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Lan, K., Qin, Z., Li, Z., Hu, R., Xu, X., He, W., and Li, J. (2020). "Syngas production by catalytic pyrolysis of rice straw over modified Ni-based catalyst," BioRes. 15(2), 2293-2309.


Ni-xLa/Al2O3-MgO-sawdust char catalysts were prepared by modifying the Ni/Al2O3 catalyst from two aspects of support and active components. The effect of Al2O3, MgO, sawdust char molar ratio, and La content of catalysts on syngas (H2 + CO) production in the catalytic pyrolysis of rice straw was investigated in a horizontal fixed-bed quartz tube reactor. Furthermore, the stability of catalysts with the optimum catalytic performance was tested and compared with that of the Ni/Al2O3 catalysts. X-ray diffraction, X-ray fluorescence, field emission scanning electron microscopy, energy disperse X-ray, and Brunauer-Emmett-Teller analyses were applied to understand the physiochemical properties of the supports and catalysts. The study revealed that the supports were composed of many irregular flaky particles and thus formed many pores. Moreover, the addition of La decreased the particle size of NiAl2O4 and increased the active metal surface of the Ni/Al2O3-MgO-sawdust catalysts. When the molar ratio of Al2O3, MgO, and sawdust char was 1:1:1 and the La content was 10 wt% (dry weight basis), the catalysts presented the highest syngas concentration of 78.9 vol% and the most stable performance during the catalytic pyrolysis process.

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Syngas Production by Catalytic Pyrolysis of Rice Straw over Modified Ni-based Catalyst

Kui Lan, Zhenhua Qin, Zeshan Li, Rui Hu, Xianzhou Xu, Weitao He, and Jianfen Li *

Ni-xLa/Al2O3-MgO-sawdust char catalysts were prepared by modifying the Ni/Al2O3 catalyst from two aspects of support and active components. The effect of Al2O3, MgO, sawdust char molar ratio, and La content of catalysts on syngas (H2 + CO) production in the catalytic pyrolysis of rice straw was investigated in a horizontal fixed-bed quartz tube reactor. Furthermore, the stability of catalysts with the optimum catalytic performance was tested and compared with that of the Ni/Al2O3 catalysts. X-ray diffraction, X-ray fluorescence, field emission scanning electron microscopy, energy disperse X-ray, and Brunauer-Emmett-Teller analyses were applied to understand the physiochemical properties of the supports and catalysts. The study revealed that the supports were composed of many irregular flaky particles and thus formed many pores. Moreover, the addition of La decreased the particle size of NiAl2O4 and increased the active metal surface of the Ni/Al2O3-MgO-sawdust catalysts. When the molar ratio of Al2O3, MgO, and sawdust char was 1:1:1 and the La content was 10 wt% (dry weight basis), the catalysts presented the highest syngas concentration of 78.9 vol% and the most stable performance during the catalytic pyrolysis process.

Keywords: Modified catalyst; Catalytic pyrolysis; Rice straw; Syngas

Contact information: School of Chemical and Environmental Engineering, Wuhan Polytechnic University, Wuhan 430023, China; *Corresponding author:


Biomass is a carbon neutral green energy that has great potential in reducing fossil fuel consumption and greenhouse gas emissions (Huang et al. 2016) because of its renewability, abundance, and low N/S pollution characteristics (Shen et al. 2013). Hence, the rational exploitation and utilization of biomass resources can effectively alleviate the pressure of fossil energy shortage and the problem of global warming (Chen et al. 2019). One of the aspects of biomass utilization is the production of syngas (H2+CO), which is an important gas mixture that can be used as a fuel in an internal combustion engine for power generation, as well as in a boiler for heat generation or a feedstock for Fischer-Tropsch synthesis (Demirbas 2009; Hu et al. 2016). Among various biomass resources utilization technologies, pyrolysis is considered one of the most potential thermochemical technologies in terms of the efficient and clean conversion of biomass into syngas (Dong et al. 2019). However, the presence of tar by-products in syngas hinders the large-scale commercial application of biomass pyrolysis technology (Wang et al. 2017; Yang et al. 2017). Biomass tar contains many harmful chemicals that can condense on the pipe wall and clog filters or downstream devices, leading to equipment failure (Beneroso et al. 2016). In addition, it wastes energy and can even endanger people’s health. Therefore, it is crucial to effectively remove the tar from the syngas of biomass pyrolysis.

At present, several technologies for removing the tar from the syngas have been examined, such as physical treatment (Paethanom et al. 2012), thermal pyrolysis (Fagbemi et al. 2001), plasma-assisted pyrolysis (Zhu et al. 2016), and catalytic pyrolysis (Artetxe et al. 2017). Among these methods, catalytic pyrolysis, which can degrade tar at 600 to 900 °C, is regarded as a cost-effective method because of its high reliability and fast reaction rate (Zhang et al. 2004; Li et al. 2014; Shen et al. 2018). Currently, a variety of catalysts such as olivine (Michel et al. 2013), dolomite (Yu et al. 2009), zeolites (Shao et al. 2018), noble metals (Furusawa and Tsutsumi 2005), non-nickel transition metals (Li et al. 2013), and nickel-based catalysts (He et al. 2009), have been heavily investigated in biomass catalytic pyrolysis. Noble metal catalysts have the dual characteristics of superior catalytic performance and high cost. Ni-based catalysts are widely used in tar removal from the syngas of biomass pyrolysis (Dong et al. 2016; Hu et al. 2016) due to their good catalytic activity/cost ratio (Zhang et al. 2018). However, it is worth noting that the combination of high temperature and pressure, hydrocarbons, and impurities creates a harsh environment for nickel-based catalysts. This makes the usage of nickel-based catalysts challenging due to deactivation from coke deposition and sintering (Melo and Morlanés 2005; Sehested 2006; Li et al. 2009). Hence, it is vital to develop high activity catalysts with strong capacity to resist carbon deposition and sintering.

Various metal additives, such as transition metals and alkaline earth metals, can be added to the Ni-based catalysts. According to Świerczyński et al. (2007), during the steam reforming of toluene, the presence of Ni-Fe alloy and (Ni, Mg) O solid solution restrained the formation of carbon deposition on Ni/olivine catalysts. Wang et al. (2013) studied the performance of Ni-Co/Al2O3 catalysts in pyrolysis of cedar wood. The results demonstrated that the Ni-Co/Al2O3 catalysts with the Ni/Co optimum mole ratio of 0.25 revealed much higher catalytic performance in terms of catalytic activity, the resistance of carbon deposition and catalysts life compared to the Ni/Al2O3 and Co/Al2O3 catalysts. Li et al. (2013) investigated the effect of MgO addition on the performance of Ni/γ-Al2O3 catalysts for catalytic pyrolysis of rice straw to produce hydrogen-rich syngas. They found that MgO improved the catalytic activity of Ni/γ-Al2O3 catalysts and behaved as a promoter for the water gas shift (WGS) reaction.

