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Article

Nickel Oxide Nanoparticles on KIT-6: An Efficient Catalyst in Methane Combustion

by
Xiuhui Huang
1,*,
Wenkai Yang
1,
Zeqiu Li
1,
Qin Lou
1,
Ying Tian
2 and
Junfeng Li
3,*
1
School of Energy and Power Engineering, University of Shanghai for Science and Technology, Shanghai 200093, China
2
School of Optical Electrical and Computer Engineering, University of Shanghai for Science and Technology, Shanghai 200093, China
3
Shanghai MCC20 Construction Co., Ltd., Shanghai 201999, China
*
Authors to whom correspondence should be addressed.
Processes 2023, 11(4), 1004; https://doi.org/10.3390/pr11041004
Submission received: 21 February 2023 / Revised: 16 March 2023 / Accepted: 22 March 2023 / Published: 26 March 2023
(This article belongs to the Special Issue 10th Anniversary of Processes: Women's Special Issue Series)
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Abstract

:
KIT-6 silica with well-ordered three–dimensional (3D) mesopores has been synthesized as a support for nickel-based catalysts. Transmission Electron Microscopy (TEM) and low-angle X-ray Diffraction (XRD) analysis are used to ensure that the ordered 3D mesostructure is stable after NiO incorporation. In this study, the catalytic activities of the NiO/KIT-6 samples are investigated. Additionally, the results show that a 10 wt% NiO/KIT-6 catalyst exhibits high catalytic performance in methane combustion, with T10, T50 and T90 being only 386 °C, 456 °C and 507 °C, respectively. Hydrogen Temperature Programmed Reduction (H2-TPR) studies have shown that the interaction between NiO and KIT-6 in the 10 wt% NiO/KIT-6 catalyst is weak. Methane Temperature programmed Surface Reaction (CH4-TPSR) results show that the surface oxygen of the NiO/KIT-6 catalyst allows it to exhibit a high catalytic performance. NiO/KIT-6 catalysts exhibit superior activities to SBA-15, MCF and SiO2 support catalysts because KIT-6 has a higher surface area and ordered 3D mesopore connectivity, which is favorable for better NiO dispersion and peculiar diffusion for reactant and products. Furthermore, the used catalyst maintained an ordered mesostructure and reduction property.

