Fluidized CREC Riser Simulator Research Articles

A Kinetic Model for Catalytic N-Butane Oxidative Dehydrogenation under Oxygen-Free Reaction Conditions in a Fluidized CREC Riser Simulator

This study considers the development of a kinetic model for the n-butane oxidative dehydrogenation (ODH) to C4-olefins using a VOx/MgO−γAl2O3 catalyst. The prepared catalyst contained 5 wt% V on an MgO modified γAl2O3 support. The developed catalyst exhibited both weak and medium acid sites, as revealed by NH3-temperature-programmed desorption. TPR/TPO analyses also indicated that 73% of the loaded VOx was reducible. Kinetic experiments were conducted in a fluidized CREC Riser Simulator at temperatures ranging from 475–550 °C and residence times of 5–20 s. An optimal C4-olefin selectivity of 86% was achieved at 500 °C and 10 s, with this selectivity then decreasing at higher temperatures and longer residence times. The kinetic model developed involved a Langmuir–Hinshelwood-type of kinetics that incorporated cracking, oxydehydrogenation, and complete oxidation reactions. Model parameters were determined by fitting experimental data with kinetic parameters established with narrow 95% confidence intervals and low cross-correlation.

Ga2O3/La2O3-γAl2O3 catalysts for CO2-assisted propane oxidative dehydrogenation to propylene

Novel Ga2O3/La2O3-γAl2O3 was investigated for ODH of propane to propylene using CO2 as a mild oxidant in a batch scale fluidized CREC Riser Simulator. La2O3 in the catalysts provided a control of both the reducibility and acidity, as shown by H2-TPR and NH3-TPD, respectively. The propane conversion and products selectivity were strong function of La2O3 content in the Ga2O3/La2O3-γAl2O3 catalysts. With increasing La2O3 content in the catalyst, propane conversion dropped slightly but the propylene selectivity and yields increased. It was proposed that the presence of La2O3 reduced the non-selective sites and the acidity of the catalysts, that contributed towards deep oxidation of propane and propylene. The improved activity and selectivity with CO2 addition implied that the as-synthesized catalyst possesses CO2 activation capability required for ODH reactions. Among the investigated catalysts, Ga2O3/La2O3-γAl2O3(1:1) exhibited the highest propane conversion (92 %) and propylene yield (56 %) at 600 ℃ in the presence of CO2.

A Fluidizable Catalyst for N-Butane Oxidative Dehydrogenation under Oxygen-Free Reaction Conditions

This study evaluates the effectiveness of fluidizable VOx/MgO-γAl2O3 catalysts for C4-olefin production via n-butane oxidative dehydrogenation (BODH). Catalysts were prepared via vacuum incipient wetness impregnation and then characterized by employing several techniques such as BET (Brunauer–Emmett–Teller) method, XRD (X-ray diffraction), LRS (laser Raman spectroscopy), XPS (X-ray photoelectron spectroscopy), TPR/TPO (temperature-programmed reduction/temperature-programmed oxidation), NH3-TPD (temperature-programmed desorption), NH3 -desorption kinetics and pyridine-FTIR. The BET analysis showed the prepared catalysts’ mesoporous structure and high surface areas. The XRD, LRS and XPS established the desirable presence of amorphous VOx phases. The TPR/TPO analyses corroborated catalyst stability over repeated reduction and oxidation cycles. The NH3-TPD and NH3 desorption kinetics showed that the catalysts had dominant moderate acidities and weak metal-support interactions. In addition, Pyridine-FTIR showed the critical influence of Lewis acidity. The VOx/MgO-γAl2O3 catalysts were evaluated for BODH using a fluidized CREC Riser Simulator, operated under gas-phase oxygen-free conditions, at 5 to 20 s reaction times, and at 450 °C to 600 °C temperatures. The developed VOx/MgO-γAl2O3 catalysts demonstrated performance stability throughout multiple injections of butane feed. Catalyst regeneration was also conducted after six consecutive BODH runs, and the coke formed was measured using TOC (Total Organic Carbon). Regarding the various BODH catalyst prepared, the 5 wt% V-doped MgO-γAl2O3 yielded in a fluidized CREC Riser Simulator the highest selectivity for C4-olefins, ranging from 82% to 86%, alongside a butane conversion rate of 24% to 27%, at 500 °C and at a 10 s reaction time.