Another important parameter promoting the activity and stability of catalysts is the selection of suitable supports (Li et al. 2015) because they can facilitate the dispersion of active metal and restrain the aggregation of metal particles efficiently in addition to participate in the catalytic reaction (Wang et al. 2016; Sharma et al. 2017; Zhang et al. 2017). In general, metallic oxide (Al2O3, MgO, CaO, and ZrO2), natural minerals (dolomite, olivine), and zeolites (SBA-15, ZSM-5, and ZY) are frequently applied as the support of Ni-based catalysts. Among these supports, the most widely used is alumina (Zhang et al. 2018), which has a high specific surface area to provide a suitable Ni dispersion, and its mechanical strength ensures the stability of the catalysts (Charisiou et al. 2017). Unfortunately, the abundant amounts of acid sites on the surface of alumina promote coke formation and rapid deactivation of the Ni/Al2O3 catalysts (Chen et al. 2019). Therefore, research on the modification of Al2O3 support has aroused an increasing interest. In the study of Ashok and Kawi (2014), a new Fe2O3-Al2O3 support material was synthesized and used to prepare the Ni/Fe2O3-Al2O3 catalysts. In the toluene reforming test, the Ni/Fe2O3-Al2O3 catalysts with 500 ℃ calcination temperature exhibited more than 90% toluene conversion in 26 h with a H2/CO ratio of 4.5, which performed a superior catalytic activity and stability than Ni/Fe2O3 and Ni/Al2O3 catalysts. Shi et al. (2019) modified alumina with activated carbon (AC) and studied the effect of the Ni-Fe/AC-Al2O3 catalysts on pyrolysis of rape straw to produce syngas. They reported that after using the Ni-Fe/AC-Al2O3 catalysts, the syngas yield increased to 2.22 Nm3/kg, which was more than the Ni-Fe/AC (1.93 Nm3/kg) and Ni-Fe/Al2O3 (1.69 Nm3/kg) catalysts. Moreover, the Ni-Fe/AC-Al2O3 catalysts exhibited stronger resistance to deactivation than the single-supported catalysts. Recently, the use of by-product char of biomass pyrolysis/gasification as the catalysts support has attracted considerable attention due to its relatively low cost and superior physicochemical property (Guo et al. 2018). However, the higher mass loss of the catalysts was found during the catalytic reforming process (Dong et al. 2019). Alkaline earth metal oxides, such as MgO, were also commonly used as support because they can neutralize the acid sites of alumina (Sánchez-Sánchez et al. 2007), thereby inhibiting the formation of carbon deposition. To the authors’ knowledge, when some metal oxides and biomass char are used as support alone, they can facilitate the catalysts to exhibit excellent catalytic performance. However, there also exist some defects. It may be a new research direction that combines alkaline earth metal oxides, biomass char, and Al2O3 as composite supports to improve the catalytic performance of Ni/Al2O3 catalysts; currently there are few well-established studies about this aspect.

Therefore, in the present work, a novel nickel-based catalyst was developed by modifying the conventional Ni/Al2O3 catalysts from the two directions of metal additives and support. The developed catalysts were applied to syngas production from catalytic pyrolysis of rice straw. The Al2O3-MgO-sawdust char (AMS) supports were prepared by co-precipitation method, then the optimum molar ratio of Al2O3, sawdust char, and MgO was investigated. The metal La was doped into the catalysts to change the interaction of metal-support and the structure of catalysts. In addition, the dependence of La content (0, 2, 4, 6, 8, and 10 wt% (dry weight basis)) together with the performance of the catalysts was investigated.



The rice straw (RS), collected from Wuhan, China, was chosen as the feedstock of catalytic pyrolysis in this study. The rice straw was crushed and sieved to obtain a particle size of 0.3 to 0.45 mm prior to being oven-dried for 12 h at 105 ℃. The results of ultimate and proximate analyses of the materials (Table 1) were measured by an elemental analyzer (Flash 2000; Thermo Fisher Scientific, Waltham, MA, USA) and the procedures of GB/T 28731 (2012), respectively. The aluminium nitrate, magnesium nitrate, nickel nitrate, and aqueous ammonia were purchased from Sinopharm Chemical Reagent Co., Ltd. (Shanghai, China). The lanthanum nitrate and carbamide were purchased from Aladdin Industrial Corporation (Shanghai, China). The sawdust char were obtained by pyrolysis of sawdust under a nitrogen gas flow rate of 500 mL/min from room temperature to 700 ℃ at a heating rate of 10 ℃/min in a tube furnace and maintained for 2 h to ensure the complete pyrolysis.

Table 1. Proximate and Ultimate Analyses of the Rice Straw

Catalysts Preparation

Preparation of supports

The AMS supports were prepared by the co-precipitation method. The appropriate amounts of aluminium nitrate, magnesium nitrate, and sawdust char (SC) were firstly dissolved in 200 mL deionized water with vigorous stirring for 30 min. After the mixture was evenly dispersed, the pH value of the solution was slowly adjusted to 10 with aqueous ammonia (25%) and the solution was further stirred for 3 h to complete the precipitation process. Then, the mixture solution was dried at 110 ℃ in an oven for 48 h after standing at ambient temperature for 6 h. Finally, the AMS supports were obtained after the support precursors were calcined under a nitrogen gas atmosphere from room temperature to 800 ℃ at a heating rate of 10 ℃/min in a tube furnace and kept stable for 3 h. A series of molar ratios of Al2O3 to MgO and SC were designed as 5:1:1, 4:1:1, 3:1:1, 2:1:1, and 1:1:1. The as-prepared catalyst supports were denoted as AMS-1, AMS-2, AMS-3, AMS-4, and AMS-5, respectively.

Loading of active metal

A series of Ni-based catalysts with the Ni loading of 10 wt% and various La content were prepared by co-precipitation method. A total of 5 g AMS supports were mixed with the solution containing the required amount of nickel nitrate, lanthanum nitrate, and carbamide in a 250-mL round-bottom flask. After that, the mixture solution was stirred for 2 h in an oil bath at 115 ℃ and then aged overnight. Subsequently, the mixture was dried at 110 ℃ for approximately 6 h in an oven after filtration washing to neutral with deionized water. The resulting powder was calcined under a nitrogen gas atmosphere from room temperature to 750 ℃ at a ramping rate of 10 ℃/min in a tube furnace and held for 2 h to yield NiO-xLa/AMS catalysts, where x represents the different La contents (0, 2, 4, 6, 8, and 10 wt%).

Apparatus and Procedure

The whole lab-scale catalytic pyrolysis experimental device (Fig. 1) includes a gas supply system, pyrolysis reactor, gas purification system, syngas collection, and analysis system. The conversion of rice straw to syngas was completed in a horizontal fixed-bed quartz tube furnace reactor (3 kW, 240 V). The furnace can be slid left and right to control the finishing of pyrolysis reaction of rice straw. The reactor was approximately 60 mm in inner diameter, 1400 mm in total length, and 600 mm in the heating zone. Two quartz boats were applied to hold the rice straw and catalysts. Prior to the test, two quartz boats containing 2 g of rice straw and 1 g of catalysts were placed at one end of the quartz tube, and then the flanges at both ends of the furnace were closed. After that, nitrogen was used as the carrier gas and introduced continuously into the reactor with a flow rate of 200 mL/min for 20 min to provide an oxygen-free atmosphere. Then, the reactor was heated from ambient temperature to 700 ℃ at a ramping rate of 10 ℃/min and held for 20 min. Once the temperature of heating zone was preheated to 700 ℃, the two quartz boats with feedstock and catalysts were quickly pushed in. At the end of the reaction, the valves at both sides of the tube and nitrogen source were opened and the syngas was then carried into the gas sample bag by nitrogen gas. The gas analyzer (Gasboard-3100; Cubic-Ruiyi, Wuhan, China) was used to determine the gas composition and content. Each test was repeated several times to ensure the reliability of experimental data.

Fig. 1. Schematic diagram of the experimental system


The total metal loading levels (wt%) of the catalysts were quantified by X-ray fluorescence (EDX-720; Shimadzu, Kyoto, Japan) spectrometry. The crystalline phases were detected by X-ray diffraction (XRD-7000; Shimadzu, Kyoto, Japan). The textural properties of the catalysts, such as specific surface area, total pore volume, and average pore diameter, were investigated using the N2 isothermal adsorption-desorption at 77 K by an automatic specific surface area and pore analyzer (ASAP 2460; Micromeritics, Atlanta, GA, USA). The morphological characteristics of catalysts were elucidated from the images, which were obtained using the field emission scanning electron microscope (JSM-7100F; JEOL, Ltd., Akishima, Japan) with energy dispersive X-ray (INCA X-MAX 250; OXFORD Instruments, Oxford, London). The gas product was collected with a gas sample bag and analyzed using an infrared gas analyzer (Gasboard-3100; Cubic-Ruiyi, Wuhan, China).