1. Introduction

Methane is widely available, obtained from natural gas, coal mines and biogas. It is recognized as a cleaner hydrogen-rich energy compared to others because of its high hydrogen-to-carbon ratio and high calorific value. When methane is utilized, it can be directly discharged into the atmosphere, wasting resources and causing environmental pollution, and it has a low utilization efficiency and releases polluting gases when directly burned [1,2]. In recent years, the catalytic combustion of methane has increasingly captured the interest of researchers and industry professionals, as it offers notable advantages, such as high efficiency, safety and minimal emissions of pollutants, such as NOx and CO [3,4]. The synthesis of catalysts with high activity, high resistance to sulfur poisoning, and high hydrothermal stability is crucial to the research on the catalytic combustion of methane, as methane is one of the most inert hydrocarbons. It has been found that noble metal-based catalysts (Pt, Pd, Rh, etc.) [5,6], especially supported palladium catalysts, show excellent activity during methane combustion. However, their development and industrial application are limited due to their high cost and rapid deactivation at high temperatures, as well as the fact they can cause poisoning. Non-noble metal-based catalysts, including perovskite-type catalysts, hexa-aluminate catalysts and transition metal oxide catalysts, etc., have garnered significant interest owing to their low price and high thermal stability, but their poor low-temperature activity limited their development [7,8,9]. Transition metal-based catalysts have been widely investigated in methane combustion because of their good stability and low price [10,11]. As an efficient transition metal-based catalyst, there are some reports on the use of nickel-based catalysts in the combustion of methane. R.M. [12] studied the performance of an NiO/SiO2 foam catalyst in the methane reforming reaction, which showed good stability and activity, mainly due to its good porosity and pore structure. Notably, at a reaction temperature of 600 °C, the methane conversion rate reached 42%. Huang [13] found that the catalytic performance of NiO/CeO2 was significantly enhanced in CH4 combustion, particularly when the NiO loading reached 10 wt%, and Chai R [14] found that the NiO/CeO2 catalyst also showed high stability and good water resistance in CH4 combustion. Likewise, A.S. Al-Fatesh [15] investigated the impact of an SiO2 support on catalyst performance and discovered that as the amount of silica decreased, the catalyst demonstrated an improved CH4 conversion rate and stability in methane catalytic decomposition. Lu Y [16] found that a suitable support was crucial in creating a highly effective nickel-based catalyst. In comparison to the Ni/MgO (111) catalyst, the Ce/Zr co-doped catalyst exhibited superior catalytic activity and stability. Differently, A.S. Al-Fatesh [17] investigated the effects of three different preparation methods on catalytic activity. It was found that the impregnation method can produce enough active sites on the catalyst surface to exhibit higher activity. Additionally, the addition of nickel can increase the methane conversion rate and H2 yield up to 10%. Besides the above, factors such as the calcination temperature and catalyst surface area also affect the performance of the catalyst. Anis Hamza Fakeeha [18] investigated the effect of combustion temperature on the activity and stability of catalysts. Through experiments, it was found that Co/Al2O3-ZrO2 catalysts exhibit metal–support interactions when calcined at temperatures ranging from 550 °C to 800 °C, which helps them resist sintering. At higher temperatures (800 °C), Ni/Co is uniformly distributed on the support, leading to improved coking resistance. In general, elevating the calcination temperature proves to be advantageous for enhancing catalyst performance. Anis Fakeeha [19] found that the Ni-Al-H-600 catalyst had the highest methane conversion rate and hydrogen production at 650 °C due to its larger surface area and pore volume, reaching 90% and 72%, respectively. Moreover, after being subjected to a reaction for seven hours at this temperature, it exhibited the highest activity and stability.
In other studies of the effect of nickel-based catalyst with different catalyst supports, mesoporous silica (such as MCM-41, SBA-15, KIT-6, MCF, etc.) has been widely used as a catalyst support because of its specific pore structure, high surface area, and thermal stability, and its ability to improve catalyst activity [20,21], especially SBA-15, which has ordered two-dimensional (2D) hexagonal channels and showed good catalytic effect in several reactions [22,23]. For example, Miao et al. [22] found that nickel-based SBA-15 catalysts have good catalytic stability and there is a stronger interaction between the nickel and support, as shown in the results of the CO methanation reaction. SBA-15 is also used as an effective support in methane combustion. For example, Murthy [24] and others improved the stability of the catalyst by fixing Pd on SBA-15 and uniformly dispersing it on the channel; this porous structure can inhibit Pd flow to prevent sintering. Additionally, the catalyst shows good thermal stability and catalytic activity in methane combustion.
KIT-6 has ordered 3D mesoporous channels, which makes it superior to catalysts with low-order channels (SBA-15) in mass transfer characteristics. Based on this advantage, KIT-6-based catalysts are superior to SBA-15-based catalysts in terms of reactant and product transport and catalyst activity [25]. In the research on KIT-6 in CO methanation, Lv Y [21] found that catalysts with high Ni contents showed good activity in CO methanation, owing to the unique 3D structure and large surface area of KIT-6. Congming Tang [26] characterized Ni/KIT-6 catalysts with different compositions using XRD and BET. The results indicated that the surface area and crystallinity of metal Ni in the catalysts were influenced by the reduction temperature. The prepared catalysts demonstrated impressive CH4 and CO2 conversion rates of 69.0% and 39.4%, respectively, while also exhibiting good stability. Rita Mahfouz [27] investigated the effect of Ce addition on the mesoporous structure. Through characterization, it was found that Ce promotion led to significant destruction of the porous structure, while catalysts without promotion exhibited better catalytic performances.
The above research shows that most researchers focus on the study of KIT-6 in related fields, such as CO methanation and methane dry reforming. However, there is little research on the use of KIT-6 catalysts in methane catalytic combustion. Therefore, this article examines the characteristics of catalysts from the perspective of methane catalytic combustion to provide a reference and guidance for future research.
Herein, we have synthesized a series of mesoporous silica KIT-6 support NiO samples, which have ordered mesoporous structures similar to pure KIT-6 and NiO nanoparticles embedded into the pore channels. It was found that these NiO/KIT-6 catalysts have high activities for methane combustion due to their high surface area and distinctive structure.