In-situ reforming and combustion of liquid fuel using MnOx/Ce-γAl2O3 oxygen carrier in a chemical looping combustion process

A new MnOx/Ce-γAl2O3 oxygen carrier is developed for liquid fuel based fluidized chemical looping combustion (CLC) process. The developed material serves both as a catalyst and as a source of solid phase oxygen for gasification/reforming of liquid fuel followed by the combustion of the gasified products. The support γAl2O3 is modified with cerium, improved thermal stability and minimized the interaction with the main active component MnOx. In order to validate the desired properties, the prepared MnOx/Ce-γAl2O3 samples are characterized using various physicochemical characterizations, including X-ray fluorescence (XRF), nitrogen adsorption, thermogravimetric analysis (TGA), X-ray diffraction (XRD), scanning electron microscope (SEM), temperature programmed reduction (TPR), and temperature programmed desorption (TPD). TPR, TGA and XRD analysis confirm that the Ce modification improves the thermal stability of γAl2O3 and hinders the formation of difficult reducing manganese aluminate. TPR profiles show excellent reduction and re-oxidation performances of the Ce modified samples. Based on characterizations, a selected sample is further evaluated in a fluidized CREC Riser Simulator (CREC: Chemical Reactor Engineering Centre) using n-hexane as a liquid fuel surrogate. Under the studied reaction conditions (500–650 C; 10–45 s reaction time), CO2 and CO are the main combustion products. At 650 °C, approximately 92% n-hexane combustion and 60% of CO2 selectivity was achieved, which is very encouraging, given the complexity of the interaction of liquid fuel with the solid metal oxides.

Promotional effects of CO2 on the oxidative dehydrogenation of propane over mesoporous VOX/γAl2O3 catalysts

CO2 assisted oxidative dehydrogenation (ODH) propane to propylene over fluidizable mesoporous VOx/La2O3-γAl2O3 catalysts has been investigated. The mixed oxide of La2O3 and γAl2O3 were synthesized by the co-precipitation technique and VOx was deposited on the supports by an incipient wetness impregnation approach. The prepared catalysts were characterized by various physicochemical characterizations to establish the desired properties of the catalysts. The H2-TPR indicated the supported VOx reduced in a single stage, indicating the formation of a homogeneous specie. Both the acidity and surface area of the catalysts decreased with increase of La content, as confirmed by the NH3-TPD and BET analysis, respectively. The CO2 assisted ODH of propane experiments were developed in a fluidized CREC Riser Simulator at 520–600°C. The introduction of CO2 significantly enhanced both the propane conversion and propylene selectivity. Among the studied catalysts, VOx/γ-Al2O3 catalyst showed highest propylene yields (42.7%) at 550°C.

CO2 Assisted Oxidative Dehydrogenation of Propane to Propylene over Fluidizable MoO3/La2O3-γAl2O3 Catalysts

