investigated. Therefore, the initial concentration of DCA was varied at a constant mass concentration of the photocatalyst (γ = 5 g L −1 ), a constant photon flux (dn p /dt = 10.7 µmol min −1 ), and a constant suspension volume (V = 400 mL). Figure 1A illustrates the change of the DCA concentration as determined by HPIC during UV(A) irradiation for experimental runs with DCA concentrations C s varying between 2 mmol L −1 and 20 mmol L −1 . It becomes obvious from this figure, that the DCA concentration decreased linearly with time during UV(A) irradiation. The degradation rates defined as the time derivative of the amount concentration (dC/dt) are directly obtained from the slope of the graphs. The numerical values of the thus calculated degradation rates are given in Figure 1B. The rates were found to be constant within the limits of experimental error (dC/dt = 4.79 ± 0.56 µmol L −1 min −1 ) and not affected by the initial concentration of DCA at the experimental conditions employed here. The rate of conversion was calculated inserting the reaction rate, the suspension volume V, and the stoichiometric coefficient ν(DCA) = 1 into Equation (2). A mean value dξ(DCA)/dt = 1.92 ± 0.22 µmol min −1 was obtained. the suspension in all spatial directions. Therefore, it can be assumed that the condition for a blackbody reactor, i.e., all incident photons are absorbed in the suspension, is satisfied. In a first set of experimental runs, the impact of the amount concentration of DCA on the reaction rate was investigated. Therefore, the initial concentration of DCA was varied at a constant mass concentration of the photocatalyst (γ = 5 g L − ¹), a constant photon flux (dnp/dt = 10.7 µmol min − ¹), and a constant suspension volume (V = 400 mL). Figure 1A illustrates the change of the DCA concentration as determined by HPIC during UV(A) irradiation for experimental runs with DCA concentrations Cs varying between 2 mmol L − ¹ and 20 mmol L − ¹. It becomes obvious from this figure, that the DCA concentration decreased linearly with time during UV(A) irradiation. The degradation rates defined as the time derivative of the amount concentration (dC/dt) are directly obtained from the slope of the graphs. The numerical values of the thus calculated degradation rates are given in Figure 1B. The rates were found to be constant within the limits of experimental error (dC/dt = 4.79 ± 0.56 µmol L − ¹ min − ¹) and not affected by the initial concentration of DCA at the experimental conditions employed here. The rate of conversion was calculated inserting the reaction rate, the suspension volume V, and the stoichiometric coefficient ν(DCA) = 1 into Equation (2). A mean value dξ(DCA)/dt = 1.92 ± 0.22 µmol min − ¹ was obtained. In a second set of experimental runs the impact of the mass concentration of the photocatalyst on the DCA degradation rate was investigated. The initial concentration of DCA (Cs = 10 mmol L − ¹), the photon flux (dnp/dt = 10.7 µmol min − ¹), and the suspension volume (V = 400 mL) were kept constant during these experimental runs. The measured DCA concentrations are plotted versus the irradiation time in Figure 2A. Again, linear concentration-time plots were obtained enabling the determination of the DCA degradation rates from the slopes of these plots. The degradation rates were found to be constant (dC/dt = 5.54 ± 0.43 µmol L − ¹ min − ¹) and not affected by the mass concentration γ of the photocatalyst Hombikat UV 100 ( Figure 2B). With this reaction rate, a mean rate of conversion dξ(DCA)/dt = 2.22 ± 0.17 µmol min − ¹ is calculated employing Equation (2).
In a third set of experimental runs, the suspension volume was varied at constant initial concentration of DCA (Cs = 10 mmol L − ¹), photon flux (dnp/dt = 10.7 µmol min − ¹), and mass concentration of the photocatalyst (γ = 5 g L − ¹). Again, linear concentration-time plots were obtained ( Figure 3A). However, when the degradation rates determined from the slopes of these concentration-time plots are plotted versus the suspension volume, a non-linear decrease is observed ( Figure 3B) as expected for the photocatalytic degradation of a probe compound in suspension. The In a second set of experimental runs the impact of the mass concentration of the photocatalyst on the DCA degradation rate was investigated. The initial concentration of DCA (C s = 10 mmol L −1 ), the photon flux (dn p /dt = 10.7 µmol min −1 ), and the suspension volume (V = 400 mL) were kept constant during these experimental runs. The measured DCA concentrations are plotted versus the irradiation time in Figure 2A. Again, linear concentration-time plots were obtained enabling the determination of the DCA degradation rates from the slopes of these plots. The degradation rates were found to be constant (dC/dt = 5.54 ± 0.43 µmol L −1 min −1 ) and not affected by the mass concentration γ of the photocatalyst Hombikat UV 100 ( Figure 2B). With this reaction rate, a mean rate of conversion dξ(DCA)/dt = 2.22 ± 0.17 µmol min −1 is calculated employing Equation (2).
