Mesoporous Organo-Silica Supported Chromium Oxide Catalyst for Oxidative Dehydrogenation of Ethane to Ethylene with CO 2

: Chromium oxide supported on mesoporous organo-silica (MOS) was synthesized with different Cr loading by an incipient method. The catalytic performance of a Cr(x)/MOS catalyst for CO 2 based ethane dehydrogenation was investigated. The synthesized catalysts were characterized by XRD, BET, TEM, SEM, XPS, FTIR, and UV–Vis DR measurements. The textural properties of the prepared samples showed that the mesoporous nature of MOS sample was not disturbed by chromium impregnation. Among the prepared samples, Cr(8)/MOS catalyst exhibited good distribution of chromium species along with superior concentration of Cr 6+ and the highest recorded Cr 6+ /Cr 3+ ratio. The results revealed that the superior catalytic performance was reached at Cr(8)/MOS, with 50.4% and 90.1% of ethane conversion and ethylene selectivity, respectively. The catalytic activity decreased slowly over reaction time; it declined approximately 22% after 10 h of stream operation. The roles of CO 2 -based ethane dehydrogenation were also studied, where carbon dioxide can be a source of lattice oxygen and as a hydrogen consumer in reverse water–gas shift (RWGS) reaction. The effect of various catalytic factors, such as catalytic temperature, reaction time, space gas velocity, and CO 2 partial pressure on the conversion of ethane, yield, and selectivity to ethylene, were investigated as well.


Introduction
Ethane to ethylene-based oxidative dehydrogenation (ODH) by implementing carbon dioxide as an oxidant has received much attention as a replacement to conventional thermal cracking processes and is a path for carbon dioxide utilization [1][2][3][4][5][6]. Among all investigated catalytic systems, chromium oxide supported over silica catalysts exhibits attractive catalytic performances for ODH of ethane with CO 2 . It has been found that an appropriate distribution of chromium species on the support surface is a basic ingredient to obtain a superior catalytic performance [7][8][9]. High dispersion of chromium species leads to high concentration of reducible Cr species which are supposed to be the active phases for the dehydrogenation of alkane with CO 2 [9]. The highly dispersed Cr 6+ species fully accessible to the reactant mixture have been recognized to be the active sites for light alkane dehydrogenation [10,11]. Therefore, more notice has been directed recently to siliceous mesoporous sieves, such as MCM-41 [12,13], SBA-15 [8], SBA-1 [7,10], and MSU-x [14,15] as supports for chromium-based catalytic systems. Due to their superior 2. Results and Discussion 2.1. Catalyst Characterization N 2 physisorption isotherms, along with mesopore size distribution of the prepared MOS support and Cr(x)/MOS catalysts, are illustrated in Figure 1A,B. The textural properties of synthesized samples such as BET-surface area, pore volume, and size are presented in Table 1. The physisorption isotherms display IV type profile with an H1 hysteresis loop, according to the IUPAC classification, which is a common feature of mesoporous materials. Type H1 hysteresis is associated with porous materials exhibiting pore geometry of cylindrical shape, along with pore size uniformity which is distinguished for all synthesized samples ( Figure 1A). The isotherms of Cr(x)/MOS (x = 2, 5, 8, and 11 Cr wt.%) Catalysts 2021, 11, 642 3 of 16 catalysts showed that the nitrogen molecules formed multilayer adsorption. Then, capillary condensation took place in the pores of Cr(x)/MOS. As the relative pressure increases, the mesoporous nature of the MOS sample was not disturbed by chromium impregnation. Figure 1B exhibits the distribution of pore size computed by using the BJH method. All Cr(x)/MOS (x = 2, 5, 8, and 11 Cr wt.%) catalysts displayed a consistently narrowing pore size distribution that peaked at 3.5 nm. According to textural properties (Table 1), both BET-surface area and total pore volume of the Cr(x)/MOS samples were reduced slightly when compared to the MOS support. This means that impregnation of MOS with Cr species caused further filling of the MOS pores with chromium oxide species.
