Synthesis and Application of Cerium-Incorporated SBA-16 Supported Ni-Based Oxygen Carrier in Cyclic Chemical Looping Steam Methane Reforming

Abstract

Hydrogen, as a clean energy carrier, could be produced aided by cyclic oxidation-reduction of oxygen carriers (OCs) in contact with carbonaceous fuel in chemical looping steam methane reforming (CL-SMR) process. In this study, the cerium was incorporated into the SBA-16 support structure to synthesize the Ni/Ce-SBA-16 OC. The supports were synthesized using hydrothermal method followed by impregnation of Ni and characterized via low and wide angle X-ray diffraction (XRD), Brunauer-Emmett-Teller (BET), scanning electron microscopy (SEM), coupled with energy dispersive X-ray (EDX) spectroscopy, and transmission electron micrograph (TEM) techniques. In addition, the effect of various Si/Ce molar ratios (20–60) in the support structure, Ni loading (10–30 wt %), reaction temperature (500–750 °C), and life time of optimal oxygen carrier over 16 cycles were investigated. The results of wide angle XRD and SEM revealed that the incorporation of CeO₂ in the channels of SBA-16 caused the formation of nickel metallic particles with smaller size and prevents the coke formation. The results showed that OC with 15 wt % Ni and Si/Ce molar ratio of 40 (15Ni/Ce-SBA-16(40)) has the best performance when compared with other OCs in terms of catalytic activity and structural properties. The methane conversion of about 99.7% was achieved at 700 °C using 15Ni/Ce-SBA-16(40) OC. We anticipate that the strategy can be extended to investigate a variety of novel modified mesoporous silica as the supporting material for the Ni based OCs.

1. Introduction

Hydrogen is an energy carrier that is used in various chemical and petrochemical industries, such as methanol and ammonia production, petroleum refineries and fuel cells [1,2,3,4]. Since combustion of fossil fuels releases different greenhouse gases, such as CO₂, NO_x, SO_x, and CH₄ that causes global warming effect. Hydrogen can replace these fuels [5,6,7,8].

Reforming of hydrocarbons is a well-known process for the production of hydrogen and carbon monoxide [9]. One of the reforming reactions that is conventionally used for this purpose is the partial oxidation of hydrocarbon. In this process, the oxygen source could be supplied from either air or pure oxygen. In the first oxygen source, the product is diluted with nitrogen, whereas in the second one, an oxygen plant is required [10,11]. In order to reduce the cost of reforming, chemical looping reforming (CLR) process was suggested by Mattisson and Lyngfelt [12]. One of the most important hydrocarbon sources that can be used in reforming process is methane. It has received much attention due to its low cost and high availability [13]. As indicated in Figure 1, in chemical looping steam methane reforming (CL-SMR) process, methane is converted to synthesis gas in contact with oxygen carriers in the fuel reactor while the reduced oxygen carriers is reoxidized in the air reactor [14,15].

The principle reactions that occur in the fuel reactor of CL-SMR process are as follows [16,17,18]:

$$s{\mathrm{CH}}_4+{\mathrm{Me}}_x{\mathrm{O}}_y\to {\mathrm{Me}}_x{\mathrm{O}}_{y-s}+s\mathrm{CO}+2{\mathrm{H}}_2$$

(1)

$$\mathrm{CO}+{\mathrm{H}}_2\mathrm{O}\leftrightarrow {\mathrm{H}}_2+{\mathrm{CO}}_2$$

(2)

In the air reactor, the oxygen carriers (OC) is converted to its initial oxidized form through the following reaction:

$$2{\mathrm{Me}}_x{\mathrm{O}}_{y-s} + s{\mathrm{O}}_2\to {\mathrm{Me}}_x{\mathrm{O}}_y$$

(3)

The reason that Equation (1) in reduced catalyst is not followed by partial oxidation of CO in oxidized catalyst is that CO → CO₂ reaction is an exothermic reaction with ∆H = −283 kJ/mol that occurs in low temperatures. As the reaction temperature of reforming process is high, the reverse reaction of partial oxidation of CO is occurred.