In a third set of experimental runs, the suspension volume was varied at constant initial concentration of DCA (C s = 10 mmol L −1 ), photon flux (dn p /dt = 10.7 µmol min −1 ), and mass concentration of the photocatalyst (γ = 5 g L −1 ). Again, linear concentration-time plots were obtained ( Figure 3A). However, when the degradation rates determined from the slopes of these concentration-time plots are plotted versus the suspension volume, a non-linear decrease is observed ( Figure 3B) as expected for the photocatalytic degradation of a probe compound in suspension. The reaction rates have been fitted using a regression curve dC/dt = k/V with k = 1.82 ± 0.04 µmol min −1 . Since the stoichiometric coefficient of DCA is unity, this value k corresponds directly to the rate of conversion dξ(DCA)/dt defined by Equation (2). The good agreement between the experimental and the fitted values clearly indicate the independence of the rate of conversion from the suspension volume within the limits of experimental error. This also clearly demonstrates that the experimental set-up employed here behaves like a black body reactor: with a given photocatalyst and under the condition of (apparent) zero-order kinetics with respect to the organic solute, constant photon fluxes result in constant rates of conversion! Catalysts 2019, 9,635 5 of 17 reaction rates have been fitted using a regression curve dC/dt = k/V with k = 1.82 ± 0.04 µmol min − ¹.
Since the stoichiometric coefficient of DCA is unity, this value k corresponds directly to the rate of conversion dξ(DCA)/dt defined by Equation (2). The good agreement between the experimental and the fitted values clearly indicate the independence of the rate of conversion from the suspension volume within the limits of experimental error. This also clearly demonstrates that the experimental set-up employed here behaves like a black body reactor: with a given photocatalyst and under the condition of (apparent) zero-order kinetics with respect to the organic solute, constant photon fluxes result in constant rates of conversion!   reaction rates have been fitted using a regression curve dC/dt = k/V with k = 1.82 ± 0.04 µmol min − ¹.
Since the stoichiometric coefficient of DCA is unity, this value k corresponds directly to the rate of conversion dξ(DCA)/dt defined by Equation (2). The good agreement between the experimental and the fitted values clearly indicate the independence of the rate of conversion from the suspension volume within the limits of experimental error. This also clearly demonstrates that the experimental set-up employed here behaves like a black body reactor: with a given photocatalyst and under the condition of (apparent) zero-order kinetics with respect to the organic solute, constant photon fluxes result in constant rates of conversion!   Finally, the impact of the photon flux (0.54 µmol min −1 ≤ dn p /dt ≤ 10.7 µmol min −1 ) on the reaction rate was investigated. The initial concentration of DCA (C s = 10 mmol L −1 ), the mass concentration of the photocatalyst (γ = 5 g L −1 ), and the suspension volume (400 mL) were kept constant. Figure 4A depicts the measured DCA concentrations versus the irradiation time for five selected experimental runs performed with different photon fluxes. Linear concentration-time plots were obtained with all photon fluxes in the range mentioned above, thus indicating that the photon flux is not affecting the kinetics of the DCA degradation reaction. The rates calculated from the slopes of these plots are presented in Figure 4B. A non-linear relation between the calculated degradation rates and the photon fluxes becomes obvious. Finally, the impact of the photon flux (0.54 µmol min − ¹ ≤ dnp/dt ≤ 10.7 µmol min −1 ) on the reaction rate was investigated. The initial concentration of DCA (Cs = 10 mmol L −1 ), the mass concentration of the photocatalyst (γ = 5 g L −1 ), and the suspension volume (400 mL) were kept constant. Figure 4A depicts the measured DCA concentrations versus the irradiation time for five selected experimental runs performed with different photon fluxes. Linear concentration-time plots were obtained with all photon fluxes in the range mentioned above, thus indicating that the photon flux is not affecting the kinetics of the DCA degradation reaction. The rates calculated from the slopes of these plots are presented in Figure 4B. A non-linear relation between the calculated degradation rates and the photon fluxes becomes obvious.

