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Removal of Cresols From Water by Packed Beds of Cyclodextrin-Based Hydrogels

A cyclodextrin-based polymer was prepared by crosslinking β-cyclodextrin with epichlorohydrin to be assessed as a sorbent material for cresols in packed-bed columns. Both Langmuir and Freundlich isotherms were appropriate to describe the sorption equilibrium in the conditions tested, and the thermodynamic parameters obtained for this process confirmed its exothermic nature with similar enthalpies (between − 6.8 and − 8.3 kJ/mol) for the three isomers. The removal of cresols from water was carried out in nine cycles of sorption–desorption in fixed-column experiments with the cyclodextrin hydrogel, achieving sorption capacities of 6.2, 11.6, and 15.1 mg/g for o-, m-, p-cresol, respectively. These differences in sorption capacities are due to the different chemical structures of cresols, that is, the relative position of the methyl and hydroxyl groups. However, similar sorption rates were observed for each isomer, with a mean value of 0.10 mg-cresol g-CDP–1 min–1 in all cases. The experimental data for the breakthrough and the elution curves have been successfully modeled by two effective two-parameter equations, a dose–response model for the sorption step and a pulse-peak model for the regeneration step. The cyclodextrin polymer matrix has been proven to be an effective a good sorbent material for removing cresols from water, exhibiting remarkable reusability performance and structural stability throughout the successive elution steps carried out with methanol.


Introduction
Adsorption is a mass transfer operation, included among the advanced (or tertiary) treatment technologies, applied to wastewater treatment and water purification usually to remove refractory pollutants. Through adsorption, certain constituents in the aqueous phase are transferred to the solid interface where they are retained, thus improving effluent quality. Therefore, the development of more selective adsorbents with high sorption capacities and good reusability properties is a matter of interest [1].
In particular, cyclodextrin-based hydrogels are synthetic polymeric adsorbents that have been extensively tested for this purpose [2][3][4]. Cyclodextrins (CDs) are cyclic oligosaccharides with already recognized capability as sorbents due to their amphiphilic nature by presenting a structure with a relatively hydrophobic cavity and hydrophilic edges. This makes CDs potentially useful for selective removal contaminants from water. On the other hand, given their high solubility in water, CDs are cross-linked into water-insoluble cyclodextrin-based polymers (CDPs) to enhance their usability for water treatment. For instance, taking advantage of the good sorption properties of CDs to dampen inhibitory effects by shock-loading events, CDP hydrogels have also been used as carrier particles for attached-growth of phenol-degrading bacteria in bioreactors [5,6]. The uses of cyclodextrin crosslinked polymers as sorbents of aromatic compounds have been known for years [4,7] and their application to the treatment of phenolic resin plant wastewaters has also been previously reported [8]. Recently an excelent review on recent developments of cyclodextrin-based materials has been published [9]. However, most studies refer to batch applications, but relatively few addressing the reusability of CDPs in adsorbers with continuous influent flow [10]. Even though some other affordable materials, such as coconut charcoal, might show a better adsorption performance, this investigation demonstrates that these hydrogel sorbents are stable through successive sorption-desorption cycles.
The present work addresses the performance of a CDP applied for the removal of cresols from water in several cycles of sorption-desorption in fixed-column experiments. Cresols are methylated derivatives of phenol which include three isomers: 2-methylphenol (ortho-cresol, o-cresol), 3-methylphenol (meta-, m-), and 4-methylphenol (para-, p-). As other phenolic compounds, cresols are extensively used as organic reagents in different manufacturing industries, and their discharge to the aquatic environment is a matter of concern [11]. The breakthrough curves measured for each isomer are well described by a dose-response model, whereas a pulse-peak model fits adequately the corresponding regeneration profiles obtained by elution with methanol. In addition, the sorption equilibrium data of o-, m-and p-cresol on the CDP have been fitted to the Freundlich and Langmuir isotherm models and the thermodynamic parameters of these processes have been calculated.
Cresols were determined by UV-vis spectrophotometry (HP 8452A, USA) using a diode-array detector. Absorbance measurements were made at 270, 272, and 278 nm for o-, m-and p-cresol, respectively.