Characterization of NiO/FA Catalyst

X-ray fluorescence (XRF) analysis

The elemental compositions of the support and catalysts are shown in Table 2. It should be pointed out that XRF cannot detect the carbon element; thus it was only used for qualitative analysis in this study. The XRF spectrum of the relative mass fraction ratio of Al2O3 and MgO was 2.28:1, which was close to the theoretical ratio of 2.53:1 (converted by the molar ratio of Al2O3 to MgO of 1:1), indicating that Al and Mg were successfully combined by the co-precipitation method. Meanwhile, the NiO content of the Ni/AMS-5 catalysts was 15.52 wt%, which was higher than the theoretical NiO loading of 12 wt% (converted by the theoretical Ni loading of 10 wt%). The NiO and La2O3 content of the Ni-10La/AMS-5 catalysts was also higher than the theoretical value. It has been commonly accepted that XRF is mainly for the micro-areas of material and is considered as a semi-quantitative analysis (Bo et al. 2008). Thus, there were some errors in the results. However, it can be seen that the relative contents of NiO and La2O3 were approximately equal, which was consistent with the theoretical situation. Simultaneously, it revealed that Ni and La were successfully loaded onto the support.

Table 2. XRF Analyses of the Support and Catalysts

X-ray diffraction (XRD) analysis

Figure 2 illustrates the XRD spectrograms of different supports and catalysts. It can be observed from (a) through (c) that there were several characteristic peaks around 2θ = 37.1°, 45.0°, 59.6°, and 65.8°, corresponding to the crystal structure of MgAl2O3. The appearance of the peaks at 2θ values of 37.0°, 44.9°, 59.7°, and 65.5° in (d) through (f) referred to NiAl2O4, which were indistinguishable in the XRD spectra with MgAl2O4 (Tichit et al. 1997).

Fig. 2. XRD patterns of (a) AMS-1, (b) AMS-3, (c) AMS-5, (d) Ni/AMS-1, (e) Ni/AMS-3, (f) Ni/AMS-5, (g) Ni-2La/AMS-5, (h) Ni-6La/AMS-5, and (i) Ni-10La/AMS-5

For lanthanum promoted catalysts, some new diffraction lines were detected standing for the Ni and La2O3 phase. Moreover, the XRD spectra of (g) through (i) showed that the intensity of Ni phase diffraction peaks were gradually enhanced with the increase of La additive content. This indicated that the addition of La promoter was conducive to the formation of the Ni phase. R1 to R3 were the possible reactions that occurred during the preparation of catalysts. The CO2 produced by the decomposition of Ni2(OH)2COduring calcination R3 would participate in reaction of R4. Subsequently, reaction of R5 occurred due to the presence of char in the support, and CO was produced that could reduce compound Ni to elemental Ni. Meanwhile, the higher the La content, the broader and weaker were the characteristic peaks of NiAl2O4 that appeared, demonstrating that the crystal particles became smaller (Surendar et al. 2017). This result revealed that La could effectively decrease the particle size of NiAl2O4.

It has been commonly believed that smaller metal particles engender more active sites, which are more conducive to catalytic pyrolysis reaction (Chen et al. 2019). It was noteworthy that no diffraction peaks of C appeared in the (a) through (i) XRD spectra. However, there was a weaker and wider peak around 30° in each spectrum, which was close to the main characteristic diffraction peak of C. This result indicated that the amorphous C formed during precipitation and calcination processes, leading to XRD cannot detect the diffraction peaks of C.

