The hierarchical SAPO-34 zeolites were synthesized by two-step hydrothermal process. The molar ratio of the precursors composition was: Al₂O₃:P₂O₅:SiO₂:DEA:H₂O:CTAB = 1:0.9:0.6:1.6:50:0.05. The typical synthesis procedure is as following: First, mix the pseudo-boehmite (Shandong Aluminum Company, 69.0 wt%) with distilled water (Qingdao Chengda Distilled Water Co., Ltd.) and stir until a homogeneous suspension is formed. Then, the phosphoric acid (Sinopharm Chemical Reagent Co., Ltd, 85.0 wt%) diluted with water was added dropwise into the pseudo-boehmite suspension under rapidly stirred, and kept on stirring for 40 minutes to obtain a mixed gel A. After that, the silica gel (Qingdao Ocean Chemical Co., Ltd., 25.0 wt%) was added into the mixed gel A and stirred for another 1 hour to obtain a mixed gel B. Then the gel B was dropped into the dissolve CTAB (Sinopharm Chemical Reagent Co., Ltd, 99 wt%) to obtain a mixed gel C. The gel C was aged at room temperature for 2 h with stirring, and then transferred into a 100 mL Teflon-lined stainless steel autoclave to pretreat at 100˚C for 12 hours (the sample was labeled S-F after calcination). After that, the template for the synthesis of SAPO-34DEA (Sinopharm Chemical Reagent Co., Ltd., 99 wt%) was added into the autoclave when it was cooled to room temperature. After stirred for 2 hours, the autoclave was re-covered and the mixed gel was crystallized at 180˚C for 12 hours, 24 hours, 36 hours and 48 hours, respectively. The products were separated and washed, and calcined at 550˚C for 5hours to obtain a series of hierarchical SAPO-34 molecular sieves, which were labeled as S-12, S-24, S-36 and S-48 samples.

In contrast, microporous SAPO-34 molecular sieve (labeled S-W) was synthesized by a conventional hydrothermal synthesis method according to the literature [23] . Samples synthesized by one-step crystallization route were labeled S-O. One-stepcrystallization route has the same method to obtain the aged gel C, and then the aged gel C was added into DEA and stirred for 2 hours to obtain the gel D. Finally, the gel D was transferred into the autoclave to crystallize at 180˚C for 48 hours.

The crystal phase structure and crystallinity of the sample were characterized by X-ray diffractometer (DX-2700, China, Dandong Haoyuan Instrument Co., Ltd.). Test conditions: room temperature, Cu target, Kα source, tube voltage 40 kV, tube current 30 mA, scan range 2θ = 5˚ - 40˚. The morphologies of the samples were observed using a scanning electron microscope (JSM-6390LV, JEOL, Japan). The N₂ adsorption-desorption isotherm, specific surface area, and pore volume of the samples were measured on a fully automatic specific surface area and porosity analyzer (ASAP 2460, Micron, USA). Prior to the measurement, the samples were degassed under vacuum at 300˚C for 4 hours. The coke amount for the used catalyst was analyzed by a thermogravimetric analyzer (TG209F3, Germany, NETZSCH). The coked catalyst was heated from 50˚C to 800˚C with a heating rate of 10˚C/min and air flow rate of 100 mL/min.

The acidity of the sample was measured by temperature?programmed desorption of ammonia (NH₃-TPD) on a chemisorption analyzer (FINETEC FINSORB-3010). Typically, the sample was first pretreated at 200˚C for 30 min with a ramp rate of 20˚C/min in the helium flow of 20 mL/min. When the temperature was dropped to 50˚C, the 5% NH₃/95% He was introduced to adsorbe on the catalyst for 40 min until saturation. After that, it was purged with helium at 20 mL/min for 1 h, followed by increasing temperature to 800˚C at a rate of 20˚C/min.