Abstract This study investigated the catalytic performance of a novel fluidizable MoO3 supported on La2O3-γAl2O3 composite for oxidative dehydrogenation (ODH) of propane to propylene with and without CO2. The La2O3-γAl2O3 composites were synthesized by a coprecipitation method, while the active MoO3 was deposited by an incipient wetness impregnation approach. The incorporation of La2O3 controlled both the acidity and reducibility of the catalysts, as revealed by NH3-TPD and H2-TPR analysis, respectively. The N2 adsorption/desorption isotherms analysis indicated the mesoporous pore size distribution of the catalysts. The ODH of propane experiments were developed in a fluidized CREC Riser Simulator by feeding propane with or without CO2. The performance of the synthesized catalysts was found to be a function of the La2O3 content of the support. In general, the propane conversion declined slightly, while propylene selectivity increased with the increasing La2O3 content. It was hypothesized that the presence of basic La2O3 reduced the acidity and the non-selective sites of γ-Al2O3, which were responsible for deep oxidation of propylene and propane. Among the studied catalysts, MoO3/La2O3-γAl2O31:2 displayed the highest propylene yield of 28.2 % at 600 ℃ in the absence of CO2. However, a superior yield of 35.2% was achieved over the same catalyst by the introduction of CO2-admixture in the feed at 550 ℃.

Hydrogen production via surrogate biomass gasification using 5% Ni and low loading of lanthanum co-impregnated on fluidizable γ-alumina catalysts

Abstract Nickel on alumina support offers opportunity for gasification of biomass for hydrogen production. In a recent contribution from our research team, (González Castañeda, D. G., et al. 2019) showed that cerium or lanthanum co-impregnation at 2 wt% with nickel may have a favorable effect for biomass catalytic gasification. However, and given an observed influence of lanthanum on the formation of small Ni crystallite sizes, five Ni/γ-Al2O3 based fluidizable La promoted catalysts were studied. Nickel-alumina catalysts promotion was effected varying La in the 0.5 and 1.0 wt% range. Once impregnation precursors loaded, they were reduced at 480 °C via an activation step. Catalysts were characterized using BET, XRD, AA, TPR, TPD, H2-chemisorption, TEM-EDX and FTIR. Catalyst performance was established in a fluidized CREC Riser Simulator, using: a) glucose as surrogate biomass, b) 600 °C, c) steam/biomass (S/B) ratio of 1, d) catalyst /biomass (C/B) ratio of 3.2 and e) 20 s reaction time. Data obtained was analyzed using an ANOVA statistical data analysis package with the 5 wt% Ni and 0.5–1 wt% La and Ce on γ-Al2O3 catalysts, prepared using a pH of 1 of impregnating solution were the best yielding 0.53–0.56 hydrogen molar fractions. These catalysts also gave a 39% reduced coke, and this while compared with the coke formed on the 2% Ce – 5 wt%Ni/γ-Al2O3 (González Castañeda, D. G., et al. 2019). This promising performance was assigned to the dominant NH3-TPD medium acidity, the high catalyst specific surface (∼140 m2/g), and the good 9% metal dispersion with 9–10 nm nickel crystallites.

An Eco-Friendly Fluidizable FexOy/CaO-γ-Al2O3 Catalyst for Tar Cracking during Biomass Gasification

The present study deals with the development, characterization, and performance evaluation of an eco-friendly catalyst, using 2-methoxy-4-methylphenol (2M4MP) as a surrogate tar. The 2M4MP was selected due to its chemical functionalities and the fact that it is a good model compound to represent the tar formed during biomass low temperature gasification. The eco-friendly catalyst was prepared using the typical Fe and Ca minerals which are present in ash. These ash components were added to a fluidizable γ-Al2O3 support using a multistep incipient impregnation, yielding Fe oxides as an active phase and CaO as the promoter. The prepared catalyst displayed a 120 m2/g BET specific surface area, with few γ-Al2O3 bulk phase changes, as observed with XRD. TPD-NH3 and pyridine FTIR allowed us to show the significant influence of CaO reduced support acidity. A TPR analysis provided evidence of catalyst stability during consecutive reduction–oxidation cycles. Furthermore, catalyst evaluation vis-à-vis catalytic steam 2M4MP gasification was performed using the fluidized CREC riser simulator. The obtained results confirm the high performance of the developed catalyst, with 2M4MP conversion being close to 100% and with selectivities of up to 98.6% for C1-C2 carbon-containing species, at 500 °C, with a 7.5 s reaction time and 1.5 g steam/g 2M4MP. These high tar conversions are promising efficiency indicators for alumina catalysts doped with Fe and Ca. In addition, the used catalyst particles could be blended with biochar to provide an integrated solid supplement that could return valuable mineral supplements to the soil.