Discussion
In all experimental runs performed here, a decrease of the DCA concentration accompanied by a simultaneous increase of the Cl − concentration was observed during UV(A) irradiation of aqueous DCA-TiO2 slurries. No significant change in the concentrations was observed when irradiating homogeneous DCA solutions with UV(A) light. Stirring of DCA-containing TiO2 suspensions in the dark resulted in an initial decrease of the DCA concentration. However, no increase of the concentration of Cl − was observed. Therefore, the observed changes in the DCA and Cl − concentrations in UV(A) irradiated Hombikat UV 100 suspensions can only be attributed to a photocatalytic degradation of the organic solute. The main reaction steps of the photocatalytic DCA degradation at the acidic pH of the suspension employed here (pH 3) are given by the Equations (3) to (9) (adapted from [20] and [21]): TiO2-CHCl2COO − ads + h⁺ → TiO2-CHCl2COO • ads O2 ads + • CHCl2 ads → • OOCHCl2 ads (7)

Discussion
In all experimental runs performed here, a decrease of the DCA concentration accompanied by a simultaneous increase of the Cl − concentration was observed during UV(A) irradiation of aqueous DCA-TiO 2 slurries. No significant change in the concentrations was observed when irradiating homogeneous DCA solutions with UV(A) light. Stirring of DCA-containing TiO 2 suspensions in the dark resulted in an initial decrease of the DCA concentration. However, no increase of the concentration of Cl − was observed. Therefore, the observed changes in the DCA and Cl − concentrations in UV(A) irradiated Hombikat UV 100 suspensions can only be attributed to a photocatalytic degradation of the organic solute. The main reaction steps of the photocatalytic DCA degradation at the acidic pH of the suspension employed here (pH 3) are given by the Equations (3) to (9) (adapted from [20,21]): At pH 3, DCA is mainly dissociated in its constituting ions (pK a (DCA) = 1.06 [32]) resulting in the adsorption of negatively charged dichloroacetate ions at the positively charged TiO 2 surface (Equation (4)). The reaction pathway given by the Equations (3) to (9) takes into account that the oxidation of adsorbed dichloroacetate is initiated by an interfacial electron transfer from the adsorbate to a hole that is produced upon light excitation of a photocatalyst particle. The mechanism thus considers Catalysts 2019, 9, 635 7 of 17 that, in acidic TiO 2 suspensions, direct attack of the organic adsorbate by holes is significantly more important than oxidation by OH radicals as clearly demonstrated in previous publications reporting the photocatalytic degradation of carboxylic acids [20,21,[33][34][35][36][37][38][39][40][41][42][43]. The dichloroacetoxy radical formed by direct hole oxidation of adsorbed DCA (Equation (5)) decarboxylates yielding a carbon-centered radical (photo-Kolbe reaction, Equation (6)) which reacts with molecular oxygen in a subsequent reaction step (Equation (7)). Two of the intermediate radicals react in a bimolecular reaction yielding hydrogen peroxide and phosgene (Equation (8)) which is immediately hydrolyzed into CO 2 and Cl − (Equation (9)). According to this reaction mechanism the absorption of one photon by a photocatalyst particle is required to initiate the complete mineralization of one DCA yielding CO 2 , H + , and Cl − . If this mechanistic scheme is valid, then dξ(DCA)/dt = dξ(Cl − )/dt must hold.
As discussed in the Introduction, the reaction rate dC/dt of a photocatalytic reaction in suspension is a volume-averaged value calculated by integration of the local volumetric reaction rate r x over the entire suspension volume V dC Consequently, the rates reported in the Figures 1B, 2B, 3B, and 4B are volume-averaged values. The absorbed photons result in the formation of electron-hole pairs. A fraction of the formed electrons and holes recombine in a fast process. However, the remaining holes react with adsorbed dichloroacetate in a single electron transfer reaction according to Equation (5) The parameter Φ = dξ(DCA)/dn p,abs corresponds to the volume averaged quantum yield of the photocatalytic degradation reaction under consideration [31].