sented in Table 1. The physisorption isotherms display IV type profile with an H1 hysteresis loop, according to the IUPAC classification, which is a common feature of mesoporous materials. Type H1 hysteresis is associated with porous materials exhibiting pore geometry of cylindrical shape, along with pore size uniformity which is distinguished for all synthesized samples ( Figure 1A). The isotherms of Cr(x)/MOS (x = 2, 5, 8, and 11 Cr wt.%) catalysts showed that the nitrogen molecules formed multilayer adsorption. Then, capillary condensation took place in the pores of Cr(x)/MOS. As the relative pressure increases, the mesoporous nature of the MOS sample was not disturbed by chromium impregnation. Figure 1B exhibits the distribution of pore size computed by using the BJH method. All Cr(x)/MOS (x = 2, 5, 8, and 11 Cr wt.%) catalysts displayed a consistently narrowing pore size distribution that peaked at 3.5 nm. According to textural properties (Table 1), both BET-surface area and total pore volume of the Cr(x)/MOS samples were reduced slightly when compared to the MOS support. This means that impregnation of MOS with Cr species caused further filling of the MOS pores with chromium oxide species.   [13]. The XRD patterns of the Cr(x)/MOS catalysts are illustrated in Figure 2. The diffraction peaks at 2θ = 24.5°, 33.6°, 36.2°, 41.5°, 50.2°, 54.9°, 63.4°, and 65.18° confirmed the presence of rhombohedral Cr2O3 crystals (JCPDS 00-006-0504) [9,13]. The intensities of the feature peaks of -Cr2O3 in all prepared samples increased with increasing chromium content from 2 to 11 wt.%. The small peak intensity, as in Cr(2)/MOS, and their broadness in   [9,13]. The intensities of the feature peaks of α-Cr 2 O 3 in all prepared samples increased with increasing chromium content from 2 to 11 wt.%. The small peak intensity, as in Cr(2)/MOS, and their broadness in Cr(5)/MOS and Cr(8)/MOS samples suggested a smaller size of Cr 2 O 3 crystals in these catalysts. In contrast, the Cr(11)/MOS catalyst showed higher peak intensities that could indicate the agglomeration or formation of large Cr 2 O 3 particles. Generally, α-Cr 2 O 3 crystals are detected over silica support at quite low Cr loading in comparison to other support systems (i.e., ZrO 2 and Al 2 O 3 ) [11]. The low content of hydroxyl functionality within the surface of silica motivates the formation of Cr 2 O 3 clusters, rather than a well-dispersed phase [11]. However, silica having a high surface area is essenti al in order to achieve a high dispersion of Cr species.
Catalysts 2021, 11, 642 4 of 16 systems (i.e., ZrO2 and Al2O3) [11]. The low content of hydroxyl surface of silica motivates the formation of Cr2O3 clusters, rathe phase [11]. However, silica having a high surface area is essenti high dispersion of Cr species. In order to establish more details on the surface topography and to assess the dispersion of the Cr species over Cr(x)/MOS cat ing, and EDX elemental mapping were obtained on MOS, Cr(2 Cr(11)/MOS catalysts; the images are presented in Figure 3. TE (Figure 3a*) show the formation of the mesoporous organo-silica 2 wt.% of Cr (Figure 3b*), the Cr oxides had rod and cubic shape in the range of 15-35 nm with good distribution onto the mesop trix. Increasing the Cr content to 8 wt.% (Figure 3c*) resulted in th oxide nanoparticles with growth of their sizes to 50-100 nm. Th the Cr oxide nanoparticles onto the organo-silica matrix was qui increasing the loading content of Cr oxide nanoparticles to 11 w the formation of a mixture of rod and cubic nanoparticles with s and poor distribution character onto the mesoporous organo-silic mapping also was used to investigate more about the state of di the mesoporous organo-silica matrix. It could be clearly observed well-dispersed on the surface of the mesoporous organo-silica s catalysts (Figure 3a   X-ray photoelectron measurement was employed to analyze the surface chemistry and to measure the concentration of each Cr species on the synthesized samples. The XPS spectra of the Cr(x)/MOS (x = 2, 5, 8 and 11 wt.