Article

 

Advanced Electrochemical Oxidation of Methyl Parathion at Boron-Doped Diamond Electrodes

 

Eulalio Campos-González,^a Bernardo A. Frontana-Uribe,^b Ruben Vasquez-Medrano,^a Samuel Macías-Bravo,^a and Jorge G. Ibánez^a,*

 

^a Departamento de Ingeniería y Ciencias Químicas, Universidad Iberoamericana, Prol. Reforma 880, 01219 México, D.F. México. jorge.ibanez@ibero.mx

^b Centro Conjunto de Investigación en Química Sustentable UAEM-UNAM, Toluca 50200, Estado de México. México.

 

Received February 11^th, 2014
Accepted April 3^rd, 2014.

 

Abstract

Plaguicide pollution is a major problem in agricultural zones due to their intensive use to attain increased crop yields. In the present work commercial methyl parathion (MP), was electrochemically degraded in a divided H-type cell equipped with two boron doped diamond electrodes, BDDE and a Nafion cation exchange membrane. High removals (i.e., > 90%) of total organic carbon, TOC and of chemical oxygen demand, COD were obtained after 180 min at a current density, j of 5 mA/cm² with specific energy consumption, E_sp of ca. 200 kWh per kg of COD degraded. These results show that the anodic oxidation route may be an efficient alternative for MP degradation in polluted waters.

Key words: Methyl parathion, BDDE, TOC, COD, current density, specific energy consumption.

 

Resumen

La contaminación por plaguicidas es uno de los mayores problemas en zonas en donde se utilizan para mejorar el rendimiento de los cultivos. En el presente trabajo se reporta la degradación de metil paratión comercial (MP) en una celda tipo H, con dos electrodos de diamante dopado con Boro (EDDB) y una membrana Nafion de intercambio catiónico. Una alta remoción (> 90%) de carbón orgánico total (COT) y de la demanda química de oxígeno (DQO) son obtenidas después de 180 min a una densidad de corriente j de 5 mA/cm² con un consumo especifico de energía E_sp de 200 kWh por kg de DQO degradado. Estos resultados muestran que la oxidación anódica puede ser una alternativa eficiente para la degradación de MP en aguas contaminadas.

Palabras clave: Metil paratión, EDDB, COT, DQO, densidad de corriente, consumo específico de energía.

 

Introduction

The use of substances in crops for pest control has being known since the Middle Ages, when sulfur was used for such activities [1]. During the last century the production of these substances was industrialized. In the 1930s the first synthetic pesticides markedly improved crop yields (e.g., methyl parathion, MP in 1933) and their use intensified substantially [2]. MP is a very useful non systemic pesticide in food and fiber crops [3, 4]. In spite of their great usefulness many of these pesticides represent a human health threat affecting the contact chain, from those who apply them to the final consumers. In addition, due to their difficult biodegradation and easiness for lixiviation [4] pollution problems arise in surface waters, aquifers and soils. In this way, MP has been detected in rivers like the Sacramento in California [5] and the Ebro in Spain [6]. MP is still used in some countries for its effectiveness but banned in others [4, 7]. A solution is now required for the disposal or elimination of these residues from the toxic and difficult-to-degrade products stored unused in commercial containers, as well as in containers of expired products. The Food and Agricultural Organization of the United Nations, FAO estimates that there are some 400,000 tons of expired pesticides in storage [5] and that the disposal cost of obsolete pesticides is of the order of USD $3000-4500 per ton, depending on their composition [8].

Since MP is a highly recalcitrant, toxic, and persistent herbicide [5] it is mandatory to develop methods to treat it so that the resulting effluents be biodegradable. Typical proposed processes include adsorption [6, 7], ozonization [9], electrochemical oxidation with Ti/Pt/Ir anodes [10], photocatalytic oxidation [11], ultrasonic irradiation [12], bioremediation [13], and thermal desorption [8]. Even though adsorption can achieve high removal efficiencies, the contaminants are simply separated from their original matrix but not degraded. Advanced oxidation processes, AOP (i.e., those involving the production of highly oxidizing ^●OH radicals) can achieve high mineralization yields as is the case of the photo-Fenton [11] and electro-Fenton processes [14].

