Facile and Rapid Synthesis of Durable SSZ-13 Catalyst Using Choline Chloride Template for Methanol-to-Olefins Reaction

Abstract

In the current study, a facile and rapid synthesis approach for a SSZ-13 catalyst using choline chloride (CC) as a template was proposed, and the catalytic performance for the methanol-to-olefins (MTO) reaction was examined. With a proper amount of CC addition (i.e., m(CC)/m(SiO₂) = 0.14), uniform and homogeneously distributed cubic SSZ-13 crystals were obtained within 4 h with lower aggregation. The synthesized catalyst demonstrated excellent porous features with a total specific surface area and mesopore volume of 641.71 m²·g⁻¹ and 0.04 cm³·g⁻¹, respectively. The optimized strong and weak acid sites on SSZ-13 were obtained by regulating the m(CC)/m(SiO₂) ratio. The less strong acid sites and a larger amount of weak acid sites in the synthesized catalyst were conducive to the catalytic performance of the MTO reaction under a lower reaction temperature (450 °C). The appropriate acidity and well-developed pore structure of synthesized SSZ-13 could also slow down the carbon deposition rate and, thus, significantly improve the catalytic lifetime of the catalyst. The methanol conversion rate and initial selectivity of light olefin using the synthesized catalyst could maintain over 95% and 50%, respectively, and a lifetime of 172 min was achieved. Although the low olefin selectivity of the synthesized SSZ-13 catalyst was slightly lower than that of the purchased one, its desirable features were thought to have good potential for industrial application.

1. Introduction

The methanol-to-olefins (MTO) reaction has been intensively studied in recent years with a particular focus on the development of highly reactive and durable catalysts [1,2,3]. Chabazite (CHA) zeolite with a favorable structure is expected to be an ideal candidate for the MTO reaction [4,5]. As a promising CHA material, SSZ-13 has a unique porous structure and a high hydrothermal stability that enables its high efficiency and selectivity [6,7]. The ordered crystal structure is quite essential for the preparation of the SSZ-13 zeolite. Conventionally, the costly N, N, N-trimethyl-1-adamantyl ammonium hydroxide (TMADaOH) was used as a template for the synthesis of SSZ-13. Although the properties of the hierarchical pore SSZ-13 are excellent, its synthesis process is complicated with the inevitable environmental pollution caused by the toxic template precursor TMADaOH. In addition, a long synthesis period (more than one week) is usually needed to compensate for the slow growth of the crystal. Therefore, the development of an environmentally friendly and cost-effective template agent or non-template agent method with a reduced synthesis cycle remains a challenge to be tackled. A novel route for rapid and facile synthesis of the SSZ-13 catalyst is crucial and necessary.

The key factors affecting the synthesis of the SSZ-13 zeolite are the template and processing conditions. The seed-guided method complying with the core–shell growth mechanism in the crystallization process could affect the structure of the molecular sieve. Synthesis of a high-purity SSZ-13 molecular sieve was achieved by crystallization under 100 °C for 4 days after exploring the influence of the number of seeds [8,9]. Alternatively, the synthesis period of the SSZ-13 zeolite was significantly decreased to a few hours by steam-assisted crystallization without the aid of a seed crystal [10,11]. Currently, an emerging process of a template method for controlling the mesoporous structure and adjusting the size of the pore channel is now attracting more attention. A series of growth-modifier-assisted synthesis methods were established based on the disclosed particle attachment crystallization mechanism. Particularly, significant progress has been made in the use of polymers to control the synthesis of zeolites. Polymer hydrogels consist of three-dimensional networks of polymer chains cross-linked by physical means. They can be used as micro- or nano-reactors to control the nucleation, assembly, and growth of zeolites [12,13]. By combining TMADaOH and C_22-44Br₂ (2 bromo-n-22~44 alkane) in the gelation process, a hierarchical pore SSZ-13 molecular sieve was synthesized in one step [14]. However, such methods were usually with a high synthesis cost and low yield, which hindered its further industrial production.