% Cr) samples are presented in Figure 4A,B. In order to find the ratios of various oxidation states of Cr species, the Cr2p spectra were deconvoluted and the results are given in Table 2. According to the XPS survey spectrum of the Cr(8)/MOS catalyst ( Figure 4A), Cr, O, Si and C elements are present on the surface of Cr(x)/MOS catalysts. Their peaks are located at 576 (Cr 2p), 529.6(O1s), 284.6(C1s), 153(Si2s) and 103.4(Si2p) electron volts. Figure 4B displays the finely scanned XPS spectra of Cr2p of the formed catalysts. It can be observed that two intensive peaks were detected in the Cr 2p3/2 spectrum for all prepared samples; one at around ~577 eV, whereas the other was at ~579 eV, which can be correlated to Cr 3+ and Cr 6+ , respectively [26][27][28]. According the reported literature, the Cr species with high oxidation state are the main components responsible for the higher performance of Cr-based catalytic systems during the dehydrogenation of light alkanes [2,29,30]. Wang et al. suggested that the surface Cr 3+ species and Cr 6+ /Cr 3+ ratio is quite important in the ethane dehydrogenation [11], whereas Ge and his team found that the species with high oxidation states (Cr 5+ /Cr 6+ ) are crucial for this reaction [31]. XPS peaks of Cr2p3/2 and Cr2p1/2 were further deconvoluted into two more peaks by using a Gaussian-Lorentzian-Voigt fitting method, considering the spinorbit splitting of 9.3 eV and 2:1 height ratio. Based on the previous literature reports, the peaks at ~579 and ~589 eV are normally associated with the Cr 6+ ions, while energies at 577, and 587 eV are ascribed to the Cr 3+ [5,12,32,33]. It was observed that both Cr 6+ and Cr 3+ had existed on the surface of all prepared samples, but with changes in their Cr 6+ /Cr 3+ X-ray photoelectron measurement was employed to analyze the surface chemistry and to measure the concentration of each Cr species on the synthesized samples. The XPS spectra of the Cr(x)/MOS (x = 2, 5, 8 and 11 wt.% Cr) samples are presented in Figure 4A,B. In order to find the ratios of various oxidation states of Cr species, the Cr2p spectra were deconvoluted and the results are given in Table 2. According to the XPS survey spectrum of the Cr(8)/MOS catalyst ( Figure 4A), Cr, O, Si and C elements are present on the surface of Cr(x)/MOS catalysts. Their peaks are located at 576 (Cr 2p), 529.6(O1s), 284.6(C1s), 153(Si2s) and 103.4(Si2p) electron volts. Figure 4B displays the finely scanned XPS spectra of Cr2p of the formed catalysts. It can be observed that two intensive peaks were detected in the Cr 2p 3/2 spectrum for all prepared samples; one at around~577 eV, whereas the other was at~579 eV, which can be correlated to Cr 3+ and Cr 6+ , respectively [26][27][28]. According the reported literature, the Cr species with high oxidation state are the main components responsible for the higher performance of Cr-based catalytic systems during the dehydrogenation of light alkanes [2,29,30]. Wang et al. suggested that the surface Cr 3+ species and Cr 6+ /Cr 3+ ratio is quite important in the ethane dehydrogenation [11], whereas Ge and his team found that the species with high oxidation states (Cr 5+ /Cr 6+ ) are crucial for this reaction [31]. XPS peaks of Cr2p 3/2 and Cr2p 1/2 were further deconvoluted into two more peaks by using a Gaussian-Lorentzian-Voigt fitting method, considering the spin-orbit splitting of 9.3 eV and 2:1 height ratio. Based on the previous literature reports, the peaks at~579 and~589 eV are normally associated with the Cr 6+ ions, while energies at 577, and 587 eV are ascribed to the Cr 3+ [5,12,32,33]. It was observed that both Cr 6+ and Cr 3+ had existed on the surface of all prepared samples, but with changes in their Cr 6+ /Cr 3+ ratio. Table 2 summarizes the ratios. According to the quantitative data (Table 2), the Cr 6+ /Cr 3+ ratio increased with the increasing Cr content up to 8 wt.% Cr, but with further a Cr increase to 11 wt.%, the ratio dropped. The Cr(8)/MOS catalyst showed the highest Cr 6+ /Cr 3+ ratio of~0.66. The dominance of Cr 6+ at the surface of the optimum catalyst proposes a superior catalytic conversion toward ODH of C 2 H 6 with CO 2 .
a Cr increase to 11 wt.%, the ratio dropped. The Cr(8)/MOS catalyst showed the highest Cr 6+ /Cr 3+ ratio of ~0.66. The dominance of Cr 6+ at the surface of the optimum catalyst proposes a superior catalytic conversion toward ODH of C2H6 with CO2.    The presence of Cr of different oxidation states was also illustrated with UV-Vis DR measurements, and the spectra are presented in Figure 5A. In all spectra, two main absorption peaks at 270 and 370 nm are detected. These two peaks are associated with charge transfer of O 2− → Cr 6+ within chromate species with a tetrahedral structure [34][35][36]. An additional shoulder band is also observed at around 415 nm, which is attributed to dichromate or poly-chromates on the catalysts surface [26,37]. Contrastingly, the peaks at 470 and 600 nm are assigned to d-d transition of Cr 3+ species within the octahedral structure [5,11,26,[38][39][40]. It can be observed that the intensity of Cr 6+ bands increased with increasing chromium loading up to 8 wt.%, and the Cr(8)/MOS catalyst had the highest Cr 6+ bands and the lowest Cr 3+ bands among all the prepared samples. Further increasing the chromium loading resulted in reducing the intensity of Cr 6+ bands, as shown in Cr(11)/MOS catalyst, and increasing the Cr 3+ intensities as results of Cr 2 O 3 phase formation. Fourier-transform infrared spectroscopy measurements of Cr(x)/MOS catalysts were conducted in the 680-4000 cm −1 range, and spectra are illustrated in Figure 5B. Silica presence in the prepared samples was confirmed by the existence of 810 and 1090 cm −1 absorption bands that are assigned to symmetric vibrations of Si-O-Si bonding in the samples. Disappearance of chromium absorption bands at 905 cm −1 was due to overlapping with the SiO 2 vibration band. The absorption band at about 1636 cm −1 is assigned to the adsorbed water [13]. The peak observed at 2360 cm −1 can be related to CO 2 which is adsorbed from the air [41,42]. It can be seen that there is no noticeable difference for the synthesized samples with various Cr content, because similar FTIR bands were detected. The presence of Cr of different oxidation states was also illustrated with UV-Vis DR measurements, and the spectra are presented in Figure 5A. In all spectra, two main absorption peaks at 270 and 370 nm are detected. These two peaks are associated with charge transfer of O 2− → Cr 6+ within chromate species with a tetrahedral structure [34][35][36]. An additional shoulder band is also observed at around 415 nm, which is attributed to dichromate or poly-chromates on the catalysts surface [26,37]. Contrastingly, the peaks at 470 and 600 nm are assigned to d-d transition of Cr 3+ species within the octahedral structure [5,11,26,[38][39][40]. It can be observed that the intensity of Cr 6+ bands increased with increasing chromium loading up to 8 wt.%, and the Cr(8)/MOS catalyst had the highest Cr 6+ bands and the lowest Cr 3+ bands among all the prepared samples. Further increasing the chromium loading resulted in reducing the intensity of Cr 6+ bands, as shown in Cr(11)/MOS catalyst, and increasing the Cr 3+ intensities as results of Cr2O3 phase formation. Fourier-transform infrared spectroscopy measurements of Cr(x)/MOS catalysts were conducted in the 680-4000 cm −1 range, and spectra are illustrated in Figure 5B. Silica presence in the prepared samples was confirmed by the existence of 810 and 1090 cm −1 absorption bands that are assigned to symmetric vibrations of Si-O-Si bonding in the samples. Disappearance of chromium absorption bands at 905 cm −1 was due to overlapping with the SiO2 vibration band. The absorption band at about 1636 cm −1 is assigned to the adsorbed water [13]. The peak observed at 2360 cm −1 can be related to CO2 which is adsorbed from the air [41,42]. It can be seen that there is no noticeable difference for the synthesized samples with various Cr content, because similar FTIR bands were detected.

Catalytic Performance of Cr(x)/MOS Catalysts
The catalytic activity for the formed Cr(x)/MOS samples was tested for oxidative CO2 ethane dehydrogenation at various catalytic temperatures, and the results are displayed in Figure 6. It can be noticed that both the conversion of ethane and the yield of ethylene rapidly increased with catalytic temperature due to the endothermic character of the ODH reaction. Conversely, the selectivity of ethylene dropped slightly with catalytic temperature, suggesting that hydrocracking reactions are present at high catalytic temperatures. Moreover, the experimental results obviously showed that the Cr loading is a key element in the catalytic performance of Cr(x)/MOS catalysts. The ethane conversion as well as the

Catalytic Performance of Cr(x)/MOS Catalysts