In Figure 5, the rates of conversion dξ(DCA)/dt for all experimental runs performed at a photon flux of 10.7 µmol min -1 are plotted versus the DCA concentration C s , the mass concentration γ of the photocatalyst and the suspension volume V. The average rate of DCA conversion was calculated as dξ(DCA)/dt = 2.02 ± 0.24 µmol min −1 (N = 13). With this average rate of conversion and the photon flux of 10.7 µmol min −1 emitted by the light source and determined by actinometry, the average quantum yield Φ of the photocatalytic DCA oxidation in the presence of Hombikat UV 100 was calculated to be 0.189 ± 0.023. For the purpose of comparison, the rates of conversion of Cl − are included in Figure 5. The average rate of conversion was calculated to be dξ(Cl − )/dt = 1.64 ± 0.48 µmol min −1 (N = 13) which corresponds to an average quantum yield Φ = 0.153 ± 0.046 for the photocatalytic DCA oxidation in acidic suspension containing Hombikat UV 100.
It becomes obvious from the data presented in Figure 5 that chloride is released slower than DCA is photocatalytically oxidized. The rate dξ(Cl − )/dt was found to be almost 20% lower than dξ(DCA)/dt. Obviously, the relation dξ(DCA)/dt = dξ(Cl − )/dt, whose validity is mandatory if the DCA degradation follows the reaction path proposed above (Equation (3) -(9)), does not hold.
Chloride is known to adsorb on a TiO 2 surface at acidic pH [28,44]. A Langmuir adsorption constant of 0.69 L mmol −1 was reported for the adsorption of Cl − on a Degussa P25 surface at pH 3 [44]. Certainly, the adsorbed fraction of the photocatalytically generated Cl − is not available for the quantification by HPIC. Losses due to the evolution of molecular chlorine, which might be formed via hole oxidation of adsorbed Cl − and subsequent dimerization of two Cl • , seems to be unlikely [44]. However, the formation of chloro-organic intermediates cannot be excluded. One possible reaction is the formation of tetrachloroethane by dimerization of two dichloromethyl radicals. Small amounts of tetrachloroethane were detected during the light-induced oxidation of dichloromethane in the presence of chlorocuprate ions [45], and in O 2 -free suspensions of TiO 2 [46]. The analogous formation of ethane by dimerization of two methyl radicals was demonstrated to occur during the photocatalytic reaction of acetic acid in O 2 -free [42,43,47,48] and in O 2 -containing TiO 2 suspensions [48]. Possibly, reactions of • CHClCOO − and • CCl 2 COO − , whose intermediary formation and subsequent reactions to chloro-organic compounds has been discussed [49], must also be considered. Chemseddine and Boehm, who have investigated the photocatalytic DCA degradation in aqueous slurries of Degussa P25 TiO 2 , reported a rate of CO 2 evolution significantly lower than the rate of Cl − formation. They emphasized, however, that almost all the chlorine bound in the reactant was released as chloride [26]. Asmus and co-workers observed the formation of small amounts of oxalic acid during irradiation of DCA in the presence of Degussa [50]. On the other hand, Ballari and co-authors, who have investigated the DCA degradation in the presence of an anatase TiO 2 , reported that 2 moles of Cl − are generated from 1 mole of degraded DCA, and that the chromatographically determined DCA concentrations were almost equal to the concentrations calculated from corresponding TOC measurements. They concluded that no stable organic intermediates are formed during the photocatalytic degradation of DCA [20]. Zalazar et al. reported small differences between the measured concentrations of organic carbon (TOC) and Cl − and the values expected from the measured DCA concentrations in the initial phase of the experimental runs. However, they claimed that a statistical test does not indicate these deviations are significant [21]. The preceding discussion suggests that the observed low rates of conversion of Cl − compared to the rates of conversion of DCA are most likely caused by losses due to the adsorption of Cl − on the photocatalyst surface. However, this should not preclude the possible formation of organochlorine compounds. Chloride is known to adsorb on a TiO2 surface at acidic pH [28,44]. A Langmuir adsorption constant of 0.69 L mmol − ¹ was reported for the adsorption of Cl − on a Degussa P25 surface at pH 3 [44]. Certainly, the adsorbed fraction of the photocatalytically generated Cl − is not available for the quantification by HPIC. Losses due to the evolution of molecular chlorine, which might be formed via hole oxidation of adsorbed Cl − and subsequent dimerization of two Cl • , seems to be unlikely [44]. However, the formation of chloro-organic intermediates cannot be excluded. One possible reaction is the formation of tetrachloroethane by dimerization of two dichloromethyl radicals. Small amounts The rates of conversion dξ(DCA)/dt and dξ(Cl − )/dt were found to be constant within the limits of experimental error and not affected by the initial concentration of the probe compound dichloroacetic acid, C s , the mass concentration of the photocatalyst Hombikat UV 100, γ, and the suspension volume V, when C s and γ are larger than 2 mmol L −1 and 1 g L −1 , respectively. The deviations from the average values of dξ(DCA)/dt and dξ(Cl − )/dt were found to be about 12% and 30%, respectively. The observed variance is possibly due to the inhomogeneity of the commercial Hombikat UV 100, as had already been reported for Degussa P25 (now Aeroxide TiO 2 P25, Evonik Industries AG, Essen, Germany) [51]. It should be noted, however, that the reproducibility found here for the rate of DCA conversion is within the usual range in photocatalytic experiments [52,53]. The larger experimental error in the determination of dξ(Cl − )/dt is attributed to the significantly lower concentrations of chloride formed during the photocatalytic degradation of DCA. Employing a black body photoreactor, rates of conversion can thus be determined with sufficiently good reproducibility.
