Effectiveness of metal oxide catalysts for the degradation of 1,4-dioxane

Abstract

1,4-dioxane, commonly used as a solvent stabilizer and industrial solvent, is an environmental contaminant and probable carcinogen. In this study, we explored the concept of using metal oxides to activate H₂O₂ catalytically at neutral pH in the dark for 1,4-dioxane degradation. Based on batch kinetics measurements, materials that displayed the most suitable characteristics (high 1,4-dioxane degradation activity and high H₂O₂ consumption efficiency) were ZrO₂, WO_x/ZrO₂, and CuO. In contrast, materials like TiO₂, WO₃, and aluminosilicate zeolite Y exhibited both low 1,4-dioxane degradation and H₂O₂ consumption activities. Other materials (e.g., Fe₂O₃ and CeO₂) consumed H₂O₂ rapidly, however 1,4-dioxane degradation was negligible. The supported metal oxide WO_x/ZrO₂ was the most active for 1,4-dioxane degradation and had higher H₂O₂ consumption efficiency compared to ZrO₂. In situ acetonitrile poisoning and FTIR spectroscopy results indicate different surface acid sites for 1,4-dioxane and H₂O₂ adsorption and reaction. Electron paramagnetic resonance measurements indicate that H₂O₂ forms hydroxyl radicals (˙OH) in the presence of CuO, and unusually, forms superoxide/peroxyl radicals (˙O₂⁻) in the presence of WO_x/ZrO₂. The identified material properties suggest metal oxides/H₂O₂ as a potential advanced oxidation process in the treatment of 1,4-dioxane and other recalcitrant organic compounds.

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1. Introduction

1,4-dioxane is an industrial solvent,¹ a byproduct present in personal-care products,¹ and a suspected carcinogen with US state maximum contaminant limits that are frequently below 1 ppb. Because it is used to stabilize chlorinated volatile organic compound (CVOC) solvents,^1–5 1,4-dioxane was found by Adamson et al. to co-occur at 76% of California sites containing trichloroethane, and at 68% of sites containing 1,1-dichloroethene.² Extrapolating this co-occurrence problem to the 15 000–25 000 US sites that are contaminated with CVOCs,⁶ 1,4-dioxane is likely widespread.

A number of advanced oxidation processes (AOPs) have been investigated for 1,4-dioxane remediation, including ex situ UV oxidative processes (UV/H₂O₂, UV/ozone),⁷ photocatalysis,^8–10 or sonolysis and photocatalysis.¹¹ A few studies looked at catalytic destruction of 1,4-dioxane, but most required the addition of high-energy resources such as UV light,^12,13 ultrasonic waves,¹⁴ or electricity,^15–17 which are not only costly from an energy perspective, but may also require the use of complicated reactor configurations and may not be suitable for universal treatment of 1,4-dioxane contamination (e.g. in chemical plumes).

“Dark” (non-photocatalytic) heterogeneous catalysis, which does not require additional energy sources, may be a more passive and more economically practical approach to treating 1,4-dioxane in water. Efforts have been made in the past to study the activation of chemical oxidants for AOP using materials as a heterogeneous form of Fenton's reagent, but few have focused much on 1,4-dioxane nor provided an experimental understanding of the surface chemistry.^18,19 CuO has been investigated using ozone as oxidant, and implicated Lewis acid sites for the decomposition of ozone.²⁰ A Pd-based catalyst was reported effective for degrading 1,4-dioxane using peroxymonosulfate, and suggested surface-bound radicals were responsible for degradation.²¹ Two studies discussed using H₂O₂; one a titanosilicate zeolite that was slightly active in water at 60 °C,²² and another concerning Fe(II)-containing clays that showed degradation activity on the order of several days.²³ Unexplored for 1,4-dioxane degradation and other contaminants are a number of materials reported to be able to nonphotocatalytically catalyze the dark dissociation of H₂O₂, such as ZrO₂ ²⁴ and TiO₂.²⁵ Furthermore, any materials properties of these unconventional H₂O₂-active materials which allow them to degrade organics is unclear.