The catalytic activity for the formed Cr(x)/MOS samples was tested for oxidative CO 2 ethane dehydrogenation at various catalytic temperatures, and the results are displayed in Figure 6. It can be noticed that both the conversion of ethane and the yield of ethylene rapidly increased with catalytic temperature due to the endothermic character of the ODH reaction. Conversely, the selectivity of ethylene dropped slightly with catalytic temperature, suggesting that hydrocracking reactions are present at high catalytic temperatures. Moreover, the experimental results obviously showed that the Cr loading is a key element in the catalytic performance of Cr(x)/MOS catalysts. The ethane conversion as well as the ethylene yield increased significantly with increasing the chromium content of Cr(x)/MOS up to 8 wt.% Cr, and then gradually decreased with further increases in chromium content to the Cr(11)/MOS catalyst. However, this drop in activity at high Cr loading is mainly caused by the formation of less active chromium oxide crystals. The XRD, UV-Vis DRS of Cr(11)/MOS catalyst showed that the crystalline α-Cr 2 O 3 is dominant in this sample. In contrast, the Cr(8)/MOS catalyst showed the highest catalytic activity for the CO 2 -based ODH of ethane over the tested range of temperatures. The high activity of this catalyst could be related to superior chromium species distribution with high concentrations of reducible Cr 6+ on the surface of the Cr(8)/MOS sample. It has been reported that the high concentration of reducible Cr 6+ species is significant for the dehydrogenation reaction [15,40].  The SEM and XPS measurements clearly show that the Cr species were highly dis persed and Cr 6+ species predominated on the prepared Cr(8)/MOS catalyst. In addition the XPS results illustrated that the superior number of Cr 6+ species and subsequently the highest Cr 6+ /Cr 3+ ratio were recorded for the Cr(8)/MOS sample, which was reflected in its activity. The catalyst displayed an ethane conversion of 50.4% at 700 °C after one hour on the reaction stream and an ethylene yield of 45.4%. Table 3 summarizes the performance of some Cr-supported catalytic systems tested in the ethane dehydrogenation with CO2 including Cr(8)/MOS prepared for this study. Although reaction conditions were diverse Cr/MOS exhibited comparable ethane conversion and higher activity than some catalysts listed in the table, which is partly attributed to reaction conditions or the number of used catalysts. The results show that Cr/MOS is a promising active catalyst for the ODH o ethane.  The SEM and XPS measurements clearly show that the Cr species were highly dispersed and Cr 6+ species predominated on the prepared Cr(8)/MOS catalyst. In addition, the XPS results illustrated that the superior number of Cr 6+ species and subsequently the highest Cr 6+ /Cr 3+ ratio were recorded for the Cr(8)/MOS sample, which was reflected in its activity. The catalyst displayed an ethane conversion of 50.4% at 700 • C after one hour on the reaction stream and an ethylene yield of 45.4%. Table 3 summarizes the performance of some Cr-supported catalytic systems tested in the ethane dehydrogenation with CO 2 , including Cr(8)/MOS prepared for this study. Although reaction conditions were diverse, Cr/MOS exhibited comparable ethane conversion and higher activity than some catalysts listed in the table, which is partly attributed to reaction conditions or the number of used catalysts. The results show that Cr/MOS is a promising active catalyst for the ODH of ethane. In addition to catalytic temperature and chromium loading effects, stability of the prepared catalysts was also investigated at 700 • C for 10 h, and the results are shown in Figure 7. For all samples, the conversion of ethane and the yield of ethylene decreased slowly over catalytic time, proposing a slight de-activation of the tested catalysts. Unlike our previously [3,12,46] investigated catalytic systems, deactivation of the Cr(x)/MOS catalytic system declined approximately 22% after 10 h of on-stream operation. For instance, using large-pore mesoporous silica as a support for the chromium-based catalytic system led to the same catalytic activity (50.5% and 91.1% conversion of ethane and selectivity of ethylene, respectively), but with 39% declination in the catalytic activity for the same reaction conditions [43]. Additionally, the results of this work are comparable to those other researcher groups, indicating its importance. Shi et al., for example, tested Cr(5) /SBA-15 for ethane dehydrogenation and found that the ethane conversation dropped from 46.3 to 23.6% after reacting for 5 h [8]. In addition to coke formation, the catalyst deactivation took place basically due to the reduction of high valence states of CrOx species, whereas the numbers of re-oxidized Cr 3+ species were reduced with the passage of reaction time while the non-redox agglomerated Cr sites were increased. However, enhancement of the stability of Cr(x)/MOS catalysts could partly be attributed to the presence of organic components on the wall pore which may resist the agglomeration of Cr sites and inhibit catalyst sintering. In addition to catalytic temperature and chromium loading effects, stability of the prepared catalysts was also investigated at 700 °C for 10 h, and the results are shown in Figure 7. For all samples, the conversion of ethane and the yield of ethylene decreased slowly over catalytic time, proposing a slight de-activation of the tested catalysts. Unlike our previously [3,12,46] investigated catalytic systems, deactivation of the Cr(x)/MOS catalytic system declined approximately 22% after 10 h of on-stream operation. For instance, using large-pore mesoporous silica as a support for the chromium-based catalytic system led to the same catalytic activity (50.5% and 91.1% conversion of ethane and selectivity of ethylene, respectively), but with 39% declination in the catalytic activity for the same reaction conditions [43]. Additionally, the results of this work are comparable to those other researcher groups, indicating its importance. Shi et al., for example, tested Cr(5) /SBA-15 for ethane dehydrogenation and found that the ethane conversation dropped from 46.3 to 23.6% after reacting for 5 h [8]. In addition to coke formation, the catalyst deactivation took place basically due to the