Sorbent
A cyclodextrin-based polymer (CDP) was tested as a sorbent for o-, m-and p-cresol in packed-bed experiments. Practically spherical particles of CDP hydrogel were prepared by oil-water suspension polymerization, using a CD:epichlorohydrin molar ratio of 11:1 (feed basis), according to method described by Romo et al. [12]. The swelling capacity of CDP was 5.1 g-water/g-dry gel, whereas a composition of 58.0 wt.% of cyclodextrin (measured by CHN elemental analysis). Previous characterization of this CDP hydrogel gave a swollen particle density of 1055 g/L, that is, a bulk density of 765 g/L for a bed voidage of 27.5% [10].
The CDP beads were wet sieved to separate the fraction used in this study, with a particle size range of 1.00-1.25 mm.

Sorption Isotherms
Batch experiments at natural pH (about 6.6) were carried out to determine the sorption isotherms of the three cresols by CDP at 15, 25, 35 and 45 °C. To this end, known amounts of dry CDP particles (from 20 to 250 mg) were added to 50 mL of aqueous solutions of cresols with different initial concentrations. Amber glass bottles (Supelco, 2 fl oz, USA) with septum-sealed caps (Supelco, Mininert valve, USA) were used. The systems were kept stirred for 3 h (Velp Scientifica, Multistirrer 15, Italy) inside a 150-L insulated chamber with forced-air heating and temperature control (Crouzet, CTD43, France). Preliminary kinetic tests (data not showed) indicated that equilibrium was achieved in less than one hour in all cases.
Once equilibrium was reached, the remaining cresol was analyzed in each supernatant, and the sortion capacity (q) calculated as follows: where V was the volume of aqueous solution, W CDP the dry weight of sorbent, and C 0 and C* the initial and equilibrium concentrations of cresol, respectively.
where K F and n were the parameters of Freundlich isotherm, and K L and q M the Langmuir ones.
From the relationship between equilibrium and thermodynamics, the sorption equilibrium constant (K S , dimensionless) can be expressed as follows: where ρ W is water density at each temperature. Hence, experimental data were fitted to Eq. (4) to determine the sorption thermodynamic parameters for each sorbate: enthalpy (ΔH 0 ), entropy (ΔS 0 ), and free energy (ΔG 0 ).

Sorption-desorption experiments
Three packed bed columns (Supelco, Omnifit 15-mm glass column, USA) were operated in an isothermal chamber at 25 ± 1 ºC. Each column was filled with 1.700 ± 0.002 g of hydrogel (dry basis), which yielded a bed height of about 75 mm after swelling of CDP beads (bulk density 765 g-swollen gel/L, bed voidage 0.275). A previous preparation of the each bed was carried out by flowing deionized water through the columns to allow the equilibrium swelling of CDP particles. Separate stock solutions (1.0 mmol/L) were used as influent feed, one for each cresol and column. Each so-prepared influent was delivered by a multichannel peristaltic pump (Masterflex L/S Cole Palmer, USA) at a flow rate of 2.60 mL/min (i.e. hydraulic residence time 5.10 min) through each bed. The experiments were performed at the natural pH of the cresol solutions. In each operating cycle, once sorbent saturation was achieved, beds were regenerated by elution with methanol at a flow-rate of 2.60 mL/min. Methanol had already shown better performance than ethanol and isopropanol in the regeneration of phenol-saturated CDP beds [10]. Effluent samples were periodically collected from each column and stored in glass vials until further analysis.