The kinetics of light-induced reactions of organic compounds in photocatalyst suspensions are usually analyzed by Langmuir−Hinshelwood-type rate laws [53][54][55][56][57][58][59][60][61][62][63], which can all be written as Depending on the underlying mechanistic assumptions, the physical meaning of the kinetic parameters k 1 , k 2 , and k 3 are different in the different Langmuir−Hinshelwood-type rate laws [53][54][55][56][57][58][59][60][61][62][63]. It is well known, that the macroscopic reaction rate dC/dt depends not only on the substrate concentration C but also on the concentration of the photocatalyst γ and the photon flux density I 0 . The rate law given by Equation (12) explicitly describes only the correlation between the reaction rate and the substrate concentration. The dependence of the reaction rate on the other two mentioned variables is implicitly included in the kinetic parameters k 1 and k 3 , which thus do not represent constants but functions of these variables. In an early work, it was deduced from mechanistic considerations that k 1 = k 1 I α 0 , where the exponent α is 1 at low light intensities and 0.5 at high light intensities [54]. It has later been experimentally observed that in many cases dC/dt is proportional to I α 0 with 0 ≤ α ≤ 1 [64]. This resulted in rate laws in which k 1 as well as k 3 are depending on I 0 [55,56,58,59,64]. The concentration of the photocatalyst is at least included in k 1 , which comprises the maximum concentration of available adsorption sites, which naturally depends on the photocatalyst concentration. However, the impact of the photocatalyst concentration on the rate of a photocatalytic reaction is usually low over a wide concentration range [12]. Other physico-chemical parameters such as temperature, ionic strength, oxygen concentration, and pH, being known to affect the reaction rate, are assumed to be constant during the entire photocatalytic reaction, and are therefore usually not included in the kinetic expression.
During the derivation of most of the Langmuir-Hinshelwood-type rate laws used to interpret experimental data from photocatalytic degradation experiments it was ignored that the observed macroscopic reaction rate is a volume-averaged quantity. A macroscopic rate law for a photocatalytic reaction must however result from the integration of the local volumetric reaction rates over the entire suspension volume (Equation (10)). This approach was very recently used by Bloh and co-authors, resulting in a rate law which describes the impact of the concentration of the reactant C, the mass concentration of the heterogeneous photocatalyst γ, and the photon flux density I 0 on the observable macroscopic reaction rate dC/dt [62,63]. As this rate law was used to analyze the kinetic data presented in the Figure 1B, Figure 2B, and Figure 4B, the essential steps of the derivation are presented here to elucidate the restricting assumptions and simplifications.
Bloh assumed a bimolecular reaction between photo-generated reactive sites on the surface of the photocatalyst and the reactant. Essential in his approach is the ascertainment that only a limited number of sites on the photocatalyst surface are capable of forming these reactive surface sites. For the concentration of the reactive surface sites C rs in a small volume within the suspension, he assumed a steady-state of formation, decay (recombination), and reaction with the reactant [63] dC rs dt = 0 = r formation − r decay − r reaction Catalysts 2019, 9,635 10 of 17 In this equation, r p,x and η are the local volumetric rate of photon absorption and the efficiency of the conversion of photons yielding reactive surface sites, respectively. The maximum concentration of reactive surface sites, the concentration of generated surface sites, and the concentration of the reactant are indicated as C rs,0 , C rs , and C R , respectively. The symbols k d and k represent the rate constants of the recombination and the interfacial charge transfer reaction. Employing this approach, the local rate r x of the considered photocatalytic reaction is given by For the derivation of the local rate of photon absorption, Bloh neglected scattering effects by the photocatalyst particles and assumed that the photon absorption is correctly described by the Lambert-Beer law [63]. This approach results in Insertion of this expression for the local volumetric rate of photon absorption into Equation (14) yields the local reaction rate and, after integration over the whole suspension volume, the macroscopic rate law of the photocatalytic conversion of the reactant This rate law simplifies for suspensions of high optical density, where e γd γηI 0 k d +kC rs,0 C R holds, into It should be noted that this derivation implicitly includes some additional assumptions. Thus, it is assumed that both the reactant and the photocatalyst are uniformly distributed throughout the suspension volume so no concentration gradients become operative. Moreover, the derivation assumes that the photocatalyst is the only light-absorbing species and that the conversion of monochromatic light into reactive surface sites occurs with an efficiency independent from the local photon flux density.