reduction of high valence states of CrOx species, whereas the numbers of re-oxidized Cr 3+ species were reduced with the passage of reaction time while the non-redox agglomerated Cr sites were increased. However, enhancement of the stability of Cr(x)/MOS catalysts could partly be attributed to the presence of organic components on the wall pore which may resist the agglomeration of Cr sites and inhibit catalyst sintering. CO2-based oxidative dehydrogenation of ethane over the Cr(8)/MOS catalyst was also studied at various gas hourly space velocities (GHSV), and the results are presented in Figure 8. The GHSV was altered by changing the reactant flow rate while maintaining Therefore, slight deactivation of the Cr(x)/MOS catalytic system happened mostly because of the reduction of high-valence Cr 6+ of CrOx species along with coke formation. However, for better understanding of the reasons of deactivation after the reaction, characterizations of spent catalyst were compared with the fresh catalyst and the results are included as a supplementary file. Even after 10 h of on-stream operation, Cr(8)/MOS showed high catalytic activity, with 40.81% and 38.37% for the conversion of ethane and yield of ethylene, respectively. CO 2 -based oxidative dehydrogenation of ethane over the Cr(8)/MOS catalyst was also studied at various gas hourly space velocities (GHSV), and the results are presented in Figure 8. The GHSV was altered by changing the reactant flow rate while maintaining the same reactant ratio. From the results, the conversion of ethane as well as yield of ethylene decreased, while ethylene selectivity's increased by increasing the GHSV. These results were expected because increasing the space velocity will reduce the reactants' residence time inside the catalytic system, which leads to decreases in ethane conversion. In order to clarify the role of carbon dioxide in the dehydrogenation of ethane, the catalytic reaction was conducted in the presence and absence of CO 2 over the optimum catalyst (Cr(8)/MOS) at various temperatures, and the results are presented in Figure 9. the same reactant ratio. From the results, the conversion of ethane as well as yield of ethylene decreased, while ethylene selectivity's increased by increasing the GHSV. These results were expected because increasing the space velocity will reduce the reactants' residence time inside the catalytic system, which leads to decreases in ethane conversion. In order to clarify the role of carbon dioxide in the dehydrogenation of ethane, the catalytic reaction was conducted in the presence and absence of CO2 over the optimum catalyst (Cr(8)/MOS) at various temperatures, and the results are presented in Figure 9. It can be observed that the catalytic performance of the Cr(8)/MOS sample increased with reaction temperature, regardless of the presence or absence of CO2 in the reaction. Moreover, the catalytic performance of Cr(8)/MOS in the presence of CO2 was clearly superior than that in the absence of it, revealing the enhancement effects of carbon dioxide for ethane dehydrogenation. Furthermore, ethylene selectivity was slightly improved in the presence of CO2 as an oxidation agent. In the presence of carbon dioxide, ethylene was simultaneously formed either by dehydrogenation or oxidative dehydrogenation reactions, and a high conversion of ethane and yield of ethylene could be obtained, while the dehydrogenation of ethane without of CO2 was thermodynamically limited [11,47]. Reaction mechanisms of ethane dehydrogenation with CO2 over Cr-based catalysts follow the Mars-van Krevelen redox-type mechanism. This mechanism has been proposed for chromium [14,16,[48][49][50], vanadium [51,52], manganese [53], and iron [54] oxide-based catalysts. In our catalytic system, the mechanism suggests that ethylene is simultaneously produced by the dehydrogenation and oxidative dehydrogenation of ethane [9,29,33,43,55]. According to the mechanism, oxidative dehydrogenation of ethane in the presence of CO2 follows the following steps:  Ethane adsorbs on Cr-species active site and/or acidic site of support;  Adsorbed ethane reacts with lattice oxygen atoms of CrO3 to produce both ethylene and water, and Cr 3+ , as a result of Cr 6+ reduction; 3C2H6 + 2CrO3⟷3C2H4 + Cr2O3 + 3H2O  Re-oxidation of Cr3+ by surface oxygen species formed by the dissociation of CO2 Cr2O3 + 3CO2⟷3CO +2CrO3 In addition to the above reactions, the following reactions occurred:  Dehydrogenation of ethane C2H6⟷C2H4 + H2  Reverse water-gas shift (RWGS) reaction, which shifted ethane dehydrogenation towards increased ethylene production H2 + CO2⟷CO + H2O Another possible reaction is:  Hydrocracking of ethane to methane C2H6+H2⟷CH4 + H2 However, carbon dioxide could contribute either directly, by supplying the lattice oxygen in the oxidative dehydrogenation reaction, or indirectly, by removing the produced hydrogen from the dehydrogenation reaction [9]. On the other hand, the catalyst stability could be enhanced when the dehydrogenation reaction was carried out in the presence of CO2, where it assists by removing the deposited carbon on the catalyst surface according the following equation [56]: Eventually, the catalytic performance of the Cr/MOS catalyst in the CO2 atmosphere was clearly higher than that in the absence of it, suggesting the stimulating role of CO2 for the oxidative dehydrogenation of ethane in the presence of CO2. These findings are consistent with previous studies of light alkane oxidative dehydrogenation over Cr-based catalysts [5,33,45].