CO(NH2)2 + 3H2O → CO2 + 2NH3•H2O (R1)

2Ni2+ + 4OH + CO2 → Ni2(OH)2CO3 + H2O (R2)

Ni2(OH)2CO3 → NiO + CO2 +H2O (R3)

La2O3 + CO2 → La2O2CO3 (R4)

La2O2CO3 + C → La2O3 + CO (R5)

Field emission scanning electron microscopy (FESEM) and energy dispersive X-ray (EDX) analysis

The surface morphology of the support and catalysts were investigated by FESEM images, and the distribution of inorganic matters in the support and catalysts were analyzed by EDX, which are presented in Fig. 3 and Table 3. Figure 3(a) shows that the supports were composed by many irregular flaky particles and thus formed many pores. After loading Ni, the surface of catalysts became a relatively regular circular or elliptical flaky interlace structure, and some particles were filled in them as illustrated in Fig. 3(c). It can be seen from Fig. 2(d) through (f) that Ni was present in the form of NiAl2O4 in the Ni/AMS-5 catalysts. Therefore, the regular flaky structure was mainly generated by the interaction between active component and support. In contrast to Fig. 3(c), there were fewer particles between the flakes on the surface of the Ni-10La/AMS-5 catalysts in Fig. 3(e), which increased the amount of pores and facilitated more exposure of active sites to volatiles. The elemental composition analysis of the support and catalysts are listed in Table 3, revealing that the relative contents of Ni and La were close to the theoretical load of 10 wt%, indicating the active metal was successfully loaded on the support.

Table 3. Element Compositions of Support and Catalysts

Fig. 3. FESEM-EDX images of (a) AMS-5, (b) AMS-5 EDX, (c) Ni/AMS-5, (d) Ni/AMS-5 EDX, (e) Ni-10La/AMS-5, and (f) Ni-10La/AMS-5 EDX

Brunauer–Emmett–Taylor (BET) analysis

The BET surface area, total pore volume, and average pore diameter of the supports and catalysts are summarized in Table 4. Compared with the AMS-5 support, the BET surface area of the Ni/AMS-5 catalysts decreased from 186.8 to 91.5 m2•g-1, which was ascribed to the fact that some of the active component Ni was loaded into the pore of the support surface. After addition of La, the BET surface area of catalysts increased from 91.5 to 130.2 and 158.4 m2•g-1, which was consistent with FESEM analysis. The XRD analysis showed that the introduction of La reduced the crystal size of NiAl2O4, which meant that originally blocked pores were partially exposed. The BET surface area may not be the key factor influencing the catalytic activity. Moreover, the superb catalytic performance was more determined by active components (Yu et al. 2019). Wu et al. (2013) studied the catalytic pyrolysis of biomass over Ni-Ca/Zn-Al catalysts, observing that Ni-Ca-Al (1:9) catalysts with the highest BET surface area exhibited the lowest H2 yield, which was similar with the results in Fig. 5. Moreover, the variation trends in the total pore volume was consistent with that of the BET surface area. The average pore diameter of the AMS-5 support, Ni/AMS-5, Ni-6La/AMS-5, and Ni-10La/AMS-5 catalysts was 12.9, 13.8, 12.1, and 13.3 nm, respectively. Catalysts with high average pore diameter can promote the reactivity of catalytic pyrolysis process because its average pore size is sufficient for gases diffusing into the active sites of catalysts for secondary cracking reaction to yield syngas (Loy et al. 2018).