High-performance VOx on SrO-γAl2O3 catalyst for oxidative cracking of n-hexane to light olefins under anaerobic environment

Novel VOx/SrO-γAl2O3 catalysts have been investigated in oxidative cracking of n-hexane to light olefins. The supports, with different SrO/γAl2O3 ratios, were synthesized by a surfactant-free method, while VOx was incorporated on SrO-γAl2O3 by impregnation. NH3-TPD showed that the acidity of the catalysts decreased with the increase of SrO. The incorporation of SrO also modified the reducibility (H2-TPR) of the catalysts. VOx appeared as amorphous polymeric species on the support, confirmed by XRD, Raman and FTIR analyses. The oxidative cracking of n-hexane was conducted by using a fluidized CREC Riser Simulator in absence of gas phase oxygen. Under the studied reaction conditions (525−600°C; 10−25s), the products contained mainly light olefins (ethylene, propylene and butenes), paraffins, and carbon oxides. Among the synthesized catalysts, VOx/SrO-γAl2O3 1:1 showed highest olefins selectivity (88%) at high n-hexane conversion (84%) because of its balanced acidity and moderate VOx-support interactions.

Ru-Promoted Ni/Al2O3 Fluidized Catalyst for Biomass Gasification

Fluidizable catalysts based on Ni/Al2O3 with added Ru were used for the gasification of a lignin surrogate (2-methoxy-4-methylphenol) in a fluidized CREC Riser Simulator reactor. This was done in order to quantify lignin surrogate conversion and lignin surrogate products (H2, CO, CO2 and CH4) as well as the coke deposited on the catalyst. The catalysts that were evaluated contained 5% wt. Ni with various Ru loadings (0.25%, 0.5% and 1% wt). These catalysts were synthesized using an incipient Ni and Ru co-impregnation. Catalysts were characterized using XRD, N2 adsorption-desorption (BET Surface Area, BJH), Temperature Programmed Reduction (TPR), Temperature Programmed Desorption (TPD) and H2 chemisorption. Catalytic steam gasification took place at 550, 600 and 650 °C using 0.5, 1.0 and 1.5, steam/biomass ratios. The results obtained showed that Ru addition helped to decrease both nickel crystallite site sizes and catalyst acid site density. Moreover, it was observed that coke on the catalyst was reduced by 60%. This was the case when compared to the runs with the Ni/Al2O3 free of Ru.

Downer fluidized bed reactor modeling for catalytic propane oxidative dehydrogenation with high propylene selectivity

This study reports a simulation of the catalytic propane oxidative dehydrogenation (PODH) in a circulating fluidized bed downer reactor. A relevant kinetics based on experimental work by the authors (Rostom and de Lasa, 2018), developed in a fluidized CREC Riser Simulator is considered. As well, Computational Particle Fluid Dynamics (CPFD) models featuring either “Particle Clusters” or “Single Particles” flows are implemented. The CPFD results obtained in a 20-m length unit show a 28% propane total conversion and 93% propylene selectivity using the “Single Particle” flow model. However, and once the more rigorous particle cluster flow is accounted for, the propane conversion is reduced significantly to 20%, while the propylene selectivity remains at 94% level. Thus, the obtained results show that, a PODH simulation using CPFD, requires one to account for “Particle Clusters”. This type of comprehensive model is required to establish unambiguously the downer reactor performance and is of critical value for the development of downflow reactors for other catalytic processes.