Effects of the CO2/C2H6 ratio on C2H6 dehydrogenation over the most active catalyst at various reaction temperatures were investigated, and the results are shown in Figure  10. It can be seen that, for all temperatures, both ethane conversion and ethylene yield increased with increasing CO2/C2H6 ratio until it attained its peak at ratio equal to five, after which it was almost constant with further increases in the CO2/C2H6 ratio.  It can be observed that the catalytic performance of the Cr(8)/MOS sample increased with reaction temperature, regardless of the presence or absence of CO 2 in the reaction. Moreover, the catalytic performance of Cr(8)/MOS in the presence of CO 2 was clearly superior than that in the absence of it, revealing the enhancement effects of carbon dioxide for ethane dehydrogenation. Furthermore, ethylene selectivity was slightly improved in the presence of CO 2 as an oxidation agent. In the presence of carbon dioxide, ethylene was simultaneously formed either by dehydrogenation or oxidative dehydrogenation reactions, and a high conversion of ethane and yield of ethylene could be obtained, while the dehydrogenation of ethane without of CO 2 was thermodynamically limited [11,47]. Reaction mechanisms of ethane dehydrogenation with CO 2 over Cr-based catalysts follow the Mars-van Krevelen redox-type mechanism. This mechanism has been proposed for chromium [14,16,[48][49][50], vanadium [51,52], manganese [53], and iron [54] oxide-based catalysts. In our catalytic system, the mechanism suggests that ethylene is simultaneously produced by the dehydrogenation and oxidative dehydrogenation of ethane [9,29,33,43,55]. According to the mechanism, oxidative dehydrogenation of ethane in the presence of CO 2 follows the following steps: However, carbon dioxide could contribute either directly, by supplying the lattice oxygen in the oxidative dehydrogenation reaction, or indirectly, by removing the produced hydrogen from the dehydrogenation reaction [9]. On the other hand, the catalyst stability could be enhanced when the dehydrogenation reaction was carried out in the presence of CO 2 , where it assists by removing the deposited carbon on the catalyst surface according the following equation [56]: Eventually, the catalytic performance of the Cr/MOS catalyst in the CO 2 atmosphere was clearly higher than that in the absence of it, suggesting the stimulating role of CO 2 for the oxidative dehydrogenation of ethane in the presence of CO 2 . These findings are consistent with previous studies of light alkane oxidative dehydrogenation over Cr-based catalysts [5,33,45].
Effects of the CO 2 /C 2 H 6 ratio on C 2 H 6 dehydrogenation over the most active catalyst at various reaction temperatures were investigated, and the results are shown in Figure 10. It can be seen that, for all temperatures, both ethane conversion and ethylene yield increased with increasing CO 2 /C 2 H 6 ratio until it attained its peak at ratio equal to five, after which it was almost constant with further increases in the CO 2 /C 2 H 6 ratio.

Catalyst Preparation
Mesoporous organo-silica (MOS) was prepared by using BTEB and CTAC as the or gano-silica source and surfactant, respectively. In a typical procedure, 4.40 ml o CH3(CH2)15N(Cl)(CH3)3, 52.5 ml of H2O, and 4 ml of NH4OH were combined and stirred for 10 min, in which a homogeneous solution was formed. After that, 5 ml of C6H4 (S (OC2H5)3)2 was added dropwise under vigorous stirring for 60 minutes. Then, the formed precipitate was filtered, washed, and dried overnight. The dried powder was then heat treated at 550 °C for 12 h.