Table 4. Textural Properties of Support and Catalysts

Effect of Modified Ni/Al2O3 Catalysts in Pyrolysis of RS

Effect of modified supports in pyrolysis of RS

The dependence of different modified supports on the gas concentration is presented in Fig. 4, while the reaction temperature, holding time, and Ni loading was fixed at 700 ℃, 20 min, and 10 wt%, respectively. As a comparison, the situation of non-catalytic pyrolysis and addition of the Ni/Al2Ocatalysts was also evaluated under the same reaction conditions. The syngas concentration for RS pyrolysis after addition of catalysts was always higher than RS pyrolysis alone at the same reaction conditions. The syngas concentration was increased from the smallest of 31.5 vol% (RS) to the highest of 69.2 vol% (Ni/AMS-5) when the catalysts were used. Previous literature has reported that metallic nickel can promote the tar cracking by dissociating C–O and subsequently rupturing C–H and C═C bonds, thus contributing to the syngas component (i.e., H2 and CO) formation (Matas Güell et al. 2011). Meanwhile, the catalysts facilitated tar dry reforming reaction (R6) towards the positive direction, which made more tar decompose into H2 and CO. Figure 4 shows that the lower CHconcentration usually was associated with the higher H2 and CO concentration, especially after using the Ni/Al2O3, Ni/AMS-4, and Ni/AMS-5 catalysts. This phenomenon was ascribed to these catalysts and was excellent in activating methane steam reforming (R7 and R8) and decomposition (R9). Similar results have been reached by Loy et al. (2018), who reported that the highest H2 concentration associated with the lowest CH4 concentration was obtained after introducing nickel into the pyrolysis of rice husk. Furthermore, compared with the Ni/Al2Ocatalysts, the Ni/AMS-5 catalysts increased syngas concentration by 14.9 vol% including 9.8 vol% H2 and 5.1 vol% CO. These findings indicated that the Ni/AMS-5 catalysts exhibited a better catalytic activity than the Ni/Al2O3 catalysts in the syngas production. From Fig. 4, it can be obtained that H2 and CO concentrations were increased from 25.6 vol% and 18.9 vol% to 40.8 vol% and 28.4 vol%, respectively, when the ratio of Al2O3, MgO, and SC was decreased from 5:1:1 (Ni/AMS-1) to 1:1:1 (Ni/AMS-5). In addition, the CH4 and CO2 concentration declined slightly with the increment of MgO and SC relative content. These results revealed that a suitable ratio of Al2O3, MgO, and SC could enhance CH4 reforming reaction (R7, R8, and R10) towards the positive direction.

Tar dry reforming reaction:

CnHm + nCO2 → 2nCO + m/2H2 (R6)

CH4 steam reforming reaction: CH4 + H2O → CO + 3H2 (R7)

CH4 + 2H2O → CO2 + 4H2 (R8)

CH4 decomposition: CH→ C + 2H2 (R9)

CHdry reforming reaction: CO2 + CH4 → 2CO + 2H2 (R10)

Water gas shift reaction (WGS): CO + H2O→ H2 + CO2 (R11)

The higher heating values (HHV) and lower heating values (LHV) of the gas products were calculated according to Eqs. 1 and 2 (Shahbaz et al. 2017). As shown in Table 5, the HHV of the gas products ranged from 9.51 to 10.57 MJ/m3 after the addition of modified catalysts. Bridgwater (1996) reported that the average HHV of non-catalytic pyrolysis of biomass was 4 to 7 MJ/m3. This meant that all modified catalysts can enhance the pyrolysis of RS to produce more energy. In addition, both HHV and LHV of the gas products reached maximum value when the Ni/AMS-5 catalysts were used. Consequently, compared to other catalysts, the Ni/AMS-5 catalysts were more effective for clean energy production. In contrast, the Ni/Al2O3 catalysts exhibited the worst activity in producing high quality fuel gas. This can be ascribed to the lower CH4 and CO concentration after using the Ni/Al2O3 catalysts.

It has been revealed that in chemical manufacturing industries, such as Fischer-Tropsch synthesis, petrochemical manufacture, and bio-oil production, the H2/CO molar ratio of syngas should be in the range of 1 to 3 (Lu and Lee 2007). From Table 5, the H2/CO molar ratio increased from the lowest value (0.79) of non-catalytic pyrolysis to the highest value (1.43) of catalytic pyrolysis by the Ni/AMS-5 catalysts. The data indicates that the Ni/AMS-5 catalysts performed well in improving the quality of syngas similarly and were more preferable for chemical manufacturing.

LHV = (25.7 H2 + 30 CO + 85.4 CH4) × 0.0042 (1)

HHV = (30.52 H2 + 30.18 CO + 95 CH4) × 0.0042 (2)

In Eqs. 1 and 2, the unit of LHV and HHV is MJ/m3; H2, CO, and CH4 were the volume fractions (vol%) in the fuel gas.

Fig. 4. Effect of support types on the concentration of H2 (vol%) and CO (vol%)

Table 5. Gas Characteristics of RS Pyrolysis with and Without Catalysts