Limited mass transfer in the microporous molecular sieve and formation of coke in the cages could lead to a high deactivation propensity and low efficiency for the catalytic MTO reaction. Introducing hierarchical pores to the zeolite is one of the methods for the extensive utilization of CHA-type zeolite in the MTO reaction [15,16,17]. At present, extensive studies have also been conducted to reduce the crystal size to the nanoscale or introduce auxiliary mesopores/macropores to obtain hierarchical pore materials [18,19]. The use of organic guide agents, such as a cationic polymer template agent, anionic polyacrylamide (APAM), and/or polydimethyldiallyl chloride (PDADMAC), to self-assemble could result in the formation of hierarchical pores with an intermediate pore size of about 5~20 nm and micropore size of 0.8 nm [20,21]. Such approaches have been proven to be a useful method to prepare mesoporous molecular sieves [22].

The status quo determines that the facile and rapid synthetic method of the SSZ-13 zeolite is crucial to a sustainable methanol economy. This study aimed to demonstrate a novel synthesis process for the SSZ-13 zeolite based on the traditional hydrothermal method. A series of process parameters were optimized, including the quaternary ammonium alkali, silica/alumina ratio, alkali/silicon ratio, water/silicon ratio, amount of seed, aging time, and crystallization temperature. In particular, the role of soft template choline chloride (CC) was revealed. In addition, the effects of CC on the porous characteristics and catalytic performance of SSZ-13 were also examined. It is expected that the synthesis of novel molecular sieve materials will be extended through a greener and more efficient process.

2. Results and Discussion

2.1. The Crystal Structure of Synthesized SSZ-13

Primarily, a series of processing parameters, including the silica/alumina ratio, alkali/silicon ratio, water/silicon ratio, amount of seed, aging time, and crystallization temperature, were systematically optimized (as shown in Figure S1). The key factor, namely the ratio of n(CC)/n(SiO₂), impacting the catalyst feature was principally focused. The XRD patterns of synthesized materials with different ratios of m(CC)/m(SiO₂) are presented in Figure 1. Without the addition of the CC template, the product was an ANA (Analcime)-zeolite in pure phase (Figure 1a). With the addition of the CC template agent, the characteristic peak of ANA at 2θ = 15.9° gradually disappeared. The secondary structural unit of SSZ-13 was gradually formed in the mixed gel. As m(CC)/m(SiO₂) = 0.14, a pure SSZ-13 phase was generated with a relative crystallinity of 101.2% (Figure 1d, Table S1). This could prove that the CC template greatly accelerated the formation of the SSZ-13 structure. In addition, the excessively increasing amount of the CC template agent did not show an apparent influence on the SSZ-13 crystal structure. Therefore, the m(CC)/m(SiO₂) ratio of 0.14 was the optimal condition to obtain a fully crystallized SSZ-13 molecular sieve with low cost (taking the commercially available SSZ-13 as a reference). The optimized condition details for the synthesis of SSZ-13 using the CC template are described in the Supplementary Materials and Figure S1.

2.2. Morphology of Catalysts

Figure 2 presents the SEM images of prepared SSZ-13 catalysts with different ratios of m(CC)/m(SiO₂) = 0.07, 0.14, and 0.32. The sample prepared by m(CC)/m(SiO₂) = 0.07 was irregular particles dominated by a cubic shape and mixed with many differently sized crystals (Figure 2a). It was thought that with the lower addition of the template agent, it would be hard to achieve complete crystallization of the amorphous gel into regular SSZ-13 molecular sieves. The particles were severely aggregated rather than homogeneously dispersive. The serious aggregation was ascribed to the lack of a specification template agent and slow nucleation rate as well as the insufficient crystal nucleus formation during the hydrothermal synthesis. With the m(CC)/m(SiO₂) ratio increased to 0.14, the irregular particles gradually disappeared, as shown in Figure 2b. Even though the particles demonstrated slight aggregation, the cubic crystals were homogeneously distributed. The appropriate amount of template could meet the condition for rapid and ordered growth of catalyst crystals. Compared with the synthesized sample with m(CC)/m(SiO₂) = 0.14, it could be seen that the purchased commercial SSZ-13 sample was still in serious agglomeration form (Figure 2d). This may indicate the excellent performance of as-prepared SSZ-13 using a choline chloride template. With the m(CC)/m(SiO₂) ratio increased to 0.32, the particles became a worse agglomeration (Figure 2c), and the crystal morphology changed to be ambiguous. It was considered that the excessive amount of the choline chloride template might promote the growth of the larger sized crystal and, consequently, induce the locally sudden agglomeration. This is consistent with the XRD analysis that indicated that m(CC)/m(SiO₂) = 0.14 is the optimal condition to obtain relative uniform and cubic particles without undesired agglomeration. In addition, the synthesis time was shortened to 4 h, which highly improved the preparing efficiency.