Modeling of breakthrough and elution curves
The breakthrough and elution profiles were described as a function of time (t) by a dose-response curve (Eq. 5) and a pulse-peak model (Eq. 6), respectively.
being C the concentration of cresol in the effluent; C 0 the concentration at time zero; t 1/2 the time needed for C to become equal to C 0 /2; b the sharpness coefficient; and k, c and d are fitting parameters. Therefore, a two-parameter equation is assumed for breakthrough curves, and a threeparameter model for regeneration curves. However, considering the mass conservation law for both steps of adsorption (Eq. 7) and desorption (Eq. 8), a boundary condition can be applied to fix k so that Eq. (6) finally has two independent adjustable parameters (c and d).
where W 1 and W 2 are the amounts of cresol adsorbed and desorbed, respectively; and Q 1 and Q 2 the influent and elutant flow rates, respectively.
The quality of the proposed models was assessed by multiple nonlinear regression analysis by minimizing the residuals between the experimental and predicted values. The standard errors of the estimate (SSE) were calculated according to: where N is the number of data used (in fact, N -2 represents the number of degrees of freedom for each analysis model). A detailed description of the modeling approach can be found in Peñas et al. [10].

Sorption isotherms
The Freundlich and Langmuir isotherms (Eqs. 2 and 3, respectively), the most-widely used models, were employed to describe the sorption equilibrium data of cresols onto the CDP beads. The best-fitted parameters obtained in the batch assays are listed in Table 1 for both models, and the standard errors of the estimate (SSE) have also been included for comparison. Standard errors are indicated in parentheses where applicable. In general, a very acceptable fit was obtained with both models. Interestingly, Rekharsky and Inoue [13] reported virtually equal values for the inclusion complexation of p-cresol with β-cyclodextrin (1:1 molar ratio) at 25 °C.
As representative examples, Fig. 1 shows the experimental equilibrium data from the batch sorption experiments at the two lowest temperatures assayed (15 and 25 °C). The respective solid curves were calculated by applying the corresponding isotherm models (Eq. 2 and 3, respectively), and are included to illustrate the quality of the fit. The same trend was observed for the other temperatures. For each individual cresol, a joint representation of the four isotherms leads to a confusing graph, with data points very close to each other, so this type of graph has been omitted.
The Langmuir parameter q M represents the theoretical maximum amount of sorbate per unit mass of sorbent forming a complete monolayer, and is related to the maximum sorption capacity of the solid. As observed, for each temperature in the tested conditions, this maximum capacity was higher with p-cresol than with m-cresol, and this in turn was higher than that of o-cresol. According to our experimental results (not shown), the β-CD/cresols interaction constants at 25 °C (values in L/mol) vary in the order: Nevertheless, in addition to the host-guest inclusion complexation, these sorbates can also establish other interactions with the crosslinked networks. Thus, it is shown that there is some synergistic behaviour when both are considered. As is well known, aromatic molecules and residues can be encapsulated within cyclodextrin rings. For instance, the formation of a host-guest inclusion complex between m-cresol into the hydrophobic cavity of β-CD with 1:1 stoichiometry has been recently confirmed by several experimental techniques [14]. Nevertheless, the interactions of such phenolic sorbates with the hydrogel crosslinked networks (also known as 'secondary' cavities) by means of hydrogen bonding cannot be discarded either [15]. The decreasing trend in the q M values with rise in temperature is consistent with the exothermic nature of the sorption process of cresols onto CDP matrices [15]. Likewise, the sorption thermodynamic parameters obtained from Eq. (4), summarized in Table 2, confirm the spontaneity of this process and also its exothermic nature. As observed, the corresponding values are very close to each other, showing few differences between them. These results are quantitatively similar to those reported for the adsorption of cresols on polymeric resin adsorbents [16].

Sorption Experiments
The experimental data for the breakthrough curves obtained for the sorption of cresols onto the CDP beds were satisfactorily fitted to the dose-response model. The corresponding fitting parameters are listed in Table 3 for the nine cycles performed for each cresol. In addition, the amount of retained sorbate is obtained from Eq. (7). As observed, acceptable fit to Eq. (5) was achieved in all systems (calculated determination coefficients, R 2 > 0.99). As a thumb rule, for each cresol, the fitting parameters (t 1/2 and b) exhibited a slight decreasing trend as cycle number increases. The calculated t 1/2 values for o-cresol   (average 30.6 ± 0.8 min) were significantly lower than those for m-cresol (59.6 ± 0.8 min) and these in turn lower than those for p-cresol (72.1 ± 6.5 min). This implies that the CDP matrix becomes saturated first with o-cresol, then with m-cresol, and finally with p-cresol. However, this does not mean that the sorption kinetics become faster for the former or, consequently, slower for the latter. It should be noted that the amounts sorbed in each cycle were low for o-cresol (average 10.6 ± 0.1 mg), medium for m-cresol (19.8 ± 0.6 mg), and higher for p-cresol (25.7 ± 1.1 mg). Thus, the average sorption capacities of the isomers in these experimental conditions were 6.2 ± 0.1 mg/g-CDP for o-cresol, 11.6 ± 0.3 mg/g for m-cresol, and 15.1 ± 0.6 mg/g for p-cresol. In fact, keeping in mind that t 1/2 represents the half time to reach sorbent saturation, the average sorption rate (estimated as ½ W ads t 1/2 -1 ) reached a very similar value in the three cases (0.172, 0.166, and 0.178 mg/min for o-, m-, and p-cresol, respectively). In other words, a strong correlation between t 1/2 and W ads was found (R 2 = 0.9888). This can be explained by considering that the isomers present practically the same molecular volume, 0.1088 ± 0.0003 nm 3 [17], and the available sorption sites of the CDP bed do not change during the experiments. Therefore, once the most accessible external sites are occupied, molecular diffusion through the CDP matrix is easier for p-cresol than for o-cresol due to their respective molecular structures (the relative position of methyl and hydroxyl groups) and, at the same time, more sites are suitable for the sorption. Note that the effective diameters of cresols are of the same order (slightly higher) than that of β-CD cavities.
Representative examples of the experimental data and the predicted breakthrough curves (calculated from Eq. 5) are shown in Fig. 2. No significant differences were observed from test run 1 to 9 with each sorbate used. The good reusability of the CDP sorbent is evidenced for m-cresol (Fig. 2a) with three different sorption cycles (test runs 1, 5, and 9). The effect of the sorbent-sorbate interaction is visualized (Fig. 2b) for the same operating cycle (test run 3). Similar trends were found for each cresol and for each test run performed.
There is relatively few research on sorption of cresols in fixed-bed columns. A comparative of maximum sorption capacities for several adsorbents towards cresols is listed in Table 4. All of the references included, except that concerning this study, were performed in batch systems. It can be observed that large differences are found in the experimental conditions applied by each case. Likewise, El Naas et al. [33] reported adsorption capacities up to 63 mg of total phenols per gram of a granular activated carbon when studying the removal of phenols from an oil refinery wastewater in fixedbed column experiments at 25 °C. Unfortunately, aggregate values are given for all phenols present in the industrial effluent treated, but specific figures for each compound are not available.
In addition, experimentation with repeated adsorption cycles is less common. For instance, the retention of p-cresol on two different modified vermiculites, even while achieving good initial sorption capacities, showed a marked decrease in reusability after only three cycles of use [27]. After four cycles of regeneration with an ethanol/acetic acid solution, the adsorption capacity of imprinted nanocomposites from biomass bacterial cellulose was reduced to 10% for o-cresol and about 6-7% for m-cresol and p-cresol [23].
On the other hand, in view of the scarcity of works with cresols and cyclodextrin-based sorbents, it is interesting to point out some recent studies on phenol adsorption on these type of materials. Thus, Peng et al. reported a maximum adsorption capacity for phenol of 36.0 mg/g with a modified β-cyclodextrin chitosan composite in batch sorption assays at 25 °C and pH 6 [34]. A sorption capacity of 29.6 mg of phenol per gram of sorbent was reached in a packedbed filled with a similar CDP treating a synthetic phenolic

Desorption Experiments
The elution profiles measured are very asymmetric, with the left-hand side increasing sharply to a maximum (at time t M ) and then the right side decreasing smoothly and asymptotically to zero. Each profile showed this maximum concentration peak at around 5-10 min after turning on the eluent pump, and reaching several times the initial concentration value used in the corresponding sorption test (this maximum height is here defined as C/C 0,M ). The experimental data for the elution of the three isomers from the CDP beds were also successfully fitted (calculated determination coefficients, R 2 > 0.98) to the pulse-peak model (Eq. 6). The results obtained are listed in Table 5: the independent parameters (c and d; therefore, also N -2 degrees of freedom), the dependent variable k (derived from the boundary condition given by Eq. 8), and the calculated values of peak time and peak height (t M and the C/C 0,M , respectively). It is noteworthy that the average of the calculated t M values did not vary significantly from one isomer to another: 8.02 ± 0.36 min for o-cresol, 7.80 ± 0.23 min for m-cresol, and 8.13 ± 0.30 min for p-cresol. In contrast to t M , the C/C 0,M values obtained did appear to have a clear relationship with the sorption capacities of CDP found for each isomer. Thus, mean C/C 0,M values of 1.95 ± 0.10 were estimated for o-cresol, 3.72 ± 0.22 for m-cresol, and 4.96 ± 0.27 for p-cresol.
As illustrative examples, the experimental data of elution curves with the three eluents for the same operating cycle are shown in Fig. 3. The corresponding profiles calculated by Eq. (6) have been plotted for clarity. As was the case with the breakthrough curves, for each cresol isomer, very similar desorption profiles were found from test run 1 to 9 (see Fig. 3a for m-cresol). The effect of the type of sorbate on the elution profile is depicted for the same cycle (test run 3) in Fig. 3b. Despite the difference in amplitude in the profiles for each isomer, the time needed for achieving the desorption of the half amount of sorbate retained at each CDP bed was calculated to be relatively constant (between 13.5 and 14 min). Again, a similar pattern was observed for each isomer and for each test run carried out.
Likewise, the structural appearance of the three CDP beds (one for each isomer tested) remained unchanged throughout the nine sorption-desorption cycles. The same finding was observed when almost up to thirty cycles with phenol were performed with other similar CDP bed [10], being that favorable condition attributed to the relative similarity in solvent polarities between methanol and water. Considering this fact, together with the adsorption capacities achieved, the present work demonstrates that CDPs would be good candidate materials to be used in multiple-cycle operations for the removal of cresols from water. Even though some other affordable materials, such as coconut charcoal, might show a better adsorption performance, the present investigation shows that these hydrogel sorbents are stable through successive sorption-desorption cycles.

Conclusions
The sorption of cresol isomers in packed beds composed of hydrogel beads of a cyclodextrin-based polymer and their regeneration have been studied for nine operating cycles. In addition, it has been shown that both Langmuir and Freundlich isotherms yield appropriate fittings in the range of conditions studied. Higher cresol concentrations in the batch experiments would be required to ascertain whether this material behaves as a homogeneous (i.e. Langmuir-like) one. Nevertheless, the sorption experiments carried out allowed to obtain the thermodynamic parameters of the process and confirm its exothermic nature with similar enthalpies for the three isomers. No significant different profiles for both sorption and desorption steps were observed under the experimental conditions applied. The mean sorption capacities of CDP beds were found to be 6.2 mg/g-CDP for o-cresol, 11.6 mg/g for m-cresol, and 15.1 mg/g for p-cresol. Nevertheless, no substantial differences were observed in the sorption rates for each isomer, giving a mean value of about 0.10 mg-cresol g-CDP -1 min -1 in all systems. An analogous pattern was seen in the regeneration step, where half of the retained isomer on CDP bed was always released in a similar elution time (approximately 14 min). The differences in cresol sorption capacities of the CDP are attributable to the different chemical structures of the isomers. The experimental data for the breakthrough and the elution curves have been successfully modeled by two effective two-parameter equations, a dose-response model for the sorption step and a pulse-peak model for the regeneration step. The CDP matrix has been proven to be an effective a good sorbent material for removing cresols from water, exhibiting remarkable reusability performance and structural stability throughout the successive elution steps carried out with methanol.