Revisiting Oxidative Dehydrogenation of Ethane by W Doping into MoVMn Mixed Oxides at Low Temperature

Al-Hazmi, Mohammed H.; Odedairo, Taiwo; Al-Dossari, Adel S.; Choi, YongMan

doi:https://doi.org/10.1155/2015/102583

Advances in Physical Chemistry

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Abstract Introduction Experimental Results and Discussion Conclusions Acknowledgments References Copyright Related Articles

Research Article | Open Access

Volume 2015 | Article ID 102583 | https://doi.org/10.1155/2015/102583

Revisiting Oxidative Dehydrogenation of Ethane by W Doping into MoVMn Mixed Oxides at Low Temperature

Mohammed H. Al-Hazmi,¹Taiwo Odedairo,^1,2Adel S. Al-Dossari,¹and YongMan Choi¹

Academic Editor: Jinlong Gong

Received09 Nov 2014

Revised17 Dec 2014

Accepted31 Dec 2014

Published27 Jan 2015

Abstract

The catalytic performance of MoVMnW mixed oxides was investigated in the oxidative dehydrogenation of ethane at three different reaction temperatures (235, 255, and 275°C) using oxygen as an oxidant. The catalysts were characterized by using X-ray diffraction, temperature-programmed reduction, and scanning electron microscopy. The MoVMnW mixed oxide catalyst showed the 70–90% of ethylene selectivity at the reaction temperatures. However, a significant decrease in the selectivity of ethylene was observed by increasing the reaction temperature from 235°C to 275°C.

1. Introduction

Ethylene (C₂H₄) is an important building block used in the petrochemical industry [1]. Its primary production method is the energy-intensive steam cracking process [2] which is usually carried out at > 800°C [3]. Over 100 million metric tons of ethylene is produced annually by means of the steam cracking of long carbon-chain hydrocarbons. In addition to the high energy cost, unavoidable side reactions and the deactivation of catalysts by carbon deposition are other technical shortcomings of the process. Increasing attention has been directed towards the oxidative dehydrogenation (ODH) of alkanes because of its potential benefit of using abundant and inexpensive raw materials [4–6]. The ODH of light alkanes offers a potentially attractive route to alkenes since the reaction is exothermic [2] and avoids the thermodynamic constraints of nonoxidative routes by forming by-product water [7]. However, a low yield and selectivity of olefins still retard the industrial application of the ODH. To date, about a 20% yield of ethylene was reported in the literature, and for industrial applications, it requires the ethylene productivity of above [8]. The ODH of ethane to ethylene has received less attention than the nonoxidative cracking [9]. However, ethane is the second-largest component of natural gas and the primary product of the methane conversion by oxidative coupling. Thus, a large number of catalysts have been investigated for the ODH of ethane and propane, for example, using Mo-V based catalysts [10–13]. It was reported that a V based catalyst is one of the most active and selective single metal catalysts in the ODH [14, 15], while V [10, 16–18], Mo [12, 13, 19–21], Pt [22–25] based catalysts, and MoV mixed oxides [26–28] are the most widely studied transition-metal catalysts for the ODH of ethane. Furthermore, a more complicated material (i.e., Mo₁V_0.25Nb_0.12Pd_0.0005O_x [29–31]) with two different catalytic centers, such as the ODH of ethane and the heterogeneous Wacker oxidation of ethylene to acetic acid, was reported. The catalytic activity of MoV based catalysts supported on TiO₂ and Al₂O₃ was investigated in the ODH of both ethane and propane [32]. Recently, the catalytic properties of the acidic and basic forms of Ni-, Cu-, and Fe-loaded Y zeolites were investigated in the ODH of ethane to ethylene [33]. As discussed above, although numerous studies on the ODH of ethane using MoV based mixed oxides were reported [29, 31, 32, 34, 35], to the best of our knowledge, little studies using W doping into MoV mixed oxide catalysts have been reported in the literature [35, 36], demonstrating the ethane conversion is the best using a 6.3 mol% W doping to MoVMn mixed oxide catalysts. In this study, to obtain a more systematic, optimal condition of MoVMnW based catalysts for the ODH of ethane, we investigated the effect of various reaction conditions (i.e., contact time, reaction temperature, and conversion) on the selectivities of ethylene, acetic acid, and CO_x.