The choice of oxygen carrier plays an important role in CLR process. The OC must have enough oxygen transport capacity, high selectivity towards synthesis gas, high stable performance for successive cycles, and low tendency toward coke formation [19,20]. The OC is comprised of a porous support and redox active sites.

Some metal oxides including NiO, CuO, Fe₂O₃, CoO, and MnO₂ are considered as effective oxygen carriers to promote CLR procedure. It was reported that Ni-based OCs revealed high oxygen transfer rate and capacity. In addition, the cyclic chemical looping results showed the high selectivity toward H₂ and CO using Ni OC [21]. Diego et al. [22] tested NiO-γAl₂O₃ oxygen carrier in the CLR using methane as fuel and determined the effect of different operating variables, such as the temperature of fuel reactor in the range of 800–900 °C, H₂O/CH₄ molar ratio (0–0.5), and solid circulation rate. Their results showed that OC conversion was increased at higher temperatures and with increasing H₂O/CH₄ molar ratio, H₂, and CO₂ conversions were increased, whereas CO conversion was decreased. Liu and his coworkers [23] prepared Ni grafted SBA-15 and MCM-41 catalysts for CO₂ reforming of methane. The obtained results showed that 5 wt % Ni/SBA-15 catalyst has the highest catalytic activity and long-time stability.

Nevertheless, the dispersed Ni active sites are quickly deactivated because of coke formation and/or sintering of the support and metallic phases in CL-SMR process [24].

Mesoporous materials could be applied as the support of OC to improve Ni active sites dispersion and prevent the aggregation of Ni nanoparticles. They include a range of large surface area, with diameters in the range of 2–50 nm. One kind of porous based materials are SBA-type silica groups. The SBA-16 mesoporous silica is known as one of the novel structure of this family. Thick pore walls, high surface area, prominent thermal and hydrothermal stability, three-dimensional (3D) and cubic structure make SBA-16 be an outstanding catalyst or support [25]. However, as pure SBA-16 suffers from lack of sufficient acidity and coke deposition, the modification seems to be needed.

A suggested solution is the modification of support structure with an appropriate promoter such as CeO₂, La₂O₃, CaO, Al₂O₃, and MgO [10,26,27,28,29,30]. Lindo et al. [26] assessed Ni catalysts supported on Al-SBA-15 mesoporous materials for ethanol steam reforming. They found that the incorporation of Al³⁺ cations into the frame work of SBA-15 leads to strong interaction between NiO active sites and Al-SBA-15 carrier. Qian et al. [27] have proved that the presence of La in Ni/SBA-15 in methane dry reforming significantly improved catalytic activity and stability. The CO₂ adsorption capacity was increased by addition of La into the framework of SBA-15.

The redox properties of CeO₂ (${\mathrm{Ce}}^{4+}\leftrightarrow {\mathrm{Ce}}^{3+}$) improve the mobility of surface oxygen that lowers carbon deposition on active sites. Also, the metal-support interaction and the dispersion of metal particles are increased in the presence of CeO₂ [31]. Wang et al. [28] tested Ce-SBA-15 supported nickel OC synthesized by direct hydrothermal method in methane reforming with CO₂. The results showed that the cerium incorporated in the framework of SBA-15 leads to formation of nickel particles with smaller size, which prevents the carbon deposition. Li and her coworkers [32] examined CeO₂-promoted Ni/SBA-15 catalysts in ethanol steam reforming. The results revealed that the incorporated CeO₂ particles promote the homogeneous distribution of Ni and Ce in order to achieve large Ni/CeO₂ interface.

To the best of our knowledge, this is the first paper on the incorporation of cerium into the framework of SBA-16 and its application as the supporting material of Ni-based OC in CL-SMR process. The aim of this paper is to synthesize Ce-SBA-16 support by the hydrothermal method and to impregnate nickel on this modified support to have Ni-based OC. In addition, various characterizations were performed to investigate the surface and textural properties of the supports, used and fresh OC. Some parameters, such as Ni loading percentage, the effect of Si to Ce molar ratio in the support, reaction temperature, and life time of optimum OC over 16 cycles were studied.