In general, it is assumed that in heterogeneous photocatalytic reactions, the reacting substrate is adsorbed on the surface of the photocatalyst (Equation (4)). Thus, a photocatalyst particle provides both the sites for the formation of the reactive surface sites and the sites at which the reactant adsorbs. With the amounts of surface sites available to yield the reactive surface sites and to adsorb the reactant per unit mass of photocatalyst, f rs and f a , and the coverage of the photocatalyst by the reactant, θ, the product C rs,0 C R can be written as γf rs f a θ. With the rate constant k r = kf rs f a and the Langmuir adsorption isotherm θ = K a C/(1 + K a C), the rate law is obtained [63]. This rate law (that by the way can be written like Equation (12)) enables to correlate experimentally accessible reaction rates with the concentration of the reactant C, the mass concentration of the heterogeneous photocatalyst γ, and the photon flux density I 0 . The rate law given by Equation (19) was employed here to analyze the kinetic data presented in the Figures 1B, 2B, and 4B (Figure 6). The use of this equation seems reasonable when the light source is considered as a sphere in the center of the black body photoreactor. Furthermore, it is assumed that reflection at the interface between the sphere and the suspension as well as back-scattering finally causes the photons incident into the sphere to penetrate uniformly over the entire surface into the suspension. The volume in which the photocatalytic reaction occurs is hence a thin, uniformly irradiated layer surrounding the outer wall of this sphere. Neglecting the change in photon flux density due to the light propagation geometry, the local volumetric rate of photon absorption is thus given by Equation (15) and I 0 = 1 4πr 2 sphere dn p dt . It is a characteristic of a black body photoreactor in which all entering photons are absorbed inside the suspension, that the external geometry of the reactor does not affect the reaction rate. It is thus appropriate to consider the entire suspension volume V as a layer of thickness d spherically enveloping the central light-emitting sphere.
The experimental results presented above clearly evince that DCA adsorbs at the surface of Hombikat UV 100 under the experimental conditions employed in this study. From the values of γ, C s and C 0 given in Figures 1A, 2A, 3A, and 4A, an average amount of adsorbed DCA per unit mass of the photocatalyst, (C s −C 0 )/γ, was calculated to be 151 ± 42 µmol g −1 . The large variance of this value is an additional indication of the assumed inhomogeneity of the photocatalyst Hombikat UV 100. Hufschmidt et al. reported DCA loadings of 45-60 µmol g −1 and 70-90 µmol g −1 for platinized anatase-rutile composites (Degussa P25, 50 m 2 g −1 ) and platinized anatase (Hombikat UV 100, 300 m 2 g −1 ), respectively, in aqueous suspensions at pH 3 [65]. From data published by Czili and Horváth for the adsorption of DCA at pH 3, values of ≈50 µmol g −1 , ≈20 µmol g −1 , and ≈20 µmol g −1 are estimated for the anatase-rutile composite Degussa P25 (50 m 2 g −1 ), anatase (9.6 m 2 g −1 ), and rutile (9.7 m 2 g −1 ), respectively [49]. The calculated DCA loading on Hombikat UV 100 thus agrees reasonably well with published values. Several authors have described the adsorption of aliphatic carboxylic acids, such as acetic acid and dichloroacetic acid, from acidic aqueous solutions on TiO 2 surfaces by Langmuir adsorption isotherms [44,66,67]. Krivec et al. investigated the adsorption of DCA on Degussa P25 at pH 3 and calculated the maximum amount of adsorbed DCA to be 43 µmol g -1 . The maximum amount was found to decrease to 22 µmol g -1 in the presence of 0.5 mmol L −1 Cl − . They reported a Langmuir adsorption constant for DCA of 1.64 L mmol −1 unaffected by the presence of Cl − [44]. It thus seems justified to analyze the experimental data obtained here employing the rate law Equation (19), which requires Langmuir adsorption of the DCA on the Hombikat UV 100 surface.
