Oxidative Dehydrogenation of n-Butane over LaV Catalysts Supported on TiO<sub>2</sub>

Cam, Le Minh; Huyen, Ngo Duc; Ha, Nguyen Ngoc

doi:https://doi.org/10.1155/2013/868906

Journal of Chemistry

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Abstract Introduction Experimental Results Conclusions Acknowledgments References Copyright Related Articles

Research Article | Open Access

Volume 2013 | Article ID 868906 | https://doi.org/10.1155/2013/868906

Oxidative Dehydrogenation of n-Butane over LaV Catalysts Supported on TiO₂

Le Minh Cam,¹Ngo Duc Huyen,¹and Nguyen Ngoc Ha¹

Academic Editor: Sedat Yurdakal

Received02 May 2013

Revised26 Jul 2013

Accepted02 Aug 2013

Published09 Sept 2013

Abstract

The catalytic performance of vanadia catalysts with 15 wt% V supported on TiO₂ and (15 wt% V + 4.6 wt% La) supported on TiO₂ in oxidative dehydrogenation (ODH) of n-butane was investigated. The catalysts were characterized by means of TPD-NH₃, TPR-H₂, UV-Vis, and BET. Testing of samples showed that vanadia catalysts were active for the reaction. It was found that La doping of V/TiO₂ catalyst had a negative effect on the dispersion of V species and led to formation of V₂O₅ clusters. This resulted in a loss of activity. Although slight improvement of selectivity was observed in comparison to undoped V/TiO₂ samples due to lower acidity of La-doped –V/TiO₂, this could not compensate the loss of activity and finally did not lead to higher butene yields.

1. Introduction

Oxidative dehydrogenation of light alkanes has been a research topic of consistent interest from the 1980s [1–3]. The presence of oxygen raises the thermodynamic restrictions of dehydrogenation, and the exothermic character of the reaction renders it an energetically efficient process [4, 5]. The development of efficient heterogeneous catalysts for the oxidative dehydrogenation of alkanes is of great importance because of the economic benefits of using light alkanes for the production of important base chemicals [6, 7]. In order to make the process commercially feasible, the main objective is to maximize the selectivity to alkenes, a significant issue, since the deep oxidation of alkanes and alkenes (reaction products) is thermodynamically favoured [8–11]. Experimental studies have proposed that the ODH reaction of C₂–C₄ alkane over transition metal based catalysts occurs following a Mars-van Krevelen redox mechanism [12] in which surface catalytic sites are reduced by hydrocarbon with participation of the lattice oxygen and followed by reoxidation with adsorbed O₂ from the gas phase. It is well known that the catalyst behavior depends on a number factors, such as the chemical nature of the active species, the redox properties, and the acid-base character, which in turn depend on transition metal loading, dispersion, and support effects [13].

In case of butane ODH, vanadium supported catalysts are considered good catalysts, and vanadium appears to be the selective catalytic site. The coordination of vanadium in the active centres and the density of the active sites belong to the most important factors determining the catalytic performance of V catalysts. It has been postulated in the literature that tetrahedrally coordinated V centres are more selective but less active than octahedral ones [14]. However, there are discrepancies between different authors whether isolated VO₄ tetrahedra are more effective than units possessing V–O–V entities. The concentration of vanadium phase on the catalyst surface depends on the method of preparation and on the nature and amounts of supports or promoters eventually added to that active phase [15–19]. Very good results for vanadium dispersion and catalytic properties have been obtained by preparing the TiO₂–SiO₂ support by grafting [20]. The literature provides some information on both the method of anchoring vanadium on SiO₂ and TiO₂–SiO₂ and the properties of the obtained catalysts, but there is very little information about the vanadium alkoxide-support interaction, the relationship between dispersion and vanadium load, the amount of adsorbed vanadium corresponding to the monolayer, and the effect of calcination on surface modification. Lakshmi et al. [21] have used the sol-gel method to prepare vanadium catalysts supported on TiO₂–SiO₂ and Zr₂O–SiO₂. Murgia et al. [15] suggested that a preparation method, which causes the vanadium to be distributed homogeneously at the surface and in the bulk, was preferred over a method which deposits vanadium only at the surface. The investigation of the catalytic properties of vanadia supported catalysts in propane ODH showed that more selective catalysts were obtained on basic metal oxide supports [13]. The presence of basic sites enhances the fast desorption of the produced olefins from the catalytic surface, resulting in higher selectivities. Furthermore, Galli et al. [22] demonstrated that doping vanadia catalysts with basic promoters has a beneficial effect in n-butane ODH by increasing the olefin selectivity.