2. Results and Discussion

2.1. Sample Characterization

Low angle XRD pattern of Ce-SBA-16(40) (Figure 2) shows a main peak at 2θ value of about 0.9° and a less peak at 2θ equal to 2.2°, respectively, corresponding to 110 and 211 Bragg’s reflections. These two peaks could be indexed to a mesoporous 3D cubic structure of SBA-16 with space group of 1m3m [33]. Previous authors synthesized various metal incorporated SBA-16 materials and characterized them with low angle XRD. They showed that the SBA-16 structure was preserved after incorporation of different loadings of metal into the structure of SBA-16 [34,35].

Figure 3 indicates a comparison between wide angle XRD patterns of unreacted 15Ni/Ce-SBA-16(40) and 15Ni/Ce-SBA-16(∞) OCs. According to Figure 3b, Ce is observed in the form of CeO₂ and CeNi₂ in modified supported OC. Also, in this figure, SiO₂ peaks are slightly shifted to right because of larger ionic radii of Ce⁴⁺ when compared with Si⁴⁺, which is proved the presence of Ce particles in the framework of SBA-16 [36]. As indicated in this figure, by the addition of cerium into the framework of SBA-16, NiO peaks (2θ = 37°, 43°, 63°, 76°, and 79°) became wider that indicates the presence of Ce caused fine nickel oxide particles on the surface of OC. This can be proved by debye sherrer equation. From this equation, the average NiO particle size was 8.8 nm for 15Ni/Ce-SBA-16(40) and 14.1 nm for 15Ni/Ce-SBA-16(∞) oxygen carriers. According to 01-083-2071 reference pattern code, Ni₂SiO₄ is observed at peaks of 2θ = 35°, 38°, 45°, and 51°.

In order to investigate the porous structure of catalysts, the N₂ adsorption/desorption isotherms of Ce-SBA-16(∞), Ce-SBA-16(20), Ce-SBA-16(40), Ce-SBA-16(60) supports, and 15Ni/Ce-SBA-16(40) OC are shown in Figure 4a. As can be seen in this figure, all of the prepared samples exhibit type-IV isotherms with a H₂ hysteresis loop characteristic of mesoporous oxygen carrier with cubic cage-like structure. For all the samples, the first hysteresis loop starts at P/P₀ = 0.4, demonstrating the presence of messoporous framework and the second hysteresis loop that starts at P/P₀ = 0.7 showing the mesoporosity of inter-particles. When compared with pure SBA-16, the inflection point of modified supports hysteresis shifts to higher values of the P/P₀. This shift reveals that Ce-metal oxide particles could be incorporated into the inner structure of SBA-16, which is in accordance with XRD results [37]. The impregnated sample (15Ni/Ce-SBA-16(40)) represents a very narrow hysteresis loop area with a low quality of type-IV N₂ adsorption/desorption isotherm, which may be caused by the coexistence of disordered mesoporous structure [38]. In addition, it seems to be related to the pore blockage due to Ni deposition on the pore gate. The pore size distribution of Ce-SBA-16(y) (20, 40, 60 and ∞) supports and fresh 15Ni/Ce-SBA-16(40), as obtained from Barret-Joyner-Halenda (BJH) method, are illustrated in Figure 4b. The Ce-SBA-16(20, 40) supports show a narrow and sharp peak, indicating that these materials possess uniform mesopore structure. Whereas, Ce-SBA-16(60) has a wide and less sharp peak with an average pore diameter centered at 3.49 nm. A much wider range of size distribution is obtained by impregnating nickel on the Ce-SBA-16(40) support revealing the existence of the pore blocking phenomena.

The structure characteristics of various mesoporous supports are presented in

Table 1. Structure characteristics of Ce-SBA-16(20, 40, 60, ∞) and fresh 15Ni/Ce-SBA-16(40) OC.