Syngas chemical looping combustion using a highly performing fluidizable oxygen carrier

• A high performing 20 wt%Ni-1 wt%Co-5 wt%La/γ-Al 2 O 3 oxygen carrier is reported. • The preparation method secures a stable fluidizable OC with enhanced reactivity. • This OC carrier is suitable for biomass gasification derived syngas combustion. • This OC yields up to 92% CO 2 yields in the 550-650 º C range. • This OC is free from NiAl 2 O 4 formation in the targeted temperature operating range. Biomass steam gasification produces a blend of H 2 , CO, CH 4 and CO 2 , designated as syngas. Syngas can be further combusted using fluidizable oxygen carriers (OC). This operation which is known as Chemical Looping Combustion (CLC), is valuable for syngas combustion as it involves nickel oxidation and nickel reduction, which are both exothermic reactions. To improve syngas CLC and establish its application, a new Ni-based oxygen carrier was studied using a Co and La modified γ-Al 2 O 3 support. This type of OC considerably limits the NiAl 2 O 4 formation. A Highly Performing Oxygen Carrier (HPOC) was engineered using a special preparation methodology to exclude NiAl 2 O 4 species formation. The evaluation of this HPOC was developed using the fluidized CREC Riser Simulator reactor at mild CLC 550–650 °C temperatures. Reaction conditions employed ranged from 2 to 40 s and used a 0.5–1 fuel to oxygen stoichiometric supply ratio (ψ). It is shown that under these conditions, the HPOC demonstrates a stable performance, yielding 75–92% CO 2 , displaying a 1.84–2.75 wt% (gO 2 /gOC) oxygen transport capacity with 40–60% solid phase oxygen conversion.

Fluidizable Ni/Ce-meso-Al2O3 for gasification of glucose: Effect of catalyst reduction on hydrogen selectivity

A new template-free technique is applied to develop fluidizable Ce-Al2O3 support and impregnated with nickel. The Ni(x)/Ce-Al2O3 catalysts are evaluated in a fluidized CREC Riser Simulator using glucose as biomass surrogate. XRD shows that nickel is well-dispersed on Ce-Al2O3. The acidity of the catalysts decreased from 0.317 to 0.202mmol NH3/g-sample as the nickel loading was increased. In catalyst evaluation, it is found that the reduced catalysts favor bond cleavage, promotes water gas shift and steam reforming reactions to give hydrogen/syngas as more selective products. Ni(20)/Ce-Al2O3 exhibited lowest extent of coking and produced hydrogen rich syngas with H2/CO≈1.75:1.

Fluidizable NiO–Fe 2 O 3 /SiO 2 –γAl 2 O 3 for tar (toluene) conversion in biomass gasification

Abstract This communication reports synergetic effects of bimetallic Ni–Fe on NiO–Fe2O3/SiO2–γAl2O3 catalysts for biomass tar (toluene) conversion. The catalysts were successfully synthesized using a one-pot, solvent-deficient method and characterized using XRD, N2 adsorption isotherm and NH3-TPD techniques. The introduction of SiO2 enhanced thermal stability of the NiO–Fe2O3/SiO2–γAl2O3 catalysts, as observed in XRD and BET surface area analysis. The synthesized NiO–Fe2O3/SiO2–γAl2O3 catalysts showed high BET specific surface area (52–58 m2/g) even after calcination at 950 °C. The NH3-TPD analysis exhibited that the addition of NiO significantly decreased the strong acid sites of the NiO–Fe2O3/SiO2–γAl2O3 catalysts. The performance of the synthesized catalysts were evaluated in a fluidized CREC Riser Simulator using toluene as a tar model compound. The NiO containing NiO–Fe2O3/SiO2–γAl2O3 catalyst yielded high toluene conversion with higher H2 concentration in the produced gas, as compared to Fe2O3/SiO2–γAl2O3 catalyst. The presence of nickel promoted both methane reforming and water-gas shift reactions, contributed to higher H2 concentration in the producer gas. A gasification process model, as developed in Aspen Plus, also showed that hydrogen composition of the producer gas can also be enhanced by adjusting the gasification temperature, pressure and steam/biomass ratios. These results indicate that the NiO–Fe2O3/SiO2–γAl2O3 catalyst has a great potential for industrial use since it is a relatively cheap, less toxic, and stable for extended period of gasification operation. The spent catalyst materials are also useful to produce other commercial products, such as Portland cement and glass-ceramics.

Fluidized bed oxidative dehydrogenation of ethane to ethylene over VOx/Ce-γAl2O3 catalysts: Reduction kinetics and catalyst activity

Cerium-doped γ-Al2O3 (Ce-γAl2O3) catalyst supports are prepared with various amounts of cerium (0.2–5wt.%). An excess solvent impregnation method is used to saturate the vanadium (5wt%) on the cerium-modified supports. The XRD and FTIR characterization techniques indicate the presence of crystalline CeO2 phase, and amorphous VOx phases on the γAl2O3. Raman analysis shows the coexistence of poly-vanadate and mono-vanadate species. BET analysis reveals a high surface area for the synthesized catalysts with a type-IV adsorption isotherm. TPR/TPO analyses show that VOx/Ce-γAl2O3 catalysts are very active and stable over repeated reduction/oxidation cycles. The stability/purity of the synthesized catalyst is also confirmed by TGA analysis. NH3-TPD characterization shows mild acidity while the TPR kinetics predicts lower activation energy for reduction. Oxidative dehydrogenation (ODH) of ethane experiments are developed over VOx/Ce-γAl2O3 catalysts under gas-phase oxygen-free conditions in a fluidized CREC Riser Simulator. Temperatures and residence times are varied between 450 and 600°C and 10–50s, respectively. A maximum ethylene selectivity of 87.9% with 10.0% ethane conversion is achieved at 550°C using the 1.0wt.% cerium-doped VOx/γ-Al2O3 catalyst. The successive ethane injections and subsequent catalyst regeneration show the stable redox characteristics of the prepared ODH catalysts.

Phenomenologically based kinetics of ODH of ethane to ethylene using lattice oxygen of VOx/Al2O3–ZrO2 catalyst

This study addresses the kinetic modeling of ethane oxidative dehydrogenation (ODH) over a 10%wt VOx catalyst supported on Al2O3–ZrO2 (1:1) in the CREC Riser Simulator Reactor. The catalyst was synthesized using impregnation by a soaking method. Following this, the catalyst was characterized using BET, XRF, TPR, NH3-TPD and Raman Spectroscopy. The ODH catalyst was studied in a fluidized CREC Riser Simulator at a temperature range of 525–600°C and with 20–50s contact time. Good ethylene selectivity of up to 82% at 8.5% ethane conversion was attained. A kinetics model was established using a Langmuir–Hinshelwood rate equation. Catalyst activity (availability of lattice oxygen) was first modeled using TPR results. This model was then incorporated with the developed L–H model for the series-parallel reaction network. Nonlinear regression was employed to estimate kinetic parameters and activation energies with their respective confidence intervals. The proposed kinetics for ODH, satisfactorily predicted ethane conversion and selectivity at the selected operating conditions.

Structural changes in FeOx/γ-Al2O3 catalysts during ethylbenzene dehydrogenation

The structural changes that occur in a FeOx/γ-Al2O3 catalyst during the dehydrogenation of ethylbenzene in a fluidized CREC Riser Simulator have been investigated. Chemical and morphological change...