In the recent past the electrochemical route has become rather popular for the treatment of recalcitrant residues [15] and has proven useful in the treatment of wastewaters from olive oil production [16], residential wastes [17], lixiviates [18], tanneries [19], textile industries [20], and the like. Electrochemical methods for advanced oxidation are environmentally friendly since they do not generate new contaminants and they can treat water during the three working shifts since they are not limited to the sun assisted photo-processes [11]. Anodic oxidation at boron-doped diamond electrodes, BDDE involving the production of ^●OH radicals has been especially successful [21-23]. For instance, high mineralization yields have been reported (80-100%) when using current densities of 50-2000 mA/cm² [24-27]. The electrochemical mineralization of recalcitrant organic matter at a BDD anode is possible due to the formation of the highly oxidizing hydroxyl radical (^●OH, E° (^●OH/H₂O) = 2.80 V/SHE) [28] on the electrode surface at the water discharge voltages in aqueous media [29]. The general reactions that describe the mineralization of organic substances are:

where R is an organic pollutant with n carbon atoms.

The accepted mechanism for the oxidation of organics at BDD electrodes involves the anodic water discharge at BDD anodes that generates ^●OH radicals adsorbed on the electrode [30]; this species can rapidly oxidize organic matter to CO₂ and H₂O. The electrode surface is then regenerated and both intermediates are produced again after water oxidation. The amount of ^●OH radicals adsorbed on the electrode depends on the potential used, the anode material, and the extent of the secondary reaction of oxygen production. For this reason the oxidation of organic matter effectively occurs in the vicinity of the anode.

In the present work a lab-scale electrochemical method is discussed for the treatment of MP using BDDE both as anode and cathode. Similar works reported to date indicate fairly high energy consumption (i.e., 1.16 kWh g⁻¹) during MP elimination [27], which represents a challenge and confirms the difficulty involved in degrading such type of pollutants.

 

Experimental

Reagents

Methyl parathion (O,O-diethyl O-(4-nitrophenyl) phosphorothioate, MP was used either pure (99.9% pure, Supelco^® Analytical, Bellefonte, PA) or from a commercial suspension (Foliol 70%, Cheminova). Na₂SO₄ (Sigma Aldrich^®, 99% pure) and NaHSO₄ (Fluka Analytical, 95% pure) were used together as supporting electrolytes. Milli-Q water ≥ 18.2 MΩ cm was used throughout the entire experimentation protocol.

2.2 UV-vis calibration curve for MP

MP (Sigma-Aldrich, 99.9% pure) was diluted as needed to prepare 1-10 ppm standard solution. Its natural solubility in water is 55 - 60 mg/L [2]. Due to the oily nature of the system, a methodical reproducibility was rather difficult. For this reason the mixtures were vigorously stirred for 20 min and sonicated in a Branson 1510 Ultrasonic Cleaner for 30 min to achieve complete solubilization. A qualitative UV-vis scan with a Varian Cary 50-C spectrophotometer at 4800 nm min⁻¹ revealed a peak suitable for analysis at λ = 277 and a calibration curve was elaborated from the corresponding absorbance results. Concentrations higher than 10 ppm fell outside the linear range of the corresponding Lambert - Beer plot. The regression equation obtained is Abs = 0.0448 C (in ppm), R² = 0.9788. See Figure 1.

2.3 Preparation of MP solutions from the commercial precursor

The commercial insecticide Foliol (Cheminova^®) containing 450 g/L of the active constituent methyl parathion was employed in the degradation experiments. 10 g of the commercial MP suspension were diluted to 250 mL with a sulfate buffer (0.04 M Na₂SO₄ / 0.05 NaHSO₄) at pH = 2.1 ± 0.1. No further pH adjustment was performed during the electrolysis experiments. This pH was chosen since a more complete degradation of selected organic substances has been reported at low rather than at neutral or high pH values [7, 29]. Application of the same solubilization protocol as described above typically produced a 500-ppm MP solution. 100-ppm solutions were then prepared from this stock solution by appropriate dilution.

2.4 Electrochemical study

A MP voltammetric study was performed with the 100-ppm MP standard solution described earlier using a BAS-CV 50 voltammetric analyzer in a 3-electrode cell equipped with a BDD working electrode (Diachem^®, 1 cm² geometrical area with a 1-10 µm conducting diamond layer, a 500-8000 ppm boron concentration, and 0.1 Ω cm resistivity)[31]). The counter electrode was a Pt flag electrode (3 mm x 13 mm, 99 % pure Pt, American Educational Products, product 7-501-2, Fort Collins, CO) and the reference electrode was an Ag/AgCl BAS electrode.