Sample	BET Surface Area (m2/g)	Pore Diameter (nm) b	Pore Volume (cm3/g) c
Ce-SBA-16(∞ a)	538.19	3.4	0.27
Ce-SBA-16(60)	700.55	3.41	0.28
Ce-SBA-16(40)	801.02	3.42	0.33
Ce-SBA-16(20)	540.47	3.38	0.23
15Ni/Ce-SBA-16(40)	207.15	4.57	0.25

^a molar ratio of Si/Ce in the synthesis gel. ^b BJH desorption average pore diameter. ^c BJH desorption pore volume.

. It can be observed that BET surface area of ordered Ce containing samples (Ce-SBA-16(20, 40, 60)) are larger than Ce-SBA-16(∞). This is because the radius of Ce⁴⁺ cation is larger than Si⁴⁺ so the length of Ce–O bond formed is longer than that of Si-O bond length. Substitution of Ce species for Si⁴⁺ leads to a significant expansion in the mesoporous structure. This confirms that Ce species were incorporated into the framework of silica, which is in good agreement with those that were obtained by wide angle XRD [36]. The surface area of Ce-SBA-16(y) supports tended to be increased with Si/Ce ratio from y = 60–40. Further increase in Ce content (Si/Ce ratio from 40 to 20) revealed negative effect on the surface area. The pore volume and average pore size follow the similar trend with the surface area. Among the supports, Ce-SBA-16(20) displays the lowest specific surface area, pore diameter, and pore volume, because the ordered mesoporous structure of Ce-SBA-16(20) was partially destroyed. It may be the result of partial blockage of SBA-16 pores which was occurred due to presence of the cerium ions on the silica wall or even by partial collapse of the mesoporous silica structure along with the incorporation of excessive cerium. It can be observed that among Ce modified OC supports, Ce-SBA-16(40) exhibits the highest surface area, pore diameter, and pore volume. After the impregnation of Ni on Ce-SBA-16(40) support, the specific surface area is decreased significantly. It seems to be due to the size of NiO particles, which are bigger than the pore size of the support. Thus, partial blockage of pores could be occurred [39]. This is in line with the results of pore size distribution curve indicated in Figure 4b.

For further observation of structural properties, TEM images of Ce-SBA-16(40) and 15Ni/Ce-SBA-16(40) are exhibited in Figure 5. The Ce-SBA-16(40) support represents uniform mesoporous cubic structure with 1m3m space group, which is in agreement with low angle XRD results. As indicated in Figure 5b, with the impregnation of nickel on Ce-SBA-16(40) support, NiO particles caused the loss of ordered mesopores.

The shape of nickel particles and surface morphology of the OCs could be seen in SEM images before and after CL-SMR process (Figure 6). This figure indicates that after reaction, cubic NiO particles transform into spherical particles. This is because these particles reused several times. With increasing Ce content up to 40, smaller NiO particles can be observed in both used and fresh OCs. This is the result of higher surface area of Ce-SBA-16(40) support when compared with Ce-SBA-16(20, 60) supports that leads to higher and better dispersion of NiO particles on the surface of supports, which is in accordance with the results of wide angle XRD. The average particle size of 15Ni/Ce-SBA-16(40) is about 75 nm, while it is 120 and 100 nm for 15Ni/Ce-SBA-16(20) and 15Ni/Ce-SBA-16(60) OCs, respectively. Figure 6a shows that after incorporation of Ce into the framework of SBA-16, the three-dimensional structure of SBA-16 is preserved, which is consistent with the results of low angle XRD.

To sum, the slight shift of the SiO₂ peaks in XRD figure and increase in specific surface area of modified oxygen carriers are the result of incorporation of Ce particles in the SBA-16 framework.