It is well know that titania allows to obtain a very good dispersion of V₂O₅ on its surface [16]. The literature data [23, 24] reported high activity of the V₂O₅/TiO₂ system in the oxidative conversion of propane at relatively low temperature (500–600 K). The addition of potassium to the TiO₂, in particular anatase, provides an optimal chemical environment for the vanadium oxide catalytic action. Grzybowska et al. [24] suggested that the potassium hinders the formation of the electrophilic O⁻ species responsible for total oxidation of hydrocarbon. The butane oxidation over both monolayer and multilayer vanadia on TiO₂ has been reported [25, 26].

In the present paper, vanadia catalysts prepared by impregnating ammonium vanadate on a titania support were investigated. We report catalytic results obtained with 15% V catalyst supported on TiO₂ for the oxidative dehydrogenation (ODH) of n-butane. Our goal was to examine the effect of active metal at loadings exceeding a theoretical monolayer coverage. To study the effect of promoter on the catalytic performance, a sample of V/TiO₂ with addition of 5 wt% La₂O₃ (equivalent to 4.6 wt% La) was prepared. The reason for choosing La is to investigate the effect of La doping on the acid-base property of the catalyst. Due to the basicity of La₂O₃ [27] we expect the catalytic behaviour of the La-containing V/TiO₂ to be different from that of La-free V/TiO₂.

2. Experimental

2.1. Catalysts Preparation and Characterization

A commercial TiO₂ (anatase Aldrich) was used as a support. Vanadium oxide was deposited on the support by wet impregnation using aqueous NH₄VO₃ (Merck) solution. Prior to impregnation the TiO₂ support was calcined at 600°C for 3 hours. An aqueous solution of ammonium metavanadate was prepared and heated slowly. Oxalic acid (Merck) was added to the solutions (NH₄VO₃/oxalic acid = (1/2) molar) to ensure dissolution of precursor. The nominal weight loading of V was 15 wt.%. This solution was then added to an aqueous TiO₂ slurry. The resulting solution was stirred and heated until all the water was evaporated. Sample was dried overnight and calcined in air at 600°C for 4 hours. The catalyst is denoted by VT. LaV-containing TiO₂ was prepared from slurries containing aqueous solutions of ammonium metavanadate and lanthanum chloride (Aldrich). The solid obtained was then heat-treated in flow oxygen at 600°C for 4 hours (named as LaVT). The nominal weight loading of La₂O₃ was 5 wt%.

Powder X-ray diffraction (XRD) patterns were obtained using a BRUCKER D8-Advance 5005 diffractometer and Cu Kα radiation.

Specific surface areas were measured by the multipoint BET analysis method using N₂ adsorption isotherms at 77 K. The measurement was performed on TriStar 3000 analyser (Micromeritics).

Temperature programmed reduction (TPR) experiments with H₂ were carried out in a gas flow system. NH₃-temperature programmed desorption (NH₃-TPD) was used to determine the acid properties. The H₂-TPR and NH₃-TPD experiments were carried out using a Micromeritics model AutoChem II 2920. UV-Vis spectra of fresh catalysts were collected using a Cary 5000 Varian equipment.

2.2. Catalytic Tests

ODH of n-butane was performed in a fixed-bed quartz tubular reactor at atmospheric pressure and under steady state conditions. The catalyst samples (0.2 g with a 0.5 to 0.7 mm particle size) and silicon carbide were packed into the reactor to maintain a constant volume in the catalytic bed. The flow rate was 32 mL/min, and the feed comprised a mixture of n-butane, oxygen, and nitrogen with a volume ratio of 3 : 1 : 6. The reaction temperature range varied between 400°C and 550°C to achieve different conversion levels. Reactants and reaction products were analyzed in line using Trace Gas Chromatograph Ultra RGA (Thermo Scientific) equipped with a thermal conductivity detector (TCD). Three columns in a series-bypass configuration were used in the analysis: BEEA, 27.5% on Chromosorb PAW, Hayesep Q, and Mol Sieve 5A. Conversions and the selectivities to the reaction products were defined as follows: where = C₄H₈, CO, CO₂, and others (CH₄, C₂H₆, C₃H₈, C₃H₆, etc.).