The reaction rates calculated with Equation (19) are presented in Figure 6. The experimentally obtained reaction rates are included in this figure for the purpose of comparison. The kinetic parameters necessary for the calculation (given in the caption of Figure 6) were calculated by nonlinear fitting to the experimental data using a genetic algorithm [68]. However, it must be emphasized that the number of experimental data is too low to determine the parameters used in the computation with high accuracy. Despite this uncertainty resulting from the limited number of available data points (and from the simplifying assumptions made in the derivation of the rate law), a reasonable good agreement between the calculated and the experimentally obtained reaction rates becomes evident ( Figure 6).
A Langmuir-Hinshelwood-like dependence of the reaction rate on the DCA concentration becomes obvious from Figure 6A. With the adsorption constant K a = 1.023 L mmol −1 used for the computation of the lines in Figure 6, surface coverages varying from θ = 0.67 to θ = 0.95 are calculated for suspensions containing between 2 mmol L −1 and 20 mmol L −1 DCA. These coverages agree reasonable well with 0.79 ≤ θ ≤ 0.97 which are calculated with the experimentally obtained adsorption constant (K a = 1.866 ± 1.464 L mmol −1 ) for this range of DCA concentrations. The computational results show, in agreement with the experimental data, the independence of the reaction rate from the mass concentration of the photocatalyst in the range examined here ( Figure 6B). Even for the dependence of the reaction rate on the photon flux, a sufficiently good agreement between the experimentally determined rates and the values calculated with Equation (19) is obtained ( Figure 6C).
show, in agreement with the experimental data, the independence of the reaction rate from the mass concentration of the photocatalyst in the range examined here ( Figure 6B). Even for the dependence of the reaction rate on the photon flux, a sufficiently good agreement between the experimentally determined rates and the values calculated with Equation (19) is obtained ( Figure 6C). Naturally, the kinetic model enables some predictions as long as other physico-chemical parameters known to affect the reaction rate (e.g., temperature, pH, pO2) are kept constant: (i) The Langmuir-Hinshelwood-like dependence of the photocatalytic DCA degradation rate in the presence of Hombikat UV 100 on the substrate concentration is not affected by changing the photon flux. However, a decrease of the photon flux results in a significant decrease of the reaction rates ( Figure  6A). (ii) A change of the mass concentration does not affect the reaction rate when the substrate concentration as well as the photon flux is fixed ( Figure 6B). (iii) The impact of the photon flux on the reaction rate is low at high substrate concentrations, where the surface is almost saturated by adsorbed substrate ( Figure 6C). (iv) Changing the mass concentration of the photocatalyst over a wide range has almost no impact on the reaction rate as long as the photon flux is kept constant. (v) No impact of the mass concentration on the photon flux dependence of the reaction rate is observed in the range 1 g L − ¹ ≤ γ ≤ 10 g L − ¹ when the substrate concentration is fixed. The rate law chosen here to analyze the experimental data thus predicts reaction conditions in which the reaction rates at constant light intensity are almost independent from both the substrate concentration and the mass Naturally, the kinetic model enables some predictions as long as other physico-chemical parameters known to affect the reaction rate (e.g., temperature, pH, pO 2 ) are kept constant: (i) The Langmuir-Hinshelwood-like dependence of the photocatalytic DCA degradation rate in the presence of Hombikat UV 100 on the substrate concentration is not affected by changing the photon flux. However, a decrease of the photon flux results in a significant decrease of the reaction rates ( Figure 6A). (ii) A change of the mass concentration does not affect the reaction rate when the substrate concentration as well as the photon flux is fixed ( Figure 6B). (iii) The impact of the photon flux on the reaction rate is low at high substrate concentrations, where the surface is almost saturated by adsorbed substrate ( Figure 6C). (iv) Changing the mass concentration of the photocatalyst over a wide range has almost no impact on the reaction rate as long as the photon flux is kept constant. (v) No impact of the mass concentration on the photon flux dependence of the reaction rate is observed in the range 1 g L −1 ≤ γ ≤ 10 g L −1 when the substrate concentration is fixed. The rate law chosen here to analyze the experimental data thus predicts reaction conditions in which the reaction rates at constant light intensity are almost independent from both the substrate concentration and the mass concentration of the photocatalyst over wide ranges of these concentrations. Under these reaction conditions, it does not appear to be inappropriate to refer to the kinetics as a zero-order kinetics with regard to both the substrate concentration and the mass concentration of the photocatalyst.