MP degradation experiments were performed in an H-type cell (Figure 2) consisting of a 250-mL anodic compartment and a 300-mL cathodic compartment separated by a cation exchange membrane Nafion 424 to allow the passage of protons [32]. The anodic compartment was equipped with a magnetic stirring bar that provided mass transport during the entire experimental procedure to speed up the electrochemical oxidation of the organic compounds with the hydroxyl radicals. Recirculation was afforded to the catholyte by a peristaltic pump (Master Flex L/S, model 77200-62) at 550 mL/min. A 40-cm² geometrical area Diachem-Condias^® BDD electrode (1-10 µm conducting diamond layer, a 500-8000 ppm boron concentration, and 0.1 Ω cm resistivity, [31]) was inserted on each side of the cell. Prior to each experiment the anolyte was deaerated by bubbling high-purity nitrogen during 10 min at a rate of 10 cm³ min⁻¹ (Infra, Chromatographic grade). Currents from 10 to 200 mA were passed through the cell with an AMEL 2051 potentiostat/galvanostat. The pH was monitored with a Conductronic^® pH-meter. Experiments were performed at room temperature (typically 22 ºC; its variation during the experimental runs remained within ± 2.5 ^oC).

2.5 Chemical analysis

Samples from the degradation solutions were diluted 1:10 with the buffer solution in order to have the results in the linear range reported in Figure 1, and their absorbances examined at λ = 277 nm. In order to follow the amount of organic compounds remaining at each time the total organic carbon, TOC and the inorganic carbon, IC were monitored in 15-mL samples at 0, 15, 30, 60, 90, 120 and 180 min with a Shimadzu V_CPH TOC analyzer. The chemical oxygen demand, COD was monitored using the standard method [33] by placing 2-mL samples in Hach^® vials containing a strongly oxidizing dichromate solution and affording a 2-h heating protocol in a Hach® COD reactor.

The instantaneous current efficiency was calculated as the fraction of current effectively utilized for the oxidation of organic compounds as follows [34]:

where F is the Faraday´s constant (96,487 C mol⁻¹), V is the volume of the solution (in L), COD_t and COD_t+Δt represent the chemical oxygen demand (in g_O2 L⁻¹) at times t and t+Δt, respectively (in seconds), I is the current passed through the system (in A), and 8 is the oxygen equivalent mass (g eq⁻¹) [15, 34].

 

Results and Discussion

Voltammetric analysis of methyl parathion on a BDDE

Methyl parathion was voltammetrically analyzed using a BDDE in the sulfate buffer solution (Figure 3). The electrochemical window is located between -1100 and +2200 mV. The small peak observed at the foot of the anodic barrier (inset a) corresponds to the oxidative degradation of electrode impurities [35, 36]. The cathodic system (inset b) observed at ca. -750 mV corresponds to the nitroaromatic group reduction, and the other major anodic and cathodic peaks correspond to the hydroxylamine-nitrosoaromatic system [37]. The difficulty for the oxidative degradation of MP is evidenced by the lack of an anodic signal (inset c) since the sole response observed was water electrolysis. Therefore the MP oxidation is not direct and the electrochemical generation of ^●OH radicals at the BDDE is necessary to accomplish this degradation as described below.

Electrochemical degradation of methyl parathion

In order to evaluate the effect of current density on the degradation of MP, its concentration was spectrophotometrically monitored as a function of time at different applied current densities, j: 0.25, 0.625, 1.25, 2.5 and 5 mA cm⁻². Such a current density range was selected in order to maintain low energy consumption [17, 24-27]. It is well known that low current densities do not completely destroy all the organic species, but they should suffice to destroy MP which is the objective of the present work.

The MP concentrations in the electrolysis solutions were determined using the calibration curve depicted in Figure 1 after a 1:10 dilution as described above. Figures 4 and 5 show the UV-vis spectra of the MP solutions for 0.25 and 5 mA cm⁻², respectively. The peak at 277 nm is associated with the conjugate double bonds in MP [27] and thus its intensity decrease mirrors the MP concentration.

Figure 6 shows the normalized MP concentration variation as a function of time at different current densities. As the current density increases the disappearance of the pesticide becomes faster. At 5 mA/cm² the MP concentration decreases from 100 ppm down to ca. 10 ppm in merely one hour of electrolysis; after that, mass transport limitations are observed.