2. Materials and Methods

2.1. Synthesis

KIT-6 was prepared as described previously [28]. In typical synthesis, 6 g of P123 is dissolved in 217 g of distilled water and 11.8 g of concentrated HCl (37 wt%), followed by the addition of 6 g of 1-butanol and continuous stirring at 35 °C after stirring for 1 h. Then, 12.9 g of TEOS is slowly added at 35 °C and stirring is carried out at 35 °C for 24 h. After this, the solution in its final form is moved into Teflon bottles and is maintained at 100 °C for 24 h. After hydrothermal treatment, filtering, washing with deionized water until neutral, and drying at room temperature are carried out. Then, the solution is calcined for 5 h under flowing air at 550 °C to remove the organic template.
The NiO/KIT-6 sample was prepared from Ni(NO3)2 aqueous solution via the impregnation approach. The NiO content varies between 1 wt% and 15 wt%. All samples were dried at 100 °C and then calcined for 4 h in air at 450 °C to acquire the final products.
For comparison, SBA-15, MCF and SiO2 were synthesized and used as the supports, following a previous report [28,29,30,31]. Then, 10 wt% NiO/SBA-15, 10 wt% NiO/MCF and 10 wt% NiO/SiO2 samples were prepared via an impregnation approach and using 10 wt% NiO/KIT-6.

2.2. Characterization

The XRD pattern was recorded on a Bruker D8 Focus diffractometer with a wavelength of 1.541 Å (40 kV, 40 mA, canning step = 0.02o). The N2 adsorption–desorption isotherms were measured at −196 °C using the Surface Area as well as Pore Size Analyzer of NOVA 4200e. Prior to measurement, the samples were outgassed for 4 h under vacuum at 180 °C. The BET surface area of samples was calculated using Brunauer–Emmett–Teller approach. The pore size distribution was calculated using the Barrett–Joyner–Halanda approach. The overall pore volume (Vp) was estimated to be 0.985 (P/P0). The Fourier Transform Infrared (FT-IR) absorption spectrum was documented on the Nicolet NEXUS 670 FT-IR spectrometer, with thirty-two scans at 4 cm−1 effective resolution. After grinding the sample with KBr, the sample was analyzed on a thin wafer. H2-TPR was used in the TCD detector. The sample (50 mg) is placed in a quartz tube reactor. Using 5 vol% H2/N2 mixture gas of 40 mL·min−1, heated at room temperature to 800 °C at 10 °C·min−1. The CH4-TPSR reaction was carried out in quartz micro-reactor. A total of 200 mg of catalysts was pretreated in 500 °C for 30 min in 50 mL·min−1 20 vol% O2/He mixture gas. Following cooling, the sample at room temperature, 50 mL·min−1 1vol% CH4/He were heated from room temperature to 800 °C at 10 °C·min−1. A quadrupole mass spectrometer (INFICON Transpecter 2) was used to analyze the exit gas. At m/z = 15, 18, 28, 32 and 44, the signals of CH4, H2O, CO, O2, CO2 were recorded, respectively.

2.3. Tests of Catalytic Activity

In this study, several kinds of NiO/KIT-6 catalysts in methane combustion were investigated in quartz tube reactor (Ø 6 mm) at atmospheric pressure. Reagent gas mixture containing 1.0 vol% CH4 + 4.0 vol% O2 in Ar under the flow rate of 50 mL·min−1 entered a catalyst (200 mg, 20–40 mesh) bed, resulting in a weight hourly space velocity (WHSV) of 15,000 mL·g−1·h−1. Online analysis of reactants and products was carried out using a TCD gas chromatograph (GC). The activities of tcatalyst were measured at a programmed temperature of 200 °C to 700 °C when heated at a rate of 5 °C·min−1. T10, T50 and T90 represent 10%, 50% and 90%, respectively, of the catalyst activity. Additionally, the experimental setup of the reactor used is shown in Figure 1.