Materials and Methods
Dichloroacetic acid (DCA) was purchased from Sigma-Aldrich, while potassium hydroxide and potassium nitrate were purchased from Fluka and Merck respectively. All mentioned chemicals were of analytical grade and used without further purification. Hombikat UV 100 (Sachtleben Chemie, now Venator Germany GmbH, Duisburg, Germany), an anatase TiO 2 with a BET surface area of 280 m 2 g −1 was used as the photocatalysts. Ultrapure water (≥18.2 MΩ cm) was applied in all experimental runs.
Stock solutions were prepared by dissolving potassium nitrate and DCA in water resulting in solutions with 10 mmol L -1 potassium nitrate and varying DCA concentrations (2 mmol L −1 to 20 mmol L −1 ). The salt was added to minimize the change of the ionic strength associated with the release of Cl − during the photocatalytic degradation of DCA. The required amounts of TiO 2 were added to these solutions to result in mass concentrations of the photocatalyst varying between 1 g L −1 and 10 g L −1 . The pH values of the freshly prepared suspensions, which depend on the DCA concentration, were lower than 2.8. They were adjusted at pH 3 by addition of potassium hydroxide to ensure the comparability between the results of the experimental runs.
The photocatalytic runs were performed in glass bottles of suitable size containing different suspension volumes (80 mL, 100 mL, 250 mL, 400 mL, 600 mL, and 900 mL) with a monochromatic light source (Omicron Laserage Laserprodukte GmbH, Rodgau-Dudenhofen, Germany, λ max = 365 nm with full width at half maximum = 10 nm as determined with a B&W Tek SpectraRadS Xpress (B&W Tek, Newark, DE, USA), photon flux dn p,em /dt = 10.7 µmol min −1 (i.e., 0.057 mol photons m −2 s −1 at the outlet of the waveguide) as determined by ferrioxalate actinometry [69]) equipped with a suitable waveguide (2 mm core diameter) within a glass tube (outer diameter = 11 mm, inner diameter = 9 mm). The outlet of the waveguide was placed in the center of the suspension to ensure that the light entrance is surrounded by the suspension in all three spatial directions.
In all experimental runs, the suspension was magnetically stirred for 2 h in the dark in order to establish the adsorption equilibrium. Subsequently, the light source was switched on and the stirred suspension was irradiated for 3 h. Samples were taken every 30 min and centrifuged for 5 min at 13,000 rpm. The supernatant solutions were filtered through syringe filters with 0.2 mm pore size and then diluted 1:20. Quantitative analysis of DCA and chloride was performed by high performance ion chromatography (HPIC) employing a Dionex ICS-1000 instrument (Thermo Fisher Scientific, Waltham, MA, USA) equipped with an anion exchange column (Dionex Ion Pac AS9-HC 2V 250 mm) in combination with a guard column (Dionex Ion Pac AG9-HC 2V 50 mm, Thermo Fisher Scientific, Waltham, MA, USA). The column temperature was set to 35 • C. The mobile phase (flow rate = 0.3 mL min -1 ) consisted of an aqueous solution of Na 2 CO 3 (8 mmol L −1 ) and NaHCO 3 (1.5 mmol L −1 ).

Conclusions
The experimental results presented above clearly evince that the rate of a photocatalytic reaction in suspension can be determined unaffected by the scattering properties of the photocatalyst when a black body photoreactor is employed. It was shown that experimental conditions can be achieved under which the rate of the photocatalytic degradation reaction, defined as the time derivative of the extent of reaction, is constant within the limits of experimental error. Employing a black body photoreactor, rates of conversion, and quantum yields can thus be determined with sufficiently good reproducibility.
At the risk of spreading platitudes, a few remarks on the comparative assessment of different photocatalysts will be given: (i) For comparative measurements in suspensions, it should be ensured that the photocatalyst is the only light-absorbing species. The probe compound as well as intermediates and products formed during the photocatalytic reaction must therefore be optically transparent at the wavelength used for the excitation of the photocatalyst.