In the next step, a series of Cr(x)/MOS catalysts were prepared by the incipient wet ness impregnation approach where the prepared MOS support was treated with an aque ous solution having the specific amount of Cr precursor. The concentration of chromium nitrate in solution was tuned so as to obtain 2, 5, 8, and 11 wt.% of total Cr content (C total) in the final catalysts. The prepared samples were dried, and then were calcined a 650 °C for 12 h in air. The catalysts are denoted as Cr(x)/MOS, where x stands for th nominal Cr total given in wt.% of Cr.

Catalyst Characterization
All synthesized Cr(x)/MOS samples were characterized using the same instrument

Catalyst Preparation
Mesoporous organo-silica (MOS) was prepared by using BTEB and CTAC as the organo-silica source and surfactant, respectively. In a typical procedure, 4.40 ml of CH 3 (CH 2 ) 15 N(Cl)(CH 3 ) 3 , 52.5 ml of H 2 O, and 4 ml of NH 4 OH were combined and stirred for 10 min, in which a homogeneous solution was formed. After that, 5 ml of C 6 H 4 (Si (OC 2 H 5 ) 3 ) 2 was added dropwise under vigorous stirring for 60 minutes. Then, the formed precipitate was filtered, washed, and dried overnight. The dried powder was then heat-treated at 550 • C for 12 h.
In the next step, a series of Cr(x)/MOS catalysts were prepared by the incipient wetness impregnation approach where the prepared MOS support was treated with an aqueous solution having the specific amount of Cr precursor. The concentration of chromium nitrate in solution was tuned so as to obtain 2, 5, 8, and 11 wt.% of total Cr content (Cr total) in the final catalysts. The prepared samples were dried, and then were calcined at 650 • C for 12 h in air. The catalysts are denoted as Cr(x)/MOS, where x stands for the nominal Cr total given in wt.% of Cr.

Catalyst Testing
Oxidative dehydrogenation ODH reactions were performed in a stainless-steel packed catalyst bed reactor (internal diameter, 6 mm) at 600-700 • C and one atmosphere. Samples of 300 mg of Cr(x)/MOS catalysts were packed in the reactor, and glass wool was put at both ends of the catalyst bed. Prior to starting the reaction, the catalyst samples were pre-treated at 600 • C in an air atmosphere for 60 minutes before switching to the reactant mixture. During the test, the feed mixture ratio was maintained at 1:5:4 for ethane, carbon dioxide and nitrogen gases, respectively. Additionally, the total flowrate was kept at 75 mL/min. Carbon dioxide was replaced with N 2 when the experiments were implemented in the absence of CO 2 . The ODH reaction was performed within a 600-700 • C temperature range. The tested samples were maintained at the reaction conditions for 20 min before starting the analysis. Both the reactants and the reaction products were analyzed by on-line Agilent 6890 N gas chromatography (Agilent 6890N, Agilent, Santa Clara, CA, USA) which was connected to the reactor outlet. The GC was equipped with TCD and FID detectors, and using hayesep Q, molecular sieve 5 Å, and gas pro-columns.

Conclusions
CO 2 -based ethane oxidative dehydrogenation was studied over supported chromium oxide on mesoporous organo-silica (MOS). The results show that the prepared Cr(x)/MOS catalysts possessed promising catalytic performance in the dehydrogenation of ethane, with a less than 23% drop of its activity after 600 min. A highly active and stable catalyst Cr(8)/MOS was obtained, with an conversion of ethane~50.9% and selectivity of ethylenẽ 90.1%. TEM and elemental mapping showed a gradual increment of the size of CrOx species, along with their poor distribution with increasing the Cr content. EDX analysis revealed CrOx content close to the proposed added values during the impregnation step. XPS measurements revealed that Cr 6+ /Cr 3+ ratio increased with increasing the Cr content up to 8 wt.% Cr, but with a further Cr increase to 11 wt.%, the ratio dropped. The high activity of this catalyst could be related to the superior chromium species distribution with high concentration of reducible Cr 6+ on the surface of the Cr(8)/MOS sample. The deactivation of the catalyst was much improved as compared to previous reports, which can be correlated to enhancement of the redox Cr species stability due to the high surface area and stable structure supports, which we developed by using MOS as a support for our catalytic system. Data Availability Statement: The raw/processed data required to reproduce these findings cannot be shared at this time as the data also forms part of an ongoing study.