3. Results and Discussion

Figure 2a indicates XRD patterns at low angles for various NiO/KIT-6 catalysts. The XRD pattern of 1% NiO/KIT-6 identifies a sharp peak of intense intensity at 2θ = 1.04 as well as a hump in (220) planes, very similar to pure KIT-6 [28], indicating that the main well-ordered mesopore remains after NiO loading. The diffraction peak of (220) plane becomes weaker with increasing loading amount of NiO, which reveals that some mesoporous structures are destroyed when a mass of NiO nanoparticles are incorporated into the pore tunnel. Figure 2b shows wide-angle XRD patterns for NiO/KIT-6 catalysts. All the samples indicate diffraction peaks of NiO in the cubic phase (JCPDS file No. 65-2901). Moreover, NiO has a wide diffraction peak, indicating that NiO particles are highly dispersed on KIT 6. With the increase in loading amounts, NiO nanoparticles began to aggregate and NiO in the cubic phase exhibits sharp diffraction peaks.
In Figure 3, the TEM images of KIT-6 and 10% NiO/KIT-6 are shown. As shown in Figure 3a, for KIT-6 a well-ordered cubic array of mesopores was observed, with a pore size of approximately 8 nm. After supporting NiO, the cubic 3D uniform channel array of mesopores can still be seen clearly. The NiO particles were assembled in mesoporous channels, which showed irregular shapes, which was suitable for the porous structure of supports.
Methane combustion took place on NiO/KIT-6 catalysts. Throughout the reaction, CH4 underwent complete oxidation to form CO2 and H2O. As indicated in Figure 4, the catalytic activity of KIT-6 could be enhanced significantly by adding NiO. In addition, the catalytic activity of the NiO/KIT-6 catalyst increases consistently when the NiO loading amount reaches 10 wt%, while 10 wt% NiO/KIT-6 samples show high activity. T10, T50 and T90 are only 386 °C, 456 °C and 507 °C, respectively, higher than others [32,33]. When the NiO loading amount reaches 15 wt%, the catalytic activity shows little change, because NiO nanoparticles destroy much of the the pore tunnel, resulting in the aggregation of NiO nanoparticles.
The textural properties and catalytic activities of all the samples are shown in Table 1. We estimated NiO particle size in the catalyst according to the diffraction peaks of cubic phase NiO using the Scherrer equation. The result shows that the particle size of NiO changes a little when the loading amounts increase, which is consistent with the wide diffraction peaks of NiO and means the NiO particles are dispersed well on KIT-6 without clumping. It is shown that there is only a tiny change in pore size, indicating that the pore structure is preserved even after using support NiO, which is in agreement with previous results. However, the BET surface areas and pore volume of NiO/KIT-6 samples decrease gradually with an increase in the NiO loading amount, due to the destruction of partial mesopores after NiO incorporation.
Figure 5 shows the H2-TPR profiles of different NiO/KIT-6 catalysts. Two hydrogen consumption peaks can be observed for all NiO/KIT-6 catalysts, named α1 and α2. The α1 peak, centered at ~355 °C, is attributed to the reduction of NiO species of low interaction with KIT-6 [34,35,36]. Additionally, the high temperature reduction peak (α2 peak) is due to the reduction of NiO, which strongly interacted with KIT-6 to form a few surface layers made up of silicate-type compounds [34,35,36]. The area of the α2 peak does not change obviously with the increase in the loading amount from 0.01 to 0.15, revealing that only a small number of NiO nanoparticles have strong interaction with the support. Therefore, the interaction between KIT-6 and NiO is weak, similar to the SBA-15 support catalyst [36], and the strong interaction is not a key factor for the improvement of activity.