2.2. Effect od Si to Ce Molar Ratios on the Activity

The effect of cerium addition to the SBA-16 structure on the oxygen carrier performance is shown in Figure 7a,b. As can be seen in Figure 7a, the methane conversion was increased by raising temperature from 500 to 750 °C due to endothermic nature of steam methane reforming [40,41,42]. In addition, the oxygen transform rate of Ni-based oxygen carrier is improved at elevated temperatures. By raising Si/Ce molar ratio in the support structure from 20 to 60, it can be clearly observed that 20Ni/Ce-SBA-16(40) showed the highest activity, especially at lower reaction temperatures. For instance, by increasing temperature up to 650 °C, average methane conversion is increased from about 58.8 to 91.4 for 20Ni/Ce-SBA-16(40), while it is about 87.5 and 87.1 at 650 °C for 20Ni/Ce-SBA-16(60) and 20Ni/Ce-SBA-16(20), respectively. The average H₂ production yield exhibited that the sample with Si/Ce = 40 has better proficiency at all of the temperatures. In addition, hydrogen production yield is increased from 58.0 to 85.0%, with increasing the temperature from 500 to 750 °C for 20Ni/Ce-SBA-16(40) OC (Figure 7b).

2.3. Effect of Ni Loading Percentage on the Performance of xNi/Ce-SBA-16(40)

Figure 8a,b demonstrates the effect of Ni loading on the catalytic activity of xNi/Ce-SBA-16(40) (x = 10, 15, 20, 25, 30 wt %) oxygen carrier in different reaction temperatures. In both figures with increasing temperature, the catalytic performance is increased, and 15Ni/Ce-SBA-16(40) OC has the highest activity, especially in lower temperatures. The methane conversion and H₂ yield are 86.0% and 68.0% at 500 °C and are reached to 99.7% and 85.6% at 700 °C. Since methane conversion and H₂ yield do not change significantly at 750 °C, the optimum reaction temperature is 700 °C. By increasing the Ni content, the amount of active sites was increased. But, further amounts of Ni particles started to mobile on the OC surface and they became agglomerated in the calcination step. Therefore, the Ni amount should be justified.

Actually, by increasing the metal loading, active oxygen transfer sites is reduced, which is the result of particle agglomeration.

2.4. Time-on-Stream Behavior of Oxygen Carrier

In order to investigate the effect of cerium incorporated into the framework of SBA-16 on the life time of OCs, the prepared samples, including 15Ni/Ce-SBA-16(∞) and 15Ni/Ce-SBA-16(40), were investigated during 16 cycles under the reaction temperature of 700 °C and steam to methane ratio of 2. As shown in Figure 9a,b, methane conversion and average hydrogen yield increased through the first seven cycles, but after that, no further increment was observed for 15Ni/Ce-SBA-16(40) OC. The methane conversion increased from 86.6 to 99.5%. The reason is that, during first cycles, not all of the nickel particles burn into oxygen to form nickel oxides and by further reduction process, suitable oxidize phases were formed. But, for 15Ni/Ce-SBA-16(∞) OC, methane conversion and hydrogen yield first increase to reach 99.9% and 84.3%, respectively, during four cycles, and then they decrease through three next cycles, but after that, no further reduction was detected, as exhibited in Figure 9a,b, coke formation on the surface of OC causes this reduction of activity [41].

The structural change (BET surface area, pore volume, and pore size) of optimized oxygen carrier after 16 redox cycles is presented in

Table 2. Structure characteristics of the deactivated 15Ni/Ce-SBA-16(40) OC after 16 redox cycles.

Oxygen Carrier	BET Surface Area (m2/g)	Pore Diameter (nm)	Pore Volume (cm3/g)
15Ni/Ce-SBA-16(40)	112.01	3.98	0.12

. The BET surface area of 15Ni/Ce-SBA-16(40) decreased from 207.15 to 112.01 (m²/g). Actually, carbon deposited on the Oxygen carrier’s surface and reduced specific surface area in reduction step. Furthermore, pore blockage and sintering of OC occurred at 700 °C [10].

Figure 10 shows a comparison between wide angle XRD patterns of 15Ni/Ce-SBA-16(40) and 15Ni/SBA-16 OCs after 16 redox cycles. As can be seen, the intensity of amorphous carbon (2θ = 44°) in the 15Ni/Ce-SBA-16(40) is less than 15Ni/Ce-SBA-16(∞), indicating that the less coke deposited on the surface area of modified OC. According to 00-021-0771 reference pattern code, NiCO₃ is detected at 2θ = 43.5° and 52°. Ni₂SiO₄ is presented at 2θ = 35.5° and 76.5° (01-083-2071 reference pattern code).