In this study, we screened commercially available relatively inexpensive metal oxide H₂O₂-active catalysts to establish a set of basic data for the degradation of aqueous-phase 1,4-dioxane using H₂O₂ at mild ambient conditions and in the dark. A 1,4-dioxane degradation rate constant was measured for each material at room temperature and atmospheric pressure, and at near-neutral pH. H₂O₂ consumption activity (quantified as a rate constant) and consumption efficiency (quantified as moles of 1,4-dioxane degraded per mole H₂O₂ consumed) were also determined. To understand the essential surface properties that direct the degradation process, we further analyzed the materials using in situ Fourier-transform infrared (FTIR) analysis of acid sites using pyridine, acid site poisoning catalytic tests using acetonitrile, and electron paramagnetic resonance (EPR). Based on these results, we proposed a reaction mechanism to explain the observed material-dependency of 1,4-dioxane degradation.

2. Materials

CuO (>97%) and γ-Al₂O₃ (>97%) were used as received from Strem Chemicals. ZrO₂ and TiO₂ P25 were obtained from Evonik. Fe₂O₃ (hydrated, catalyst grade 30–50 mesh, crushed prior to characterization and kinetic experiments), WO₃ (nanopowder), Zeolite Y (hydrogen, 30 : 1 SiO₂ : Al₂O₃), CeO₂ (99.95%, nanopowder), dichloromethane (chromasolv, 99.9%), and 1,4-dioxane (>99.5%), H₂O₂ (30%), and TiOSO₄ (∼15 wt% in dilute sulfuric acid) were used as received from Sigma Aldrich. A zirconia-supported tungsten oxide material (“WO_x/ZrO₂”, 20 wt% WO₃ content) was obtained from MEI Chemicals and used as-received. Specific surface areas (SSA) of the metal oxide materials were evaluated on a Quantachrome Autosorb IIIB using five-point BET calculations on samples degassed at 350 °C overnight. 5-Tert-butoxycarbonyl-5-methyl-1-pyrroline-N-oxide (BMPO) was obtained from Enzo Life Sciences. Deionized water was used in all experiments.

3. Analytical methods

3.1 Catalytic activity testing

For kinetic experiments, 171 mL of deionized (DI) water, 0.4 μL of 1,4-dioxane ([1,4-dioxane]₀ = 27 μM, 2.3 ppm), and 0–600 μL of 30% H₂O₂ ([H₂O₂]₀ = 0–30 mM) were added to a 250 mL Boston round bottle. After stirring, a ∼2 mL aliquot was taken from the reactor for baseline measurements of H₂O₂ and 1,4-dioxane. The catalyst was added to the reactor, which was then sealed with a septum, covered in foil to shield from ambient light, and magnetically stirred at 600 RPM. The amount of added catalyst was chosen such that the total exposed oxide surface area in the reaction medium was the same between experiments (475 m² per L-fluid, Table S1†). Aliquots (∼1.5 mL) of reaction fluid were filtered with a 0.2 μm syringe filter to remove solid catalyst prior to H₂O₂ and 1,4-dioxane concentration measurements. Each reaction was repeated three times. No degradation was observed in experiments where only 1,4-dioxane and catalyst were present.

Because of order-of-magnitude differences in initial concentrations, the disappearance of H₂O₂ and 1,4-dioxane were both modeled as pseudo-first order processes, where the rate of disappearance of reactant X (either H₂O₂ or 1,4-dioxane), r_X, is given by

where t is time, C_X is the concentration of reactant X, and k_meas,X is the measured pseudo-first order rate constant, which can be found from integrating eqn (1) to obtainwhere C_X,0 is the initial concentration of the reactant.

In order to better compare intrinsic catalytic activity, we report the pseudo-first order rate constant normalized by added catalyst surface area for each reagent for each catalyst, k_X, since only exposed catalyst sites should be active. k_X is given by

where C_cat is the concentration of catalyst surface area in the reactor (units of m² mL⁻¹), given by eqn (4)where SSA_cat is the specific surface area of the catalyst (units m² g⁻¹, as determined by BET, see Table S1†), g_cat is the grams catalyst added to the reactor (Table S1†), and V_reactor is the liquid reaction volume.

Selective site poisoning experiments were conducted using acetonitrile (which can chemisorb onto Lewis acid sites²⁶), in which the catalysts were premixed with 318 μL of 0.1 M acetonitrile stock solution (final [acetonitrile] in reactor = 186 μM).²⁷ Residual activity is defined as

3.2 H₂O₂ quantification

H₂O₂ remaining in the aliquots was quantified using titanium oxysulfate (TiOSO₄, ∼15 wt% in dilute H₂SO₄). TiOSO₄ reacts with H₂O₂ to form the yellow-colored product perititanic acid, quantifiable using UV-vis.²⁸ A standard curve was made using 0–80 μM H₂O₂ to verify that the response was linear at the maximum extinction (at λ = 405 nm). Reaction samples were diluted up to 20× to verify that absorbance at λ = 405 nm was in the standard.

3.3 1,4-Dioxane quantification

The concentration of 1,4-dioxane was determined as detailed by Li et al.²⁹ Briefly, 0.5 mL of reaction aliquot and 0.5 mL of dichloromethane (DCM) was added to an autosampler vial and vigorously shaked for at least 30 seconds to extract the 1,4-dioxane into the DCM phase. Following freezing at −20 °C for at least 1 hour, the liquid DCM was decanted from the vial and put into a fresh autosampler vial containing ∼10 mg of sodium sulfate to sequester any residual water. These samples were then analyzed via GC-MS. A calibration curve was prepared using this method with 0–3200 ppb 1,4-dioxane in deionized water.

3.4 Determination of mass transfer resistances

To ensure the reported rate constants were kinetically limited, we evaluated external mass transfer resistances as we have done previously.^30,31 We note that in this system, there is no gas phase reactants, therefore k_gl was neglected. Fig. S1,† prepared using CuO, one of the most active catalysts for H₂O₂ degradation, shows a linear increase in the measured rate constant with added catalyst, indicating there were no external mass transfer limitations in this range. The circled point corresponds to the SSA loading chosen for all other reactions.

To assess any internal mass transfer resistances, we determined the Weisz–Prater criterion (C_WP) for both the first-order degradation of H₂O₂ and 1,4-dioxane according to^32,33

where k′ is the catalyst mass normalized rate constant (m³ s⁻¹ g_cat⁻¹), ρ_c is the catalyst density (g m⁻³), R is the pellet radius (m, conservatively assumed to be 1 mm for all catalysts), and D_e is the effective diffusivity of H₂O₂ and 1,4-dioxane in the pores (assumed to be equivalent to H₂O₂ and 1,4-dioxane diffusivity in water, 5.0 × 10⁻⁶ m² h⁻¹ and 6.0 × 10⁻⁸ m² h⁻¹ respectively). As shown in Table S2,† the Weisz–Prater criterion was less than one for all materials, which implies that the catalysts' activities were not limited by internal diffusion.

3.5 EPR experiments

For the spin-trap experiments, 4 mM of CuO, WO_x/ZrO₂, or ZrO₂ was added to a s 83 mM H₂O₂ and 5–10 mM BMPO solution, then mixed for ∼2 min. Transient radical species rapidly react with BMPO, forming stable adducts.^34–37 15 μL of the reaction mixture was sampled and sealed with Critoseal. EPR spectra of the spin trapped radicals were obtained using a Bruker EMX spectrometer at room temperature. EPR measurements were taken using a frequency of 9.30 GHz, power of 20 mW, modulation frequency of 100 kHz, modulation amplitude of 0.1 G, and time constant of 0.33 s. No radicals were detected in control solutions without metal oxide.

Freeze trapping was also attempted for direct detection of radicals. In these experiments, the 5 mm o.d. EPR tubes were rapidly frozen in an EtOH/dry ice bath before transferring into liquid N₂. The measurements were conducted at 115 K using a frequency of 9.28 GHz; power of 1 mW; modulation frequency of 100 kHz, modulation amplitude of 2G, and time constant of 0.33 s.

3.6 Pyridine-FTIR

For the pyridine-FTIR experiments, the sample was pressed into a 13 mm diameter disk and analyzed in a homemade cell attached to a closed circulation system. Before pyridine adsorption, the cell was heated to 150 °C for 30 min at low pressure (<10⁻³ Pa) then allowed to cool to 25 °C. A spectrum was recorded as the background using a Bruker Tensor 27 FTIR spectrometer in transmittance mode. Gas-phase pyridine was then contacted with the sample for ∼20 min, and then the chamber evacuated at 150 °C for 30 min at low pressure (<1.0 × 10⁻³ Pa) to remove pyridine that was physically adsorbed before a FTIR spectrum of the chemisorbed pyridine was collected. Spectra were also taken after the sample was cooled to 25 °C.

For experiments looking at both pyridine and water, gas-phase water (∼1 atm) was added to the cell after the pyridine step. The water atmosphere was maintained for ∼20 min at 25 °C and then desorbed at 25 °C and 150 °C. The sample was brought to 25 °C, and an additional spectrum collected.

The Lewis acid site concentration is given by³⁸

where C_Lewis is Lewis acid site concentration (mmol g_catalyst⁻¹), R is the catalyst radius (cm), I is the integration of the Lewis band (cm⁻¹), W is the weight of disk (mg), and the factor 1.42 mol cm⁻¹ is the extinction coefficient of pyridine adsorbed to an acid site.³⁸ The W used for the experiments for CuO, ZrO₂, and WO_x/ZrO₂ were 4.17, 27.2, and 39.5 mg respectively, and the I were found to be 1.095, 4.173, and 17.317 cm⁻¹ respectively.

4. Results and discussion

Fig. 1a shows the dark catalytic activities for H₂O₂ consumption alone (without 1,4-dioxane). CeO₂, Fe₂O₃, and CuO all have high reaction rate constants, which generally agree with reported values of these Fenton-like materials, i.e., those that activate H₂O₂ via formal oxidation/reduction of the metal sites.^25,39 The exception is CuO, which was slower than other reports (Table S3†), which may be due to differences in catalyst and H₂O₂ concentrations between studies. ZrO₂ and TiO₂ showed H₂O₂ degradation ability, in agreement with previous reports.^{24,25,39–41} SiO₂ and Al₂O₃ exhibited only trace activity (also in agreement with literature),²⁵ as was the case with zeolite Y. Monometallic WO₃ was also nearly inactive.

Fig. 1 Pseudo-first order rate constants normalized by catalyst surface area for H₂O₂ consumption ([H₂O₂]₀ = 15 mM, pH = 6.5) in the (a) absence and (b) presence of 1,4-dioxane ([1,4-dioxane]₀ = 27 μM). Panel (b) shows the rate constant for H₂O₂ consumption plotted against the 1,4-dioxane degradation rate constant. (c) Stoichiometric efficiency (defined as moles 1,4-dioxane degraded per mole H₂O₂ consumed) calculated for catalysts active for 1,4-dioxane degradation at 10–12% conversion.

Fig. 1b shows catalytic activities for the H₂O₂ consumption in the presence of 1,4-dioxane, and catalytic activity for 1,4-dioxane degradation. We denote the “best” 1,4-dioxane degradation catalysts as those that quickly degrade 1,4-dioxane (high k_diox) while consuming low amounts of H₂O₂ (low k_H2O2), i.e., those closest to the lower right hand side of the semi-log k-by-k plot. Catalytic activities for H₂O₂ consumption did not generally change in the presence of 1,4-dioxane (comparing Fig. 1a and b). Materials weakly active for H₂O₂ consumption (Al₂O₃, SiO₂, and WO₃) consumed H₂O₂ more rapidly, except for zeolite Y, which became less active; all these showed minimal 1,4-dioxane degradation ability.

Catalysts most active for H₂O₂ consumption were not the most effective at degrading 1,4-dioxane; Fe₂O₃ and CeO₂, the catalysts with the highest k_H2O2, were inactive for 1,4-dioxane, and could be due to the conversion of H₂O₂ to nonreactive species under these reaction conditions (neutral pH). Materials that had the highest k_diox values were (listed in order of decreasing activity) WO_x/ZrO₂ ≫ CuO > ZrO₂ ≫ TiO₂. Their H₂O₂ consumption activity was also less than those of Fe₂O₃ and CeO₂.

We calculated the stoichiometric efficiency for the four catalysts most active for 1,4-dioxane degradation during the batch reactions (Fig. 1c). Under these conditions, CuO was the most H₂O₂-efficient, followed by TiO₂, WO_x/ZrO₂, and ZrO₂. These values are on the same order of magnitude as those measured by Sedlak and co-workers for the degradation of phenol using H₂O₂ over a silica–Fe catalyst at neutral conditions (∼0.20–0.30%).^42,43 A direct comparison of these results to other materials is made with caution, as the initial reactant amount and reactant type (50–250 mM H₂O₂ and 0.5 mM phenol vs. 15 mM H₂O₂ and 27 μM 1,4-dioxane) differ.

To further understand the surface mechanism, we explored the effects of initial H₂O₂ concentrations (1.5–30 mM) using a Langmuir–Hinshelwood–Hougen–Watson (LHHW) bimolecular surface reaction model, which assumes the two reactants (H₂O₂ and 1,4-dioxane) compete to adsorb to the same catalytic sites. The rate of H₂O₂ consumption (r′_H2O2) increased before plateauing at high [H₂O₂]₀ for WO_x/ZrO₂, CuO, and ZrO₂, which was indicative of saturation coverage of the active sites at high H₂O₂ concentrations (Fig. S2a†). The 1,4-dioxane degradation rate (r′_1,4-dioxane), however, also increased and remained pseudo-first order with respect to [H₂O₂] (Fig. S2b†), which suggests that 1,4-dioxane adsorption (and subsequent reaction) sites are not blocked at high H₂O₂ concentrations, and implies that the adsorption and reaction occurs on sites different from those for H₂O₂ adsorption/reaction (for WO_x/ZrO₂, CuO, and ZrO₂).

We also examined the radicals formed from H₂O₂ activation by the 1,4-dioxane-active catalysts. Although EPR does not necessarily provide direct evidence of surface generation of radicals, it can reveal what radicals are generated in solution with the use of the spin-trap reagent. BMPO, the spin-trap reagent used here, rapidly reacts with otherwise transient radicals to form stable radical adducts with ˙OH and ˙O₂⁻ species. The hyperfine structures of the BMPO adduct are characteristic of those of BMPO/˙OH (Fig. 2a), which fit well with two conformers with similar hyperfine splittings due to the nitrogen, the β hydrogen, and one of the γ hydrogen atoms,^35,44 indicating formation of ˙OH radical over CuO. The EPR signal did not change with the addition of superoxide dismutase (“SOD,” an enzyme which rapidly and selectively converts ˙O₂⁻ to O₂ or H₂O₂), confirming that CuO did not generate ˙O₂⁻ (Fig. S3†). This is in contrast to a recent study using ozone to degrade 1,4-dioxane over CuO, which formed primarily superoxide radical.²⁰ However, as hydroxyl radical is amongst the strongest oxidants (Table S4†), it is likely responsible for the high 1,4-dioxane degradation ability of CuO.

Fig. 2 BMPO-trapping of radical species in the H₂O₂ consumption with (a) CuO (red), (b) ZrO₂ (blue) and (c) WO_x/ZrO₂ (black). Spectra following freeze trapping over (d) CuO (red), (e) ZrO₂ (blue) and (f) WO_x/ZrO₂ (black). The small features at 3320 G for traces (d) and (e) are artifacts from the EPR sample cavity.

The spectra of BMPO-radical adducts were significantly different when ZrO₂ catalysts were exposed to H₂O₂ (Fig. 2b). The hyperfine structures of the EPR spectrum (Fig. 2b) indicates the formation of BMPO/˙O₂⁻.³⁵ BMPO/˙O₂⁻ adduct was also observed in the reaction of WO_x/ZrO₂ (Fig. 2c) and the spectrum fit well with two conformers with similar hyperfine splittings due to the nitrogen and the β hydrogen atoms (Fig. S4a and b†). Moreover, addition of SOD significantly decreased the amount of BMPO-trapped radical (Fig. S3†), corroborating that superoxide is the primary radical generated by ZrO₂ from H₂O₂. This observation is consistent with a previous work.⁴⁵

Superoxide radicals have a lower oxidation potential compared to H₂O₂ ^46,47 (Table S3†), and are considered relatively unreactive.⁴⁸ It is surprising that this species (and not ˙OH) is generated by WO_x/ZrO₂, the most active catalyst tested for 1,4-dioxane degradation. This suggests some catalytically beneficial feature of ZrO₂-supported WO_x domains that is absent from ZrO₂ and from WO₃. Direct freeze-trapping EPR measurements, in which H₂O₂/metal oxide suspensions are frozen and analyzed for any generated radicals (without using a spin-trap reagent), showed signals for superoxide radicals for WO_x/ZrO₂ (Fig. 2f). The g_x/y = 2.007 (3305 G) and g_z = 2.088 (broad peak centered at 3177 G) are typical of superoxide anion radicals in solution. The narrow peak at 3263 G (g_z = 2.032) and trough at 3315 G (g_xy = 2.002) are likely due to a WO_x/ZrO₂ surface-bound peroxyl radical whose g values, particularly g_z, are perturbed due to its binding to the surface of the catalyst and much less spin–orbit coupling than that of free superoxide radical.⁴⁹ The EPR spectrum can be fit well with a combination of these two types of radicals (Fig. S4c†). No signals were detected in freeze-trapping of ZrO₂ and H₂O₂ even though ˙O₂⁻ was spin-trapped using BMPO in the same reaction, suggesting that WO_x/ZrO₂ can better stabilize ˙O₂⁻ radicals compared to ZrO₂. In the CuO reaction with H₂O₂, the formation of ˙OH was too transient to be directly freeze-trapped.

Recognizing that 1,4-dioxane was historically used as a CVOC stabilizer due to its ability to complex with AlCl₃ formed from CVOC storage inside aluminum-lined containers,^50,51 we hypothesized that Lewis acid sites of the metal oxides are important for 1,4-dioxane degradation. We performed FTIR analysis of 1,4-dioxane-active materials using pyridine as probe molecule for surface acid sites under dry as well as humid conditions to simulate the aqueous-phase conditions of the oxidation reaction.

Characteristic peaks at ∼1445 cm⁻¹ assigned to pyridine adsorbed on Lewis acid sites were observed on WO_x/ZrO₂, ZrO₂, and CuO (Fig. 3). The concentration of Lewis acid sites was quantified by integrating the area of the 1445 cm⁻¹ peak, then normalizing by the amount of catalytic material and using an extinction coefficient previously determined by Emeis³⁸ (Table S5†). The metal oxides had similar Lewis acid site densities, which were lower than the theoretical metal site density of ∼4 atoms per nm⁻² (roughly 15–20%).^52–54

Fig. 3 FTIR spectra of chemisorbed pyridine under dehydrated and humid conditions for (a) CuO, (b) ZrO₂, and (c) WO_x/ZrO₂.

To help verify these Lewis acid sites participate in 1,4-dioxane oxidation catalysis, we co-added acetonitrile to the batch reactor tests (at amount equivalent to ∼12.5% of theoretical metal site density, Fig. 4) and quantified the resulting rate constants. As a water-soluble Lewis base (less basic but easier to handle compared to pyridine), acetonitrile lowered 1,4-dioxane degradation substantially (by ∼75–80%) over ZrO₂ and WO_x/ZrO₂, but did not affect H₂O₂ consumption much (by <5%) (Fig. 4). The Lewis acid sites of ZrO₂ and WO_x/ZrO₂ are the likely adsorption sites for 1,4-dioxane (as poisoned by acetonitrile). Acetonitrile inhibited 1,4-dioxane degradation over CuO to a lesser extent (∼48%) and H₂O₂ consumption to a greater extent (∼13%).

Fig. 4 Residual activity of catalysts for 1,4-dioxane and H₂O₂ degradation with the addition of 0.125 moles acetonitrile per mole surface site (186 μM acetonitrile).

Humidification, which more closely resembles the aqueous reaction conditions, was introduced during FTIR analysis (Fig. 3). The introduction of water led to the appearance of Brønsted peaks (identified by characteristic pyridine IR peak at ∼1550 cm⁻¹) on CuO but not ZrO₂ or WO_x/ZrO₂. We suggest that CuO, when in water, contains Brønsted acid sites that may contribute 1,4-dioxane degradation, and that Brønsted acidity may not be an important characteristic for ZrO₂ or WO_x/ZrO₂ catalysis.

In combining the kinetic, EPR, FTIR, and surface poisoning results, we propose H₂O₂ dissociates onto metal surface sites into either surface adsorbed ˙OH or ˙O₂⁻ over the metal oxide surface, while Lewis-acidic sites (a minority of total sites) adsorb 1,4-dioxane (Scheme 1). The adsorbed radicals, or peroxyl radicals, react with adsorbed 1,4-dioxane, which contributes to more efficient use of H₂O₂ and to higher 1,4-dioxane degradation activity.

Scheme 1 Hypothesized general mechanism of 1,4-dioxane degradation over Lewis-acidic catalyst surfaces. 1,4-dioxane adsorbed to Lewis acid sites reacts with radicals generated from activation of H₂O₂ on surface.

5. Conclusions

In this work, we surveyed a number of H₂O₂-active metal oxide materials, and evaluated their efficacy for the aqueous catalytic degradation of 1,4-dioxane at mild conditions (ambient temperature, neutral pH, in the dark). Of the materials screened, we found that WO_x/ZrO₂ had the highest 1,4-dioxane degradation rate, followed by CuO and ZrO₂. A LHHW analysis indicated that H₂O₂ and 1,4-dioxane adsorb to distinct catalytic sites. EPR measurements indicate that CuO activates H₂O₂ into highly reactive hydroxyl radicals, while ZrO₂ and WO_x/ZrO₂ form solely less-active superoxide radicals. Pyridine-FTIR and selective poisoning experiments imply that 1,4-dioxane, a weak Lewis base, selectively adsorbs to Lewis acid sites on the catalysts. We present a possible surface-reaction mechanism in which 1,4-dioxane adsorbs to catalyst sites and reacts with metal-oxide supported radical species. These materials show promise for treatment of 1,4-dioxane contaminated waters.

Conflicts of interest

There are no conflicts to declare.

Acknowledgements

This study was supported by the Strategic Environmental Research and Development Program (SERDP) award ER-2307 and NIH NS094535 (A.-L. T.). Additional support for the collaboration came from the CAS/SAFEA International Partnership Program for Creative Research Teams. We thank C. Newell of GSI Environmental, D. Bryant of Geocleanse Intl., and S. Mahendra, M. Myers, and P. Gedalanga of UCLA for helpful discussions. K. N. H. did the kinetic studies and BET analysis, and Y. W. and F. W. did the FTIR analyses. EPR analyses were conducted by G. W. and A. T. All authors contributed toward the manuscript.

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Footnote

† Electronic supplementary information (ESI) available. See DOI: 10.1039/c9ra05007h

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