To investigate the reason behind the high performance of NiO/KIT-6 catalysts, CH4-TPSR was utilized and the findings are depicted in Figure 6. It is evident that without any oxygen introduced into the feed, methane oxidation can only occur through interaction with surface oxygen and bulk oxygen (at high temperatures) [37]. As shown in Figure 6, two CO2 generation peaks can be observed over both samples, named β1 and β2, which could correspond to the oxidation of methane by surface oxygen and bulk oxygen, respectively. The area of the β1 peak for 10 wt% NiO/KIT-6 is similar to that of pure NiO, but the NiO amount on NiO/KIT-6 is only 10 percent that of the pure NiO sample. Therefore, the surface oxygen of NiO/KIT-6 shows higher activity due to the high dispersion of NiO on KIT-6. Differing from pure NiO, the bulk oxygen of NiO/KIT-6 can be reduced by CH4 in a narrow temperature region.
The effect of the support is also investigated. The observed activities of the 10 wt% NiO/KIT-6, 10 wt% NiO/SBA-15, 10 wt% NiO/MCF and 10 wt% NiO/SiO2 catalysts are shown in Figure 7. It was found that the catalytic activities of methane combustion with NiO-based catalysts decrease in the following order: NiO/KIT-6 > NiO/ SBA-15 > NiO/MCF ≈ NiO/SiO2. The BET surface areas of KIT-6, SBA-15, MCF and SiO2 are 708, 520, 562 and 387 m2·g−1, respectively. Therefore, the remarkable enhancement in activity of NiO/KIT-6 compared to NiO/SBA-15 and NiO/SiO2 can be attributed to its 3D pore connectivity, as well as its large surface area and pore volume [38]. Though MCF also has 3D mesopores, the large pore size of MCF (15/30 nm) cannot restrict the aggregation of NiO nanoparticles effectively when NiO nanoparticles are incorporated into the pore channels.
After reaction, the used 10 wt% NiO/KIT-6 catalyst was collected for analysis. As shown in Figure 8a, the used catalyst has a sharp intense peak and a hump, as does the fresh catalyst, which reveals that the ordered mesoporous structure is retained even after reaction. Figure 8b shows that the wide-angle XRD patterns of the used catalyst are similar to those of the fresh one, without any growth of NiO particle size. There is a decrease in the surface area of the used catalyst, as it is exhibited in Table 1, due to the destruction of partial mesopores. Figure 3c shows the TEM image of the used catalyst. It can be seen clearly that the ordered mesopores remain and there is no obvious difference in pore size between the fresh catalyst and the used one. Additionally, the sizes of the NiO nanoparticles in the used catalyst are remarkably similar to those of the fresh one. The deactivation of nickel-based catalysts primarily occurs due to the formation of carbon deposits, which can take shape as carbon nanotubes during methane reforming, decomposition or partial oxidation [39,40,41]. However, no carbon nanotubes and carbon nanoparticles were observed in the TEM images, which reveals that there is no carbon deposit formation on the surface. The H2-TPR results (not shown here) show that the reduction peaks (peak temperature and peak area) of the used catalyst are nearly the same as the fresh one, which means the used catalyst may still maintain a high reduction property.
FT-IR spectroscopy was used to investigate the surface group change of the used catalyst. As shown in Figure 9a, both samples have the characteristic band of the KIT-6 framework (bands at ~1085 and 799 cm−1), corresponding to the T–O asymmetric stretching vibrations and T–O symmetric stretching vibrations, respectively [42]. The CO32− group (bands at ~1350 and 1520 cm−1), which can combine with Ni2+ ions to generate carbonates and then result in deactivation, was not observed in the FT-IR spectrum of the used catalyst. Therefore, there is no significant change to the NiO/KIT-6 catalyst during the combustion of methane. However, as displayed in Table 1, there is a decrease in the surface area of the catalyst, owing to the destruction of partial mesopores in the reaction. So, future work should focus on the enhancement of the thermal stability of the NiO/KIT-6 catalyst.
TG–DTA curves of the fresh and used 10% NiO/KIT-6 catalysts are presented in Figure 9b. It can be seen that, below 200 °C, the weight loss values of both samples are about 3%, attributed to removal of crystalline water, in agreement with the FT-IR spectra results. At above 200 °C, the tiny weight loss of the used catalyst is similar to the fresh one, which reveals that there is no carbon deposit formation on the surface, in agreement with the TEM results. Therefore, there is no obvious change in the NiO/KIT-6 catalyst during the combustion of methane.