The catalytic performance of these samples for DTO reaction was measured with a fixed bed reactor. In brief, 2 g catalyst (20 - 40 mesh) was charged into the reactor (550 mm × 10 mm), and activated at 450˚C for 1 hour under a nitrogen (50 mL/min) atmosphere prior to reaction. Subsequently, DME gas with WHSV = 0.725 h^-1 was introduced into the reactor for 6 h, when cooling to 400˚C. The reaction product was detected on-line by Shimadzu Corporation GC-2014C gas chromatography. After the reaction stopped, the catalyst was cooled to room temperature under nitrogen, and the used catalyst was subjected to coke deposition analysis by a thermos-gravimetric analyzer.

Figure 1(a) reveals that the S-O is a mixture of SAPO-34 and SAPO-5 molecular sieve. Moreover, the S-48 is the pure SAPO-34 molecular sieve. This result indicates that the two-step method can solve the problem that mesoporous template and microporous template cannot collaborate to synthesize hierarchical SAPO-34 molecular sieves. The XRD diffraction pattern of S-F shows that the first step is to polymerize the raw materials into the aluminum phosphate under the function of CTAB.

From Figure 1(b) we can know: the S-12 and S-24 samples showed characteristic peaks of CHA structure and a peak cluster composed of three peaks at about 21˚, which is the aluminum phosphate. This is because some of the raw materials have not yet been converted into crystals due to the short crystallization time, and this part of the raw material forms the dense phase AlPO₄. The crystallinity of SAPO-34 enhanced with the improvement of crystallization time from 24 hours to 36 hours. After 36 hours of crystallization, the AlPO₄ peaks disappeared, this indicates that AlPO₄ has been completely converted to SAPO-34. After 48 hours of crystallization, the diffraction peak of S-48 is obviously higher than that of S-36. This is probably due to the existence of hierarchical

pores makes defects in crystals, which leads the diffraction peak of S-36 lower than that of S-48.

The hierarchical pores of S-36 were supported by CTAB micelles. These micelles could be destroyed by exposing to the high temperature for along time [21] . The crystals containing hierarchical structure were gradually transformed into more stable microporous crystals with the crystallization time further extended to 48 hours. That results in the obviously enhanced diffraction peak for S-48, which is also supported by the BET results. S-48 still has some defects, so the peak of S-48 is lower than that of S-W.

Figure 2(a) is the microporous SAPO-34 molecular sieve with regular cubic structure synthesized by conventional hydrothermal method. From Figure 2(b) to Figure 2(f), the formation process of the hierarchical SAPO-34 zeolite was recorded. Figure 2(b) shows that the S-F is spherical agglomerates, which were formed by the initial polymerization of raw materials under the function with CTAB. Figure 2(c) shows that the S-12 sample maintained a spherical particle, and the effect of DEA on its morphology has not yet been demonstrated. Combined with the XRD results, we can know that the nucleation could not be generated unless the existence of DEA. This is the initial stage of crystallization. The initial spherical structure has been destroyed after 24 hours of crystallization and then a large number of fragments were formed due to the existence of DEA, as shown in Figure 2(d). As the extending of crystallization time, these fragments had become crystals or participated in the crystallization process. It can be got from Figure 2(e) that the amorphous particles had disappeared and turned into crystals after 36 hours, which was consistent to the XRD results. Figure 2(f) shows that the macro-morphology of SAPO-34 zeolite changed little when the crystallization time was extended from 36 hours to 48 hours.

It can be inferred that the raw materials formed spherical aggregates under the

function of CTAB in the first step. These spherical aggregates contained CTAB micelles, and the micelles formed the hierarchical structure of spherical aggregates. Then the spherical agglomerates were destroyed, disintegrated and crystallized under the effect of DEA. From the XRD results, we can know it is difficult to obtain pure SAPO-34 without the aggregate in the first step. The aggregate generated in the first step will be disintegrated in the subsequent process, so the shape of the aggregate is not the key for this experiment. CTAB could improve the viscosity of crystalline system, which promoted the agglomeration and growth of minute crystals. Therefore, the large SAPO-34 molecular sieve with hierarchical structure was formed. The mesoporous structure assembled by CTAB was gradually destroyed and transformed into the microporous structure after a longer crystallization time. This change belongs to the variation of microstructure (supported by BET results) instead of the change of macro-morphology.