Kinetics of oxidative cracking of n‐hexane to olefins over VOx/Ce‐Al2O3 under gas phase oxygen‐free environment

The kinetics of oxidative cracking of n‐hexane to olefins using lattice oxygen of VOx/Ce‐Al2O3 is investigated. The TPR/TPO analysis shows a consistent reducibility (79%) of VOx/Ce‐Al2O3 in repeated redox cycles. The total acidity of the sample is found to be 0.54 mmol/g with 22% are strong acid sites that favors olefin selectivity. The oxidative cracking of n‐hexane in a fluidized CREC Riser simulator gives approximately 60% olefin selectivity at 30% n‐hexane conversion. A kinetic model is developed considering (1) cracking, (2) oxidative dehydrogenation (ODH), and (3) catalyst deactivations. The proposed cracking mechanism considers adsorption, C–H and C–C bond fission and desorption as elementary steps and implemented by pseudo steady state hypothesis. A Langmuir‐Hinshelwood mechanism is found to represent the ODH reactions. The developed model fits the experimental data with favorable statistical indicators. The estimated specific reaction rate constants are also found to be consistent with the product selectivity data. © 2016 American Institute of Chemical Engineers AIChE J, 63: 130–138, 2017

Reduction kinetics and catalytic activity of VOx/γ-Al2O3-ZrO2 for gas phase oxygen free ODH of ethane

Oxidative dehydrogenation (ODH) of ethane is investigated using VOx/Al2O3-ZrO2 catalysts in absence of gas phase oxygen under circulating fluidized conditions. In this approach, the catalyst particles also serve as a source of lattice oxygen. The fluidizable VOx/Al2O3-ZrO2 catalysts are prepared with various amount of VOx using a successive impregnation technique. XRF measurement confirms the consistency between the targeted and actual metal loading. Nitrogen adsorption shows type-v monolayer adsorption on VOx/Al2O3-ZrO2 surface. XRD and Raman confirm the presence of VOx species on the Al2O3-ZrO2 as a crystal phase. NH3-TPD measurement shows that the acidity of the catalysts decreases slightly with VOx loading. The VOx/Al2O3-ZrO2 catalysts are stable over repeated reduction (TPR) and oxidation (TPO) cycles. The TPR kinetics modeling reveals that the activation energy of catalyst reduction (oxygen release) increases with increasing the VOx loading. This is an indication of increasing difficulties of VOx reduction at higher VOx loading. The ODH of ethane experiments are established in a fluidized CREC-riser simulator at different temperatures (525–600°C) and reaction times (20–50s). Approximately, 89% ethylene selectivity is achieved with 10% VOx on Al2O3-ZrO2. The ethylene selectivity also remains stable over repeated ODH and catalyst regeneration cycles.

Fluidized bed ODH of ethane to ethylene over VOx–MoOx/γ-Al2O3 catalyst: Desorption kinetics and catalytic activity

Oxidative dehydrogenation (ODH) of ethane is studied in a gas phase oxygen free conditions using a VOx–MoOx/γ-Al2O3 catalyst which also acts as a carrier of lattice oxygen. The prepared catalyst and the support γ-Al2O3 are characterized using various physicochemical techniques. XRD, Raman, and FTIR analysis show the availability of VOx and MoOx species on the alumina support. The TPR analysis gives two distinct peaks for the reduction of VOx and MoOx species, respectively. The cyclic TPR/TPO shows consistent reduction behavior of the catalyst over repeated reduction and oxidation cycles. Desorption kinetics analysis reveals low activation energy for ammonia desorption from VOx–MoOx/γ-Al2O3 surface. This indicates a minimum interaction between VOx–MoOx and γ-Al2O3 confirming easy availability of lattice oxygen for reaction. The ODH of ethane experiments are conducted in a fluidized CREC Riser Simulator at temperature range of 500–650°C. The contact time is varied between 10 and 50s. Under the studied reaction conditions, ethylene, carbon dioxide, carbon monoxide and water are the major products. At fluidized condition, VOx–MoOx/γ-Al2O3 shows significant higher ethane conversion due to the intense mixing between the catalyst and the feed. High temperature and longer contact times lead to further oxidation of the desired product ethylene to give undesired products COx. In repeated ODH of ethane and re-oxidation cycles, VOx–MoOx/γ-Al2O3 shows stable ethane conversion and product selectivity which is consistent to the TPR/TPO evaluation results.