Blank runs carried out in the empty-volume reactor at 550°C allowed ruling out the occurrence of gas-phase reactions to a significant extent at the experimental conditions used for the activity tests. The dehydrogenation of n-butane had also been performed on the catalysts in the absence of oxygen in the feed. The obtained conversions can be negligible (5%). Also the ODH of n-butane was tested over pristine TiO₂, and the obtained results indicated a very poor catalytic activity.

3. Results

3.1. Catalyst Characterization

3.1.1. X-Ray Diffractions

The X-ray diffraction patterns of pure TiO₂, VT, and LaVT samples were displayed in Figure 1. The solids corresponded to well-crystallized pure phase. The characteristic peak at ca. 2θ = 25.4° corresponding to (101) plane of anatase phase is clearly observed in all samples. For the pure one, no peak brookite phases of TiO₂ are observed, and peak for rutile is also hardly seen. However, weak peaks for rutile are clearly detected in XRD pattern of VT and LaVT samples indicating an interaction between active phase and the support. As it can be seen, for VT and LaVT catalysts, crystalline V₂O₅ was detected, and an increase in the intensity of the anatase reflex, at 25.4°, can be observed. This phenomenon has already been observed [20]. That is, when vanadium is not uniformly dispersed on the surface it promoted the formation of anatase crystallites during the catalyst calcination. Sample with low lanthanum loading did not show any diffraction lines corresponding to La-containing compound suggesting that XRD analysis cannot give information about the molecular dispersion of La species.

3.1.2. BET Measurements

The characteristic properties of the catalytic materials prepared are shown in Table 1. It was found that the modification of parent samples did not significantly change the structure of these materials. The changes in illustrate a pronounced reduction of the surface due to the vanadium oxide impregnation. The surface area of the samples varied from 56 m²/g (parent TiO₂) to 27 m²/g for VT and to 11 m²/g for LaVT. This could be explained as follows: at high calcination temperature, big crystallites of V₂O₅ and additional crystalline LaVO₄ were formed. The formation of crystalline V₂O₅ as well as vanadate of La could be a reason for the drastic decrease of BET surface areas. However, the process of phase separation, being associated with a loss of specific surface area, could not be suppressed by doping with La, and thus La has no stabilising influence on the V centres.

3.1.3. UV-Vis Spectra

The UV-Vis spectroscopy provides information about the character and oxidation state of vanadium. The obtained UV-Vis spectra for both prepared samples are presented in Figure 2. For quantitative analysis of all types of surface vanadium complexes, the spectra were deconvoluted into individual bands. The deconvolution spectra, using symmetric Gaussian curves, showed that bands related to the tetrahedral and octahedral species were observed for all solids. The octahedral species were related to V⁵⁺ ions which present characteristic absorption bands between 350 and 500 nm, while highly dispersed tetrahedral species of V⁵⁺ could be related to contributions between 280 and 340 nm [15, 16]. In present work, we suggest that the bands observed at 244.3 nm (for VT) and 246.1 nm (for LaVT) correspond to titanium ions in octahedral coordination [28]. The band at 218 nm originated from isolated VO₄ tetrahedra. For VT catalyst, absorption bands around 300–350 nm can be assigned to charge transfer transitions of tetrahedrally coordinated V⁵⁺ species [15, 16]. But the position of the third band (336.4 nm) suggested that the species are low oligomeric VO₄ tetrahedra rather than isolated. The band at 400–430 nm pointed to the presence of V⁵⁺ in octahedral coordination. The small absorption around 480 originates most likely from some polymeric octahedrally coordinated vanadium sites. Low intensity of this band suggested that the octahedral V species play only a minor role in this material.

(a)

(b)

The UV-Vis spectrum of the La-doped V/TiO₂ catalyst was quite similar to that of the undoped one. However the relative intensity of the band around 300–350 nm was lower than that in the undoped suggesting that tetrahedral V centres might also be polymerized lower than La-free sample. Moreover the relative intensity of the band around 450 nm, indicating the presence of higher coordinated V species, is much higher than that in undoped sample, and its relative intensity with respect to the overall UV-vis intensity was the highest in comparison to other bands. This indicates that La does not support the dispersion of V sites.

3.1.4. H₂-TPR Spectra

The reducibility of the catalysts was measured by means of H₂-TPR. The H₂-TPR of VT and LaVT were plotted in Figure 3. For comparison, the H₂-TPR profiles of parent TiO₂ and pure V₂O₅ were also plotted. It is clear that TiO₂ was hardly reduced at the temperatures lower than 800°C. In pure V₂O₅ the first reduction peak appeared at above 600°C. However lower reduction temperatures were observed in VT and LaVT catalyst samples indicating the interaction between active sites and the support.