2.3. Variation of Microstructure

The FTIR spectra of the SSZ-13 prepared under different m(CC)/m(SiO₂) ratios are exhibited in Figure 3. Roughly, the peak vibrations of the synthesized samples were similar. The typical absorption peaks at 460, 526, 647, 777, and 1069 cm⁻¹ were assigned to the SSZ-13 molecular sieve. The asymmetric stretching of Si-O-Si or Al-O-Si bond was a wide and strong peak near 1069 cm⁻¹, which was classified as T-O-T vibration. Likewise, the peak at 777 cm⁻¹ was the symmetrical vibration of Al-O. The peak vibration of a single six-member ring was at around 526 cm⁻¹. In addition, ca. 647 cm⁻¹ was the peak vibration of a double six-member ring. The strong absorption peak near 460 cm⁻¹ was due to the bending vibration of Si-O in a silicon–oxygen tetrahedron. The peaks at 1631, 3450, and 3615 cm⁻¹ were the stretching of -OH. Two weak peaks at 2924 and 2849 cm⁻¹ were attributed to the stretching of -CH₂- derived from the residual organic template.

From Figure 3, it can be seen that the absorption peak at 1069 cm⁻¹ became narrower with the m(CC)/m(SiO₂) ratio increase, indicating the gradual order and regularity of the SSZ-13 crystal. The FTIR is extremely sensitive to the change in the silica–alumina microstructure. With the addition of choline chloride, the absorption peaks at 647 and 526 cm⁻¹ gradually appeared, revealing the formation of a bi-hexagonal ring unit in the SSZ-13 framework. The formation of the bi-hexagonal ring structure proved that the template facilitated the crystallization process; the increase in the absorption peak intensity suggested the crystallization becoming gradually complete. Clearly, the catalyst prepared with m(CC)/m(SiO₂) = 0.14 showed the sharpest peak at 1069 cm⁻¹ (Figure 3c), implying the relatively ordered Si-O-Si or Al-O-Si structure without extra distortion. This is consistent with the results discussed in XRD and SEM analyses.

2.4. The Pore Structure of as-Prepared SSZ-13

The reactions on the molecular sieve are very sensitive to the framework structure. The adsorption–desorption isotherms of synthesized samples with different m(CC)/m(SiO₂) are shown in Figure 4. In addition, their surface area and pore volume are listed in

Table 1. Pore structure characteristics of as-prepared zeolites.

Sample	SBET (m2·g−1)	Smic (m2·g−1)	Sext (m2·g−1)	Vmic (cm3·g−1)	Vmeso (cm3·g−1)
m(CC)/m(SiO2) = 0.07	419.18	410.64	8.54	0.16	0.02
m(CC)/m(SiO2) = 0.14	641.71	636.06	5.65	0.24	0.04
m(CC)/m(SiO2) = 0.32	583.62	569.04	14.57	0.21	0.03

. The results suggest that the synthesized SSZ-13 samples possessed Langmuir adsorption–desorption isothermal curves. The SSZ-13 samples had homogenously distributed microporous channels. In the low-pressure region (10⁻⁶ < P/P₀ < 0.01), an obvious spike was observed, which was induced by the adsorption of nitrogen molecules in the micropores. The adsorption plateau appeared at P/P₀ > 0.1, approaching adsorption saturation. At P/P₀ > 0.95, the adsorption isotherm gradually increased and arrived at the highest point because of capillary condensation. At the relative pressure P/P₀ = 0.45, the desorption curve closed, forming the hysteretic ring, which indicates that the synthesized zeolite contained stacking mesopores formed by the accumulation of small crystal particles. Such small particles were also found in the SEM images (Figure 2). Particularly, the catalyst prepared with m(CC)/m(SiO₂) = 0.14 showed a more significant mesopore structure with an obvious hysteretic ring (Figure 4b). As presented in Table 1, the total specific surface areas of samples prepared at m(CC)/m(SiO₂) = 0.07, 0.14, and 0.32 were 419.12, 641.71, and 583.62 m²·g⁻¹, respectively; the mesopore volumes were 0.02, 0.04, and 0.03 cm³·g⁻¹, respectively. Undoubtedly, the proper amount of template agent with m(CC)/m(SiO₂) = 0.14 achieved the largest specific surface area and the highest mesopore volume.