4. Conclusions

In this paper, a series of NiO/KIT-6 catalysts were prepared for methane combustion, and the conclusions are as follows:
(1) The main well-ordered mesopore remains after NiO loading. However, some mesoporous structures are destroyed when a mass of NiO nanoparticles is incorporated.
(2) The characterization results show that the 10 wt% NiO/KIT-6 catalyst exhibits a high BET surface area and ordered 3D mesopores, and the NiO/KIT-6 catalyst has a high reduction property and catalytic performance in methane combustion, with T10, T50 and T90 being only 386 °C, 456 °C and 507 °C, respectively.
(3) NiO particle size changes a little as the loading amounts increase, and NiO particles are dispersed well on KIT-6. However, with the further increase in the load, the destruction of mesopores will lead to a decrease in the BET surface area and pore volume.
(4) Only a small amount NiO nanoparticles strongly interact with the support. Therefore, the interaction between KIT-6 and NiO is weak, so the strong interaction is not a key factor for the improvement of activity. Hence, the high performance of the NiO/KIT-6 catalyst may be due to the high dispersion of NiO and the good mass transfer property.
(5) There is no carbon deposit formation and no obvious difference in pore size between the fresh catalyst and the used one, and it still maintains a high activity.
In summary, the NiO/KIT-6 catalyst is an efficient methane combustion catalyst.
In future research, we will focus on the catalytic mechanism of CH4 combustion over NiO/KIT-6, improve the activity and stability of the catalyst by doping Ce or other elements and surface modification, and conduct additional tests including EDX and long term stability tests and so on.

Author Contributions

X.H.: Formal analysis; Investigation; Methodology; Writing—review and editing; Writing—original draft; W.Y.: Investigation; Software; Writing—original draft; Writing—review and editing; Z.L.: Investigation; Writing—original draft; Writing—review and editing; Q.L. and Y.T.: Investigation; Software; Writing—review and editing; J.L.: Conceptualization; Data curation; Writing—original draft; Writing—review and editing. All authors have read and agreed to the published version of the manuscript.

Funding

This research was funded by National Natural Science Foundation of China [No.62003215], National Natural Science Foundation of China [No.61903251] and the Shanghai Pujiang Program [No. 22PJD047].

Data Availability Statement

The data presented in this study are available on request from the corresponding author.

Conflicts of Interest

The authors declare no conflict of interest.