The deconvolutions of H₂-TPR profiles of VT and LaVT were shown in Figure 4. The TPR profiles of VT and LaVT consisted of several peaks. This points to the presence of different species, differing in their reduction stability, and is in agreement with the results of UV-Vis and XRD. The existence of VO₄ isolated species was confirmed by TPR of the studied samples. According in the literature [7] the first reduction peak is ascribable to the reduction of surface V⁵⁺ species in distorted VO₄ species while the high temperature would correspond to the reduction of V⁵⁺ belonging to the bulk orthovanadate. In VT the TPR deconvolution showed reduction peaks centred at 496.4°C and 570.9°C. In LaVT these peaks shifted to higher temperatures 528°C and 608°C. In the same order, the vanadium dispersion decreased owing to a dramatic loss of surface area, which favours the formation of polymerised V species or even crystalline vanadates of La. Therefore, the TPR results indicated that less polymerised vanadium species can be move easily reduced than V centres in condensed phases. The peaks appearing at around 743°C for LaVT and 628°C for VT arose probably from the reduction of crystalline V₂O₅ and LaVO₄ [29].

(a)

(b)

3.1.5. NH₃-TPD

The surface acidic properties of VT and LaVT samples investigated by NH₃-PTD were compiled in Figure 5. The NH₃ desorption patterns which indicated acid sites of weak and moderate strengths were present on the catalysts. However, the presence of La decreased the moderate acid sites, and also the total NH₃ desorption in LaVT sample (3.72 mL/g catalyst) was lower than that in VT sample (4.33 mL NH₃/g catalyst). The obtained results suggested that the surface acidity of the LaVT sample was diminished by La doping.

(a)

(b)

3.2. Catalytic Tests for n-Butane Oxidative Dehydrogenation

3.2.1. Catalytic Activity

Table 2 shows conversion of n-butane and the distribution of reaction products, obtained at each temperature over VT and LaVT catalysts. For comparison, the conversion of n-butane over pristine TiO₂ and bulk V₂O₅ is also presented, but the obtained conversions can be negligible. Figure 6 shows the variation in n-butane conversion and total alkene’s selectivity with the reaction temperature.

(a)

(b)

From data reported in Table 2 the major products formed under reaction conditions with 10% O₂ as coreactant were 1-butene (1-b), tran-2-butene (2-trans), cis-2-butene (2-cis), butadiene, (C₄-1,3) CO₂, CO, and cracking products (methane, ethane, ethane, and propene). It is possible to observe an effect of the support on the activities and selectivities of vanadium based catalysts in the ODH of n-butane in agreement with the observations of many different authors reported in the literature [30]. Generally, the conversions increase with the temperature, whereas the selectivities decrease, as usual, with the conversion. Also, it was demonstrated that [20] the activity of the dispersed catalysts can be roughly related to the vanadium load. Santacesaria et al. [20] reported a conversion of 3.2% and corresponding selectivity of 51.1% obtained for the ODH of n-butane over a 5% V/TiO₂ catalyst at 500°C. However, their experimental conditions differed from those in this work: the content of V was 5% (wt.), and catalyst weight was 0.05 g (meanwhile they are 15% and 0.2 g, resp., in this work); in their work, the total feed low rate was 150 mL/min, and O₂/C₄H₁₀ ratio was 1.7. Therefore the differences in catalytic behaviour between our samples and theirs are quite reasonable.

It can be seen that, at the same vanadium loading, although La-free (VT) catalyst is slightly less selective than the respective (LaVT) sample in the studied temperature range (400–550°C), it is slightly more active (in terms of butane conversion) than the LaVT. It can be readily seen in Figure 7 that the intrinsic activity evidenced by surface area specific rates () and the corresponding turnover of the catalysts have a tendency to increase with the temperature. Moreover it can be seen that LaVT presented a lower activity compared to that of VT catalyst. This trend points to a decreasing number of ODH sites with LaVT. Since present characterizations of the materials indicated higher crystallinities in LaVT than in VT, the trend of turnover values and specific activities in Figure 7 was consistent with an inverse relationship between crystallinity and turnover and specific activity.