The energy dispersive X-ray (EDX) carbon result of 15Ni/Ce-SBA-16(40) and 15Ni/Ce-SBA-16(∞) OCs after 16 redox cycles at 700 °C is presented in

Table 3. EDX of used 15Ni/Ce-SBA-16(40) and 15Ni/Ce-SBA-16(∞) OCs.

Oxygen Carrier	Carbon (wt %)
15Ni/Ce-SBA-16(40)	0.23
15Ni/Ce-SBA-16(∞)	3.06

. The results showed that by using cerium modified OC support, deposition of coke was reduced from 3.05 to 0.23 wt %.

3. Experimental Methods

3.1. Oxygen Carrier Preparation

To synthesize the Ni/Ce-SBA-16 OC, the first step was to prepare Ce-SBA-16 support using hydrothermal method. Different ratios of Si/Ce, including 20, 40, 60, and infinite where synthesized to investigate the effect of Ce-promoter in the structure of Ce-SBA-16 support. Then, Ni/Ce-SBA-16 OCs with 10, 15, 20, 25, and 30 wt % nickel were prepared by wetness impregnation method on the optimum support.

Ce-SBA-16 was prepared using F127, TEOS, n-butanol, and Ce(NO₃)₃·6H₂O as structure directing agent, silica source, Co-surfactant, and metal precursor. For this purpose, 1.15 g F127 (Sigma-Aldrich, St. Louis, MO, USA) was dissolved in HCl (Merck 37 wt %, Darmstadt, Germany) and deionized water under stirring at 40 °C. Then, 3.1 g n-butanol (Merck) was added to the previous solution with continuous stirring. After complete dissolution, about 7.00 g TEOS (Merck) and a solution of Ce(NO₃)₃·6H₂O (Merck) were added dropwise to the slurry to achieve different Si/Ce molar ratios and stirred for 120 min. The mixture was then transferred to a Teflon lined autoclave under moderate stirring at 40 °C for 24 h. Afterwards, it was aged at 100 °C for 48 h in an oven. Then, the solid product was filtered, washed several times with double distilled water and ethanol, and dried at 100 °C for one day. The obtained powder was calcined in air at 550 °C for 6 h with a heating step of 4 °C/min. The solid product was designated as Ce-SBA-16(y), where y is the molar ratio of Si/Ce.

Nickel was introduced into the Ce-SBA-16(y) support with the incipient wetness impregnation method. The solution of desired amounts of Ni(NO₃)₂·6H₂O (Merck) in 100 mL de-ionized water was added to the mixture dropwise at 40 °C. The impregnated solids were dried at 100 °C overnight and calcined at 700 °C for 3 h. The synthesized OCs were denoted as xNi/Ce-SBA-16(y), where x refers to Ni wt %.

3.2. Oxygen Carrier Characterization

The oxygen carriers and synthesized mesoporous supports were characterized with different methods. The low angle X-ray diffraction (XRD) was carried out with PANalytical (X’pert Pro, Eindhoven, The Netherlands) instrument operating at 40 Kv and 40 mA. The data in the low angle region (2θ = 0.71–10°) were recorded with a step size of 0.02°. The high angle XRD measurements were implemented by a powder diffractometer (Bruker D8 Advance, Karlsruhe, Germany) via Cu Kα radiation at 40 Kv and 40 mA. In high angle XRD, samples were run under a step scan mode in the angular 2θ range of 10–90°, with a step size rating of 0.05°/s. Transmission electron micrograph (TEM) images of samples were collected with a Zeiss-EM10C transmission electron microscope (Oberkochen, Germany), employing an accelerating voltage of 100 kV. The surface morphology of samples was studied by scanning electron microscopy (SEM). The SEM images were collected using a TESCAN vega3 equipped with an energy dispersive X-ray (EDX) spectroscopy. For measuring the specific surface area of OCs, Brunauer-Emmett-Teller (BET) method was used by nitrogen adsorption/desorption isotherms. About 0.08 g of the samples were degassed at 250 °C with nitrogen in an automated gas adsorption instrument (ASAP-2020, Micromeritics, Atlanta, GA, USA). The pore size distribution and cumulative pore volume were achieved by BJH method and desorption branches of adsorption isotherms, respectively.

3.3. Process Activity

The performance of synthesized oxygen carriers in CL-SMR process was evaluated at atmospheric pressure in a fixed bed reactor due to the operational limits. It is noteworthy to say that previous works also used a fixed bed reactor for chemical looping reforming process [15,43,44]. In this regard, the oxygen carriers were tested by reduction-oxidation (redox) multi-cycles of gas-solid reaction. The stainless steel reactor (diameter: 16 mm, height: 1000 mm) was inserted into a vertical furnace, as shown schematically in Figure 11. Typically, 1 g of freshly oxygen carrier was introduced into the reactor on a thin porous layer in the middle of it. The volumetric flow rate of the gaseous feed stream consisting CH₄ (99.99%), Ar (99.99%) was controlled using distinct MFCs to 48.1 and 87.4 mL/min. The steam was injected with an HPLC pump to an evaporator and then mixed with gaseous mixture prior to the reactor. The reduction section was performed at temperatures in the range of 500–750 °C, with an increment of 50 °C for 50 min. Oxidation section was performed before each reduction period for 30 min with the purpose of reoxidizing the oxygen carriers and burning the deposited carbon. In this section, O₂ (20 vol %) diluted with Ar was fed to the reactor with the flow rate of 44.0 mL/min. The oxidation and reduction periods were separated by 3 min purging of argon.

The effluent of the reactor was passed through a condenser and separator to liquefy the steam and to remove any solid particles. Then, the product and unreacted gases were analyzed by an online Bruker 450 gas chromatograph equipped with a thermal conductivity detector (TCD).

Methane conversion (${\mathrm{X}}_{{\mathrm{CH}}_4}$) and hydrogen production yield (${\mathrm{y}}_{{\mathrm{H}}_2}$) were calculated as follows:

$${\mathrm{X}}_{{\mathrm{CH}}_4}=\frac{{\left(F_{{\mathrm{CH}}_4}\right)}_{in}-{\left(F_{{\mathrm{CH}}_4}\right)}_{out}}{{\left(F_{{\mathrm{CH}}_4}\right)}_{in}} \times 100$$

(4)

$${\mathrm{y}}_{{\mathrm{H}}_2}=\frac{F_{{\mathrm{H}}_2}}{2 \times F_{{\mathrm{CH}}_4}} \times 100$$

(5)

where $F_{{\mathrm{H}}_2}$, $F_{{\mathrm{CH}}_4}$ represent the outlet molar flow rate of hydrogen and the inlet molar flow rate of methane, respectively.

4. Conclusions

A series of mesoporous cerium containing SBA-16 (Ce-SBA-16) were synthesized via direct hydrothermal method as the supporting material for Ni-based oxygen carrier in a CL-SMR process. The effect of Ni loading (10–30 wt %), various Si/Ce molar ratios (20–60) in the support, reaction temperature (500–750 °C), and life time of oxygen carrier over 16 redox cycles were successfully investigated. The characterization results showed that cerium was well incorporated into the silica framework of SBA-16 without provoking structure. The results of wide angle XRD and SEM revealed that the incorporation of CeO₂ in the channels of SBA-16 caused the formation of nickel metallic particles with smaller size. This leads to a better dispersion of NiO particles on the surface of supports. In addition, it prevents the formation of coke during the process that is in agreement with EDX and XRD results of used oxygen carriers. The xNi/Ce-SBA-16(y) with x and y value of 15 and 40, respectively, revealed the highest catalytic activity and long-term stability in the CL-SMR process. The reduction temperature showed a significant consequence on methane conversion in all of the prepared samples. The methane conversion over 15Ni/Ce-SBA-16(40) oxygen carrier increased from 86.0 to 99.7%, with temperature rising from 500–700 °C. The stability tests of 15Ni/Ce-SBA-16(∞) and 15Ni/Ce-SBA-16(40) showed that the incorporation of cerium could significantly improve the lifetime of oxygen carrier at high reduction temperatures.