2. Experimental

2.1. Catalyst Preparation

As mentioned, 6.3 mol% of W doping to MoVMn mixed oxide catalysts showed the best conversion of ethane by the ODH [35]. Based on the previous study, we applied three materials of MoV_0.4Mn_0.18W₀O_x (W₀), MoV_0.4Mn_0.18W_0.063O_x (W_0.06), and MoV_0.4Mn_0.18W_0.14O_x (W_0.14). We considered W₀ and W_0.14 as the extreme cases without W and the highest doping, respectively, and W_0.06 as the optimal one in terms of the ethane conversion from the ODH. The synthesis method is described in detail elsewhere [36]. Briefly, ammonium metavanadate (Fluka Chemical) was added to deionized water and heated to 85°C, with a constant stirring. A yellow colored solution was obtained. Oxalic acid (Riedel-de Haën Chemicals) was added with water to the solution with constant stirring, while the required amount of ammonium tungstate (BDH Chemicals) and manganese acetate (Riedel-de Haën Chemicals, resp.) was slowly added to the mixture. Then, ammonium heptamolybdate (Riedel-de Haën Chemicals) was added to the solution. Precipitates were dried in an oven at 120°C and calcined at 350°C for 4 hours. The calcined catalysts were screened into uniform particles of a 40/60 mesh.

2.2. Characterization of Catalysts

The samples were characterized using several characterization tools including X-ray diffraction (XRD). It was recorded on a Mac Science MX18XHF-SRA powder diffractometer with monochromatized Cu Kα radiation (λ = 0.154 nm) at 40 kV and 30 mA. A Micromeritics AutoChem II 2920 with a thermal conductivity detector (TCD) was used for the H₂ temperature-programmed reduction (TPR) analysis to study the reduction properties of the samples. 15–20 mg of the catalyst samples was heated from 40°C to 1000°C at a heating rate of 10°C/min in 10% H₂ in Ar. Before the H₂-TPR analysis, the samples were heated for 60 min in Ar flow at 100°C. The profile of consumed H₂ was recorded by the TCD. Scanning electron microscopy (SEM) images were recorded using a JEOL JSM-5500LV. Surface area calculations were carried out using The Brunauer-Emmett-Teller (BET) method. Adsorption isotherms were measured in Quantachrome AUTO-SORB-1 at −196°C.

2.3. Reaction Apparatus and Procedures

Catalytic experiments were carried out in a fixed-bed reactor (I.D. = 0.78 cm) with the contact times of 0.08, 0.12, 0.16, 0.24, 0.32, 0.49, and 0.65 sec. The contact time was changed by varying the weight of the catalyst in the range of 50–400 mg and at a total flow of 30 mL/min. All experiments were carried out at 235, 255, and 275°C and at 200 psi. The gas feed composition used in this study was fixed at 15 vol.% ethane in 85 vol.% air. To avoid any mass resistance problem of feed, the prepared powder was pressed to pellets, then crushed, and sieved to 40–60 mesh particles. Reactants and products were analyzed using an online gas chromatograph equipped with a double detector (i.e., thermal conductivity detector (TCD) and flame ionization detector (FID)) and two columns of HayeSep D 80/100 mesh and LAC446. We confirmed the reproducibility of the experiment results within the uncertainty of ±2%. Then, we obtained the conversion (), selectivity to product (), and yield to product ().

3. Results and Discussion

3.1. Characterization of Samples

Crystalline phases of the three catalysts were characterized by XRD. Figure 1 shows XRD patterns of W₀, W_0.06, and W_0.14 calcined at 400°C. Mo suboxides (i.e., Mo₈O₂₃ (or Mo₉O₂₆), MoO₃, and (V_xMo_1−x)₅O₁₄) were noticed as the major phases (Figure 1). Also, (M_xMo_1−x)₅O₁₄ (M = V, Mn, or W) was observed as one of the major phases. The reason that most lines of MoO₃ are shifted compared to the standard pattern (JCPDS 76-1003) may be due to a modification by vanadium (i.e., orthorhombic α-V_xMo_1−xO_3−0.5x) or the formation of oxygen vacancies in MoO_3−x. Also, triclinic V_0.95Mo_0.97O₅ (JCPDS 77-0649), whose XRD patterns are close to that proposed for VMo₃O₁₁ [37], was observed. The BET surface areas of W₀, W_0.06, and W_0.14 are 15.6 m²/g, 13.9, and 15.3, respectively, indicating that the W doping shows an insignificant effort on the textural properties of the materials.

TPR in H₂ was performed to examine reduction characteristics of the mixed oxide catalysts as displayed in Figure 2. There are two reduction peaks observed for W₀ at 587°C and 677°C which correspond to the reduction of isolated V⁵⁺ species in the bulk structure of the catalyst [38, 39] and Mo⁶⁺ species [40], respectively. In addition, the observed shoulder at a temperature around 470°C is assumed to be H₂ uptake associated with the reduction of MnO₂ to Mn₂O₃ [41]. The position of the peak at 677°C is shifted to higher temperatures of 769°C (W_0.06) and 772°C (W_0.14) and becomes broadened without a significant change in peak intensities. Solsona and coworkers [42] reported a similar shift when W was added to NiO and proposed that the shift was related to an interaction between NiO and tungsten oxide nanoparticles. As shown in the peaks of W_0.06, the H₂ consumption at 470°C and 587°C was enhanced by the addition of W loading (W₀ versus W_0.06). We observed that the reduction occurred slightly at higher temperatures by adding more W into the MoVMn based catalysts (W_0.06 versus W_0.14).

Figure 3 shows typical SEM images of W₀, W_0.06, and W_0.14 doped catalysts, displaying that all samples have irregular shaped particles. The SEM image of W₀ without W ascertains a rough surface with variable shapes and sizes, and a few regions show a stack of fine crystallites (Figure 3(a)). Similarly, W_0.06 has a rough surface with variable shapes and sizes, but without a stack of fine crystallites (Figure 3(b)). The SEM images of W_0.14 determine a stack of fine crystallites, leading to a flower-like morphology (Figure 3(c)).

3.2. Catalytic Performance from the ODH of Ethane

Figure 4 shows the effect of W loading on the ethane conversion and product selectivity from the ODH of ethane at 275°C and at a reaction time of 0.65 sec. Ethylene is observed as the major product from the ODH of ethane, while acetic acid, CO, and CO₂ are also detected. The highest ethane conversion (~21.0%) is observed from the MoVMn sample with W = 0.063. The increase in the amount of W over the MoVMn sample leads to a reduction in the conversion of ethane. Similarly, the addition of W results in an increase in the selectivity of ethylene with a maximum selectivity (~74%) achieved at W = 0.063. The lowest selectivity of acetic acid (~12%) is detected at W = 0.14. The ODH experiment of ethane was carried out at two more temperatures of 235 and 255°C using the W_0.06 catalyst with the contact times of 0.08, 0.12, 0.16, 0.24, 0.32, 0.49, and 0.65 sec (Figure 5). As shown in Figure 5, ethane conversions of approximately 7.0, 11.3, and 21.0% are achieved at 235, 255, and 275°C, respectively, at a contact time of 0.65 sec. The conversion of ethane is improved as the contact time increases. In this study, the maximum ethane conversion was obtained at 275°C. The product distribution from the ODH of ethane on the W_0.06 catalyst at 235, 255, and 275°C is presented in Figure 6. At all temperatures studied, ethylene is the major product, while acetic acid and carbon oxides are also observed (i.e., ~3.5% and ~1.7%, resp., at 275°C). Figure 7 presents the influence of reaction temperatures and contact times for the selectivities of ethylene, acetic acid, and carbon oxides (CO and CO₂). The selectivities of ethylene decrease by the increase of contact times at all temperatures studied. The highest selectivity of ethylene is observed at a reaction temperature of 235°C. Increasing the reaction temperature from 235°C to 275°C leads to a reduction in the selectivity of ethylene, while an enhancement of selectivities of acetic acid, CO, and CO₂ are observed (Figure 7(b) and Table 1). Table 1 compiles theoretical selectivities of ethylene and CO_x at each reaction temperature. The trend of the reaction products over the W_0.06 catalyst indicates that ethylene is a key source of acetic acid and carbon oxides. Furthermore, the reduction of the selectivity of ethylene along with the corresponding increase of the by-products (acetic acid and carbon oxides) clearly manifests that acetic acid and carbon oxides are the secondary products from the consecutive oxidation of ethylene. The effect of ethane conversion on the selectivities of ethylene, acetic acid, CO, and CO₂ at 235, 255, and 275°C over W_0.06 is plotted in Figure 8, demonstrating a strong dependence of ethane conversion and selectivity. It is observed that the selectivity decreases as ethane conversion increases. Also, the selectivity of by-products (i.e., acetic acid, CO₂, and CO) shows a linear relation with the conversion of ethane. As the reaction temperature increases, the selectivity of ethylene decreases. Our experimental data suggest that ethylene undergoes substantial further oxidation, and the ODH of ethane can be described by the parallel consecutive scheme [43].

(a)

(b)

(a)

(b)

3.3. Kinetic Studies

A kinetic model was developed to understand the ODH of ethane on MoVMnW mixed oxide catalysts. A generally accepted scheme for the ODH of ethane is shown in Scheme 1 [3, 33, 44]. The kinetic parameters , , and α for the ODH of ethane over the W_0.06 catalyst were obtained using a nonlinear regression. To develop a kinetic model for the ODH of ethane, three assumptions were made: the ODH is isothermal, a catalyst deactivation is a function of time-on-stream (TOS), and a single deactivation function is defined for all reactions, and a thermal conversion is neglected. Based on the assumptions, rates of the disappearance of ethane () and the formation of ethylene (), acetic acid (), and carbon oxides (), respectively, are described as follows: where is a concentration of species in the units of mol/m³, is a reaction in the unit of time (i.e., at inlet of the catalyst bed, = 0, and at the outlet of the catalyst bed, = τ), is an apparent rate constant for the th reaction in the unit of s⁻¹, and is the apparent deactivation function. The measurable variables from our chromatographic analysis are the weight fraction of the species, , in the system. By definition the molar concentration, , of every species in the system can be related to its mass fraction, by the following relation: where is the total mass flow rate (kg/min), is the molecular weight of species in the system, and is the total volumetric flow rate (m³/min).

Regarding catalyst deactivation, as deactivation functions can be expressed in terms of the catalyst time-on-stream (), deactivation can also be related to the progress of the reaction [45], where α is a catalyst deactivation constant. The deactivation function based on time-on-stream was initially suggested by Voorhies [46].

Substituting (5) into (1)–(4), we have the following first order differential equations which are in terms of weight fractions of the species: where , , , , and , respectively, are given by , , , and . The temperature dependence of the rate constants was represented with the centered temperature form of the Arrhenius equation; that is, where is an average temperature introduced to reduce parameter interaction in the unit of K [47], is the rate constant for reaction at (s⁻¹), and is the activation energy for reaction (kJ/mol). Since the experimental runs were done at 235, 255, and 275°C, T_o was calculated to be 255°C. The values of the model parameters along with their corresponding 95% confidence limits (CLs) are shown in Table 2, while the resulting cross-correlation matrices are also given in Table 3. The cross-correlation matrices give good results as indicated by a low correlation between most of the parameters, with only a few exceptions. From the results of the kinetic parameters presented in Table 2, it was observed that the catalyst deactivation was found to be small, α = 0.03, indicating a low coke formation. As mentioned, the ODH of ethane can occur via the reaction network as shown in Scheme 1, in which ethane reacts with oxygen to form ethylene with a rate constant , or carbon oxides (CO_x) with a rate constant . Ethylene, then, undergoes a subsequent oxidation to CO_x and CH₃COOH with rate constants and , respectively. Rate constants and can be used to determine the ODH of ethane activities, while the ratios of rate constants (i.e., and ) are used to determine the ethylene selectivity. High ethylene yields at a reasonable contact time apparently require high values of and low values of and . The kinetic parameters (, , , and ) summarized in Table 2 confirms the high selectivity of ethylene noticed in the ODH of ethane over the W_0.06 catalyst. Apparent activation energies of , , , and kJ/mol were obtained for the ethane ODH (), ethane combustion (), alkene combustion (), and the formation of CH₃COOH from C₂H₄ (), respectively, following the order of < < < . Recently, Lin et al. [33] reported apparent activation energy of ~51.5 kJ/mol for the formation of ethylene over a K-Y zeolite. Similarly, an apparent activation energy () of ~63.2 kJ/mol was reported for the formation of ethylene over VO_x/SiO₂ catalyst [6]. These values are in good agreement with that calculated over the W_0.06 catalyst. Argyle and coworkers [7] reported apparent activation energies ~115 kJ/mol and ~60–90 kJ/mol for ethane combustion () and alkene combustion (), respectively, over an alumina-supported vanadia catalyst. The apparent activation energies obtained for ethane and ethylene combustion to form carbon oxides in this present study show a similar order of magnitude with those reported in the literature. Using the estimated kinetic parameters, we carried out kinetic modeling to examine the validity of the simulated results, and compared them with our experiments finding (i.e., Figures 5 and 9). The fitted parameters were substituted into the comprehensive model developed for this scheme, and the equations were solved numerically by using the 4th-order-Runge-Kutta routine. It was found that our prediction is in good agreement with experiment (Figures 5 and 9), demonstrating the validity of the proposed kinetic model. It is assumed that the slight deviation observed in Figure 9 at 275°C might be due to the significant side products generated at this reaction temperature. It is proposed to carry out microkinetic modeling based on a mechanistic study using density functional theory (DFT) simulations [48, 49], providing more detailed information of the conversion, selectivity, and yield of C₂H₄, CH₃COOH, CO, and CO₂ on W-doped surfaces. The DFT based study would facilitate rationally design of novel MoVMnW mixed oxide catalysts.

4. Conclusions

MoVMnW mixed oxide catalysts were revisited to examine the ODH of ethane. It was found that the addition of W to MoVMn mixed oxide catalysts improves the catalytic activity toward C₂H₄, while lowering the formation of by-products (CH₃COOH, CO, and CO₂). Using the MoV_0.4Mn_0.18W_0.063O_x (W_0.06) catalyst, we observed that the primary product of ethane oxidation is ethylene, which may go through consecutive reactions to CH₃COOH, CO, and CO₂. The best selectivity of ethylene on the catalyst was ~90% at 235°C. However, a significant decrease in the selectivity of ethylene was observed by increasing the reaction temperature from 235°C to 275°C.

Conflict of Interests

The authors declare that there is no conflict of interests regarding the publication of this paper.

Acknowledgments

The authors highly appreciated the financial support by SABIC. YongMan Choi acknowledges the technical discussion with Professor Ming-Kang Tsai. The authors thank the reviewers’ valuable comments, which have improved their paper substantially.

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Copyright © 2015 Mohammed H. Al-Hazmi et al. This is an open access article distributed under the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.

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