(a)

(b)

3.2.2. Product’s Distribution

Variation of the selectivity to the main reaction products as a function of temperature on both samples was presented in Table 2. Results in Table 2 showed that over both catalyst samples CO₂ and CO were formed at low butane conversion. This is in agreement with the reports of Murgia et al. [15]. Products were slightly decreased as conversion increased. Figures 8 and 9 plot the product distrubitions against reaction temperatures. For VT sample the main reaction product was 1-butene in the whole range of studied temperatures while no measurable selectivity toward butadiene was found. Dias et al. [7] studied ODH of n-butane over Mg-V catalysts and showed that 1-butene was a main product; however for higher reaction temperatures (above 748 K) butadiene was a major product. The selectivity towards 2-butenes was always lower than selectivity towards 1-butene. Similar results were observed by Murgia et al. [15] and Jackson and Rugmini [9]. The ratio tran/cis was approximately constant and equal to 1.42. An analogous ratio for the ODH of n-butane over 5 wt.% V₂O₅/TiO₂ was reported by Santacesaria et al. [20]. Figures 6 and 8 showed that the selectivity towards butenes decreased as conversion increased due to the consecutive reactions. Similar trends are observable for other catalysts reported in the literature [16, 20]; that is, conversion increases with the residence time, while selectivity to alkene products decreases.

(a)

(b)

The catalytic behaviour of LaVT sample was similar to VT sample. Taking into account the surface acidity of the samples, the LaVT exposed a higher selectivity than VT. The reaction products distribution was approximately the same: 1-butene was the main product, and the ratio trans/cis was constant and equal to 1.6. Especially, LaVT produced butadiene. Butadiene was formed by consecutive reactions, and competition due to carbon oxide formation from both butyl radicals and butenes [31].

Figure 9 shows the selectivities of alkenes over LaVT and VT catalysts samples at 550°C. It can be seen that the LaVT has a slightly higher selectivity of alkenes than VT.

The catalytic behaviour of LaVT sample could be attributed to the following.(i)Doping La resulted in an increase in basicity of catalyst sample (TPD-NH₃ results), and it was expected that this change will affect the catalyst selectivity but not the activity. The best selectivity induced by the presence of La₂O₃ is a well-known phenomenon described in the literature [27]. Hoang et al. [27] studying the ODH of isobutane over chromium oxide base catalysts indicated that, when La₂O₃ is present in the support, the activity is low, but the selectivity was almost 100%.(ii)The presence of La species lowers the surface area and thus also the surface vanadium dispersion due to blocking active sites (BET measurement and UV-Vis spectra) and increased reduction temperatures (TPR-H₂ results). These may have a negative effect on the catalytic performance of VT catalyst.

4. Conclusions

V catalysts supported on titania at exceeding theoretical monolayer coverage and doping with lanthanum were tested in the oxidative dehydrogenation of n-butane. In the tested conditions 1-butene was the main reaction products. Characterization of the materials showed that surface species are well dispersed on the support surface. Acidity measurements revealed that the catalyst samples possess acid sites of weak and moderate strengths. La-containing exhibited lower acidity than La-free one, and doping with lanthanum did not improve the catalytic performance of VT catalyst. The low activity could be explained with the lower dispersion of species in this sample since it favours the agglomeration of V sites. Despite the observation that lanthanum-doping improved slightly the butene selectivies due to lowered surface acidity, this could not improve the yields of butene. Therefore, it seems likely that improvement of the butene yields in the ODH of n-butane could be achieved using catalysts with highly dispersed, preferably tetrahedrally coordinated species, supported on nonacidic materials with high surface area.

Acknowledgments

This work was supported by National Foundation for Science and Technology Development Vietnam (NAFOSTED) under Project no. 104.03-2010.39.

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Copyright © 2013 Le Minh Cam 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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Journal of Chemistry

Oxidative Dehydrogenation of n-Butane over LaV Catalysts Supported on TiO2

Abstract

1. Introduction

2. Experimental

2.1. Catalysts Preparation and Characterization

2.2. Catalytic Tests

3. Results

3.1. Catalyst Characterization

3.1.1. X-Ray Diffractions

3.1.2. BET Measurements

3.1.3. UV-Vis Spectra

3.1.4. H2-TPR Spectra

3.1.5. NH3-TPD

3.2. Catalytic Tests for n-Butane Oxidative Dehydrogenation

3.2.1. Catalytic Activity

3.2.2. Product’s Distribution

4. Conclusions

Acknowledgments

References

Copyright

Oxidative Dehydrogenation of n-Butane over LaV Catalysts Supported on TiO₂

3.1.4. H₂-TPR Spectra

3.1.5. NH₃-TPD