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Figure 1. Catalyst methane catalytic combustion activity evaluation device diagram. 1. Ar; 2. O2; 3. CH4/CO; 4. Reduction Valve; 5. Stop Valve; 6. Mass Flowmeter; 7. Gas Mixing Tank; 8. Tube Heating Furnace; 9. Quartz Reactor; 10. Thermocouple; 11. Temperature Controller; 12. Digital Indicator; 13. Gas Chromatograph.
Figure 1. Catalyst methane catalytic combustion activity evaluation device diagram. 1. Ar; 2. O2; 3. CH4/CO; 4. Reduction Valve; 5. Stop Valve; 6. Mass Flowmeter; 7. Gas Mixing Tank; 8. Tube Heating Furnace; 9. Quartz Reactor; 10. Thermocouple; 11. Temperature Controller; 12. Digital Indicator; 13. Gas Chromatograph.
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Figure 2. (a) Low-angle XRD patterns and (b) Wide-angle XRD patterns of NiO/KIT-6 catalysts with various NiO loading amounts (*NiO: NiO diffraction peak).
Figure 2. (a) Low-angle XRD patterns and (b) Wide-angle XRD patterns of NiO/KIT-6 catalysts with various NiO loading amounts (*NiO: NiO diffraction peak).
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Figure 3. TEM images of (a) KIT-6, (b) fresh 10 wt% NiO/KIT-6 and (c) used 10 wt% NiO/KIT-6.
Figure 3. TEM images of (a) KIT-6, (b) fresh 10 wt% NiO/KIT-6 and (c) used 10 wt% NiO/KIT-6.
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Figure 4. Light-off curves of catalytic combustion of methane using NiO/KIT-6 catalysts.
Figure 4. Light-off curves of catalytic combustion of methane using NiO/KIT-6 catalysts.
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Figure 5. H2-TPR profiles of KIT-6-supported NiO catalysts.
Figure 5. H2-TPR profiles of KIT-6-supported NiO catalysts.
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Figure 6. MS signals of CO2 (m/z = 44) in the CH4-TPSR of NiO and 10 wt% NiO/ KIT-6 catalysts.
Figure 6. MS signals of CO2 (m/z = 44) in the CH4-TPSR of NiO and 10 wt% NiO/ KIT-6 catalysts.
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Figure 7. Methane combustion with 10 wt% NiO/KIT-6, 10 wt% NiO/SBA-15, 10 wt% NiO/MCF and 10 wt% NiO/SiO2 catalysts.
Figure 7. Methane combustion with 10 wt% NiO/KIT-6, 10 wt% NiO/SBA-15, 10 wt% NiO/MCF and 10 wt% NiO/SiO2 catalysts.
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Figure 8. (a) Low-angle XRD patterns of fresh and used 10% NiO/KIT-6 catalyst; (b) wide-angle XRD patterns of fresh and used 10% NiO/KIT-6 catalyst (∆NiO: NiO diffraction peak).
Figure 8. (a) Low-angle XRD patterns of fresh and used 10% NiO/KIT-6 catalyst; (b) wide-angle XRD patterns of fresh and used 10% NiO/KIT-6 catalyst (∆NiO: NiO diffraction peak).
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Figure 9. (a) FT-IR spectra of fresh and used 10 wt% NiO/KIT-6 catalysts and (b) TG curves of fresh and used 10% NiO/KIT-6 catalysts.
Figure 9. (a) FT-IR spectra of fresh and used 10 wt% NiO/KIT-6 catalysts and (b) TG curves of fresh and used 10% NiO/KIT-6 catalysts.
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Table
Table 1. Textural properties and catalytic activities of KIT-6 and KIT-6 support NiO samples.
Table 1. Textural properties and catalytic activities of KIT-6 and KIT-6 support NiO samples.
SamplesNiO CrystalliteBET Surface
Area (m2·g−1)		Average Pore Diameter (nm)Pore Volume
(cm3·g−1)		Catalytic Activity in CH4 Combustion
Size (nm) aT10 (°C)T50 (°C)T90 (°C)
KIT-6–7088.20.94–––
1 wt% NiO/ KIT-67.636718.10.91420523611
3 wt% NiO/ KIT-67.396387.90.87432515577
5 wt% NiO/ KIT-67.606197.80.83396496554
7 wt% NiO/ KIT-67.415467.60.72411485535
10 wt% NiO/KIT-67.654687.50.60386456507
15 wt% NiO/KIT-68.074077.50.51386457510
10 wt% NiO/KIT-6
(used) b		8.563577.50.48–––
a Crystallite sizes were calculated from the diffraction peaks of cubic phase NiO using the Scherrer equation. b 10 wt% NiO/KIT-6 catalyst was collected after reaction.
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Huang, X.; Yang, W.; Li, Z.; Lou, Q.; Tian, Y.; Li, J. Nickel Oxide Nanoparticles on KIT-6: An Efficient Catalyst in Methane Combustion. Processes 2023, 11, 1004. https://doi.org/10.3390/pr11041004

AMA Style

Huang X, Yang W, Li Z, Lou Q, Tian Y, Li J. Nickel Oxide Nanoparticles on KIT-6: An Efficient Catalyst in Methane Combustion. Processes. 2023; 11(4):1004. https://doi.org/10.3390/pr11041004

Chicago/Turabian Style

Huang, Xiuhui, Wenkai Yang, Zeqiu Li, Qin Lou, Ying Tian, and Junfeng Li. 2023. "Nickel Oxide Nanoparticles on KIT-6: An Efficient Catalyst in Methane Combustion" Processes 11, no. 4: 1004. https://doi.org/10.3390/pr11041004

APA Style

Huang, X., Yang, W., Li, Z., Lou, Q., Tian, Y., & Li, J. (2023). Nickel Oxide Nanoparticles on KIT-6: An Efficient Catalyst in Methane Combustion. Processes, 11(4), 1004. https://doi.org/10.3390/pr11041004

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