The reactions occurring in the anodic compartment are generalized in equations 1 and 2, while the simultaneous oxygen production during water electrolysis occurs as well [21]. Although MP and its degradation products are oxidized in the anodic compartment by direct reaction with the hydroxyl radicals generated from water oxidation at BDD [34], the MP disappearance does not necessarily reflect its complete mineralization. Furthermore, it is well known that intermediates produced during the degradation of some pollutants often are even more dangerous than the parent compounds themselves. Therefore the monitoring of the total amount of organic carbon, TOC would render a more realistic indicator of the disappearance of all the organic compounds from the target solution. Figure 7 shows the percent TOC removal as a function of time for all the current densities described earlier. It can be observed that the higher the current density, the higher and faster the TOC removal (up to ca. 95%).

In order to better understand the fate of the degradation products, the inorganic carbon, IC was also monitored in each solution. This gives a quantitative indication of the amount of carbon that became dissolved in the solution as carbonate [38]. Figure 8 shows the percent organic carbon removal as well as the amount of inorganic carbon found in the solution as a function of time for j = 0.25 mA cm⁻². Albeit slowly (since almost no mineralization occurs in the first half of the reaction), the system behaves normally in the sense that TOC decreases with time while IC increases at this j. On the other hand, while TOC also decreases with time at j = 5 mA cm⁻² (see Figure 9), the IC peaks rapidly at ca. 2 h. This reflects a faster mineralization (i.e., a high TOC removal, ca. 70% that produces a high IC) after which the parasitic solvent decomposition starts predominating.

Since the chemical oxygen demand, COD is an important parameter in the water treatment field this was monitored as a function of time at the same current densities described earlier (see Figure 10). In agreement with the TOC experiments, the highest j (i.e., 5 mA cm⁻²) renders the highest COD removal, reaching > 90% after 180 min. The monitoring of COD values shows that the intermediates decrease with time, which points at a total mineralization of the majority of organic matter present.

The instantaneous current efficiency, ICE is defined as the portion of the current directly used for the oxidation of organic compounds [39] and was evaluated for the treatment of the 100-ppm MP solution as a function of time and of current density (see Figure 11). The % ICE is clearly better for lower j values, which translates into a better use of current because ^●OH are preferentially produced thus limiting oxygen evolution. Higher j values promote faster degradation rates accompanied by the concomitant higher production of oxygen and an ICE decrease. This was to be expected because the origin of the ^●OH radicals is the oxidation of water molecules at the BDDE.

For our experimental conditions limited amounts of peroxodisulfate might be generated; nonetheless sulfate concentrations should be higher than 2 M for sulfate oxidation to become important [32, 40, 41].

Energy consumption, EC during electrolysis

This is a crucial issue for the determination of the effectiveness of the process. The specific energy consumption, E_sp is a key parameter to understand the scalability of water treatment systems for high influent volumes as well as the global efficiency of the oxidation process. It relates the energy consumed per kg of COD (kWh kg_COD⁻¹) as follows [39]:

where V_C = cell potential (V), = average current efficiency, and 8 is the mass equivalent of oxygen. can be calculated by integrating the ICE over the entire experimental time, τ:

Figure 12 shows the variation of E_sp and %COD removal with j. Higher j values yield higher %COD removals albeit at the expense of higher E_sp requirements.

Lastly, power consumption (P, in kWh) during the electrolytic degradation is determined as follows [42]:

where E_cell is cell potential (V), I is applied current (A) and t is electrolysis time (h). The value that recounts energy consumption per gram of COT removed is given by:

where m is the mass of TOC removed (g). See Figure 13.

The highest current density used in the present work (i.e., 5 mA cm²) is capable of mineralizing 97% of the TOC. In contrast, that reported elsewhere for MP [27] at the same j yields only 20% mineralization. This result supports the prospects of pilot plant escalation.

 

Conclusions

This work evidences that commercial MP can be efficiently mineralized in acidic aqueous solution at a BDDE with high TOC and COD removals, together with a specific energy consumption of only 12% compared to earlier reports [27]. MP removals range from 45% at 0.25 mA/cm² up to 93% at 5 mA/cm². Overall, this is a promising option for the treatment of water polluted with MP.

 

Acknowledgements

We acknowledge financial support from CONACYT in the form of a scholarship to Eulalio Campos as well as from Universidad Iberoamericana (Project 0053). Experimental assistance was provided by Ana Paula Gartland-Masana and Mario Palazuelos-Argaiz. Helpful insights from Patricio Espinosa-Montero are also gratefully acknowledged.

 

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