2.5. The Acidity of SSZ-13

The ammonia temperature-programmed desorption method (NH₃-TPD) could reveal the acid properties of the as-prepared SSZ-13. The NH₃-TPD of the SSZ-13 catalysts prepared with different m(CC)/m(SiO₂) and purchased SSZ-13 are presented in Figure 5. There were two typical desorption peaks found in the samples. The peak near 200 °C was the low-temperature desorption region, which was attributed to the interaction between acid level and ammonia gas. NH₃ could be desorbed from these weakly acidic surface hydroxyl groups, forming the weak acid potential of SSZ-13. The peak in the range of 490~540 °C was the high-temperature desorption peak from the bridging hydroxyl group (≡Si-OH-Al≡), corresponding to the strong acid center. The desorption peaks in the low-temperature region were stronger, suggesting that the weak acid sites were dominant. With the increase in m(CC)/m(SiO₂), the strong acid potential tended to shift to a high-temperature region. The corresponding peak area increased greatly at m(CC)/m(SiO₂) = 0.14.

Table 2. The acidity of as-prepared SSZ-13 measured by NH₃-TPD.

Samples	Weak Acid Site		Strong Acid Site
	Temperature (°C)	Acidity (mmol/g)	Temperature (°C)	Acidity (mmol/g)
m(CC)/m(SiO2) = 0.07	200	0.43	505	0.51
m(CC)/m(SiO2) = 0.14	210	0.67	536	0.55
m(CC)/m(SiO2) = 0.32	201	0.45	511	0.80
Purchased SSZ-13	203	0.35	510	0.56

shows that the weak and strong acidities of m(CC)/m(SiO₂) = 0.14 were 0.67 and 0.55 mmol/g, respectively. According to the SEM images, at m(CC)/m(SiO₂) = 0.14, the particle size distribution became more uniform and the specific surface area increased significantly, indicating a larger amount of acid sites on the surface. The optimized strong and weak acid sites were obtained by regulating the m(CC)/m(SiO₂), which would be conducive to the catalytic performance of such a catalyst under relatively low temperature.

2.6. Catalytic Performance for MTO Reaction

Based on the optimal conditions described, the catalytic activity of the synthesized SSZ-13 material for the MTO reaction was evaluated. As a typical acid catalytic reaction, SSZ-13 can demonstrate the role of a bifunctional catalyst. The catalytic performance of purchased (using the TMAdaOH as template) and synthesized (using the CC as template with m(CC)/m(SiO2) = 0.14) SSZ-13 for the MTO reaction is shown in Figure 6 and Figure 7. The products were mainly C1~C3 alkanes and alkenes. The ethylene and propylene were the dominant compounds, and their yield reached its highest at 60~90 min. The yields were maintained at over 35% during the test. The main byproducts were CH₄, C₂H₆, and C₃H₈. In the early stage (before 40 min) of the MTO reaction, the methanol was first decarbonylated for the formation of intermediates, such as acetate, formate, methyl acetate, and dimethoxymethane, while the zeolite was carbonylated during the induction period. The yield of byproducts was continuously decreased during the reaction period, indicating the improvement of reaction selectivity and deactivation of the catalyst.

Both the SSZ-13 catalysts maintained a high methanol conversion rate over 95% within a reaction time of 120 min, and it drastically dropped to ca. 80% at 80 min. Eventually, the conversion rate was maintained at ca. 75% in a long reaction period (Figure 6). The synthesized SSZ-13 exhibited a better conversion rate than that of the purchased one. The catalytic lifetime of the molecular sieve was defined as the duration that the methanol conversion was kept above 90%, i.e., the time from the beginning of the reaction to the methanol conversion dropping to 90%. From the NH₃-TPD analyses, the weak acidity of synthesized (m(CC)/m(SiO2) = 0.14) and purchased SSZ-13 was 0.67 and 0.35 mmol/g, respectively; the strong acidity was 0.55 and 0.56 mmol/g, respectively. Consequently, the as-prepared and purchased samples exhibited obvious differences in the catalytic lifetime. Their catalyst lifetimes were 172 and 160 min, respectively. The reaction intermediates, such as methylbenzene, were gradually converted into polycyclic aromatic hydrocarbons, which might have caused accumulation on the internal surface and outside the cage of SSZ-13, thus leading to congestion of the channel and a lower mass transfer rate. Eventually, it became difficult for the reactants to contact the active center, resulting in catalyst deactivation. It was considered that the appropriate acidity and well-developed pore structure of synthesized SSZ-13 could slow down the carbon deposition rate and significantly increase the lifetime of the catalyst.

Both SSZ-13 catalysts showed an induction period where the selectivity was quite low during the initial 40 min, as shown in Figure 7. The light olefin selectivity was highest at the reaction time of ca. 60 min. The methanol adsorbed at the acid site was the first step of MTO conversion; the deprotonation of carbenium ions and shift of methyl groups were the following reaction. The framework structure of SSZ-13 accelerated the deprotonation of carbenium ions and converted the methyl group into the alkene [23]. Such an induction reaction could occur under a low reaction temperature (i.e., <450 °C). The active hydrocarbon species formed inside the zeolite at the initial stage. Theoretically, the synthesized SSZ-13 with higher acidity would possess a strong adsorption capacity. The light olefine selectivity of the as-prepared SSZ-13 was slightly lower than that of the purchased SSZ-13. It was thus thought that the excessive micropore hindered the timely desorption and diffusion of intermediate products and consequently reduced the light olefin selectivity. Although the light olefin selectivity of the synthesized SSZ-13 was slightly lower than that of the purchased SSZ-13, the initial selectivity could be maintained above 50% within 160 min with the conversion rate over 90%. The larger amount of weak acid sites and relative smaller amount of strong acid sites on the as-prepared SSZ-13 using choline chloride as a template were beneficial for the low temperature catalytic performance and longer lifetime.

3. Experimental Section

3.1. Materials

Sodium hydroxide (NaOH), sodium meta-aluminate (NaAlO₂), aluminum isopropoxide (C₉H₂₁AlO₃), silica-sol LUDOX-40 (mSiO₂·nH₂O), aluminum nitrate nonahydrate (Al(NO₃)₃·9H₂O), ammonium chloride (NH₄Cl), and choline chloride (C₅H₁₄ClNO) were purchased from Shanghai MackLin Biochemical Technology Co., Ltd. (Shanghai, China). The reagents used in this study were analytical pure (AR).

3.2. Sample Preparation

The catalysts were prepared using the hydrothermal synthesis method. In the synthesis process, the ratios of precursors were n(SiO₂)/n(Al₂O₃) = 40, n(Na₂O)/n(SiO₂) = 0.4, and n(H₂O)/n(SiO₂) = 12. The ratio of m(CC)/m(SiO₂) was varied from 0 to 0.32. The SSZ-13 crystal seed was added into the solution with a ratio of m(seed)/m(SiO₂) = 0.4%. During the synthesis process, ca. 3.60 g NaOH and 0.49 g NaAlO₂ were dissolved in deionized water, which was subsequently added in a 2.30 g CC template agent. This solution was stirred for 10 min to ensure sufficient mixing. Subsequently, a commercially available SSZ-13 (Aos Catalytic Materials (Dalian, China) Co., Ltd.) was introduced as a homogenous seed. After intense stirring at room temperature for 20 min, 18.00 g of inorganic silica sol (Ludox-40) was added to the solution slowly. Upon stirring for another 30 min, the initial gel was transferred to a purchased hydrothermal reaction kettle lined with polytetrafluoroethylene, which was placed in a blast-drying oven at a constant temperature of 120 °C and static crystallization. After a period of crystallization, the products were washed to neutral and then dried at 120 °C. Finally, the solid product was placed in a muffle furnace and calcined at 550 °C. The templating agent was thus removed to obtain the Na-type SSZ-13 molecular sieve. The NH₄-SSZ-13 molecular sieve was obtained by exchanging the Na-type SSZ-13 with 1 mol/L of NH₄Cl solution 3 times, and, sequentially, the H-type SSZ-13 was prepared after drying and calcination.

3.3. Characterization of Zeolites

X-ray diffraction (XRD) analysis was conducted on a Rigaku RINT ultimate-III powder diffractometer (Rigaku Co., Ltd., Osaka, Japan). The sample was in powder form. The 2θ range was 5~50° with a scanning rate of 10 °/min. Cu target K_β radiation was used with a tube voltage of 40 kV and a tube current of 30 mA. A scanning electron microscope (SEM, H-7650 Hitachi Co., Ltd., Tokyo, Japan) was used to characterize the morphology and particle size of the materials prepared. FTIR analyses of the raw and as-prepared materials were conducted using an FT/IR-615 JASCO (JASCO, Ltd. Tokyo, Japan) spectrometer in transmission mode. First, the sample (ca. 1 mg) was ground to powder with a size of about 200 mesh and mixed with KBr (ca. 500 mg) using the normal KBr procedure to make the pellet. Then, the pellets were dried in an oven at 60 °C for 12 h. During analysis, the resolution was 4 cm⁻¹ in the range of 4000~400 cm⁻¹ wave number, and perspectrum was 32 scans. Nitrogen absorption and desorption tests were performed using an Autosorb iQ Station 1 (Quantachrome, Florida, United States). Pore volume and size distribution were calculated with the DFT model. Before measurement, the samples were pretreated in vacuum at 200 °C for 12 h. The surface acidity of as-prepared zeolite was determined by ammonia temperature-programmed desorption (NH₃-TPD). Chemical adsorption apparatus (BELCATII Co., Ltd., Tokyo, Japan) equipped with a thermal conductivity detector was used. About 0.05 g of the molecular sieve was loaded into the U-type tube reactor, and then 0.04 g ultrafine silica wool was added to prevent the gas from drifting away. The adsorbed gas was then removed from the sample by heating in an inert gas atmosphere to 350 °C. Subsequently, the sample was cooled to 100 °C under an ammonia flow (flow rate 30 sccm, time 60 min) to achieve saturated adsorption. The He (30 mL/min) was injected for about 30 min to remove the physically adsorbed ammonia gas. Finally, TPD was heated to 700 °C in He with a heating rate of 10 °C/min, and the amount of ammonia gas de-adsorbed from the acidic center was measured by a thermal conductivity cell detector.

3.4. Evaluation of the Catalytic Performance

The MTO reaction was carried out in a fixed-bed quartz tube reactor (Φ6 mm) using the as-prepared catalysts. The schematic of the fixed-bed reactor is illustrated in Figure 8. About 300 mg molecular sieve catalyst (40~60 mesh) and 2.7 g quartz sand were well mixed and loaded into the reactor. The reactor was then heated to 550 °C with an interval of 10 °C/min to first remove the impurities adsorbed in a molecular sieve for 1 h. Subsequently, the temperature was set to a reaction temperature of 450 °C for 20 min. The weight hourly space velocity (WHSV) was 3 h⁻¹. The reaction products were identified and quantified through an in situ gas chromatograph (GC).

4. Conclusions

The time consumption, high cost, and polluting synthesis process are the key drawbacks for the industrial utilization of SSZ-13 catalysts in MTO technology. This work demonstrated a facile and rapid synthesis approach for SSZ-13 using choline chloride as a template. The optimal synthesis condition was explored, and the catalytic performance for the methanol-to-olefins (MTO) reaction was examined. The choline chloride was proved to be effective for the synthesis of SSZ-13. An appropriate ratio of the soft template could meet the condition for rapid and ordered growth of catalyst crystals. The special molecular structure of choline chloride could greatly accelerate the formation of bi-hexagonal ring structure in the SSZ-13 framework, and it could shorten the synthesis cycle to within 4 h. With a proper amount of choline chloride addition (i.e., m(CC)/m(SiO₂) = 0.14), uniform and homogeneously distributed cubic SSZ-13 crystals were obtained with lower aggregation. The catalyst synthesized with m(CC)/m(SiO₂) = 0.14 demonstrated excellent porous features with a total specific surface area and mesopore volume of 641.71 m²·g⁻¹ and 0.04 cm³·g⁻¹, respectively. The optimized strong and weak acid sites on SSZ-13 were obtained by regulating the m(CC)/m(SiO₂). As a typical acid catalytic reaction, the SSZ-13 catalyst with strong and weak acid sites exhibited a bifunctional role. The lower amount of strong acid sites and a larger amount of weak acid sites in the synthesized catalyst were conducive to the catalytic performance for the MTO reaction under a relatively lower reaction temperature. The methanol conversion rate using synthesized catalyst was maintained over 95% within 120 min, and its lifetime was achieved to 172 min. The appropriate acidity and well-developed pore structure of synthesized SSZ-13 could slow down the carbon deposition rate and significantly increase the lifetime of the catalyst. Moreover, the initial selectivity of light olefin could be maintained above 50% within 160 min. Although the low olefin selectivity of the synthesized SSZ-13 catalyst was slightly lower than that of purchased one, its desirable features were thought to have good potential for industrial application.