All the four samples prepared by adding CTAB show H4 hysteresis loops in type IV isotherm according to the IUPAC, which was obtained by the N₂ adsorption-desorption characterization (Figure 3). Figure 3(b) is an amplified view of the samples. Figure 3(a) reveals that the starting point of the hysteresis loops is between 0.4 and 0.5 relative pressure, indicating the presence of mesoporous structure. The decreasing trend of hysteresis loop of samples from S-12 to S-48 indicates the gradual destroy of the mesoporous structure with the prolongation of crystallization time. This can also be verified by the variation of average poresize (shown in Table 1).

From the Table 1, it can be seen that the specific surface area of hierarchical molecular sieves is slightly smaller than that of microporous molecular sieves due to the low crystallinity of hierarchical molecular sieves (listed in Table 1). Meanwhile, it can be directly observed that the S_micr decreased and the S_ext increased with the prolongation of crystallization time from 24 h to 36 h, which suggests the dissolution of some small crystal particles and the accumulation of some small crystal particles to bulk crystals. S-48 has the small hysteresis loop with the small S_ext, its S_micr is similar to S-W, while its average pore size is much larger than that of S-W. These all indicate S-48 contains a little of stacking holes, which consist with our previous conjecture.

S_total: Total specific surface area, S_micr: Micropore specific surface area, S_ext: Specific surface area outside the micropore, V_total: Total pore volume, V_micr: Micropore volume, V_ext: pore volume outside the micropore volume, A_w: Integral area of weak acid peak, A_s: Integral area of strong acid peak, A_t: total area.

The acidity of catalysts shows a vital impact on the selectivity of products and catalyst lifetime in the catalytic dimethyl ether (methanol) to olefins. The acid strength and acid amount of the present catalysts were determined by using NH₃-TPD. The results are shown in Figure 4. It is observed that all the samples showed characteristic peak of weak acid center (~200˚C) and a strong acid center (~500˚C). The acid amount increased gradually with the crystallization time extending to 36 hours, while the total acid amount varied a little after 36 hours. The less acid amount of S-24 than S-36 was attributed to the lower crystallinity. With the further crystallization up to 48 hours, more silicon enter the framework due to the substitution mechanism [24] , which might cause some small silicon islands connect together and result in the reduced number of silicon hydroxyl and slightly decrease of acid amount.

According to the crystallization rule of SAPO-34, most silicon made up the framework of molecular sieve by directly participating in the process of nucleation and crystal growth, while a small amount of silicon entered by substituting mechanism in the later stage of crystallization [24] [25] . Combined with XRD results, it found that the nucleation and growth of zeolite were in progress before 36 h and the crystallization was progressed after 36 hours under our synthetic conditions. Silicon mainly joined the framework by the substitution mechanism after 36 hours, and it produced some silicon islands and enhanced the acidity of the zeolites. So the acidity of S-48 is obviously stronger than that of S-36. The acid strength of S-W with crystallization time for 48 hours is similar to that of S-36, which can be attributed to the fact that CTAB increases the viscosity of crystallization system and speeds up the growth of molecular sieves. It is reported that the crystal size affects the acidity [26] . Therefore, we believe that the enhancement of S-48 acidity is not only caused by the increase in particle size,

but also due to more silicon enters the crystal as the crystallization time increases [24] .

The results of the respective catalysts in the DTO reaction are showed in Figure 5. It shows that S-24 and S-48 were quickly deactivation after 1 hour of reaction and almost all the catalytic activity has been lost after 4 hours of reaction. The conversion rate of DME on S-36 was 77.3% after 4 hours of reaction, while that on S-W was only 27.6%. Therefore, the catalytic stability of S-36 is better than that of S-W.

Coke deposition is considered to be the main reason for the deactivation of SAPO-34 molecular sieves [27] [28] . The coke amount of the catalysts with time on stream for 6 hours was measured by thermos gravimetric analysis. The results are listed in Table 2. The results show that the coke content in S-24 is the lowest (4.37%), but it deactivated quickly. This is due to the poor crystallinity of S-24 and the lack of catalytic activity of dense phase AlPO₄, which can be confirmed by the above characterizations.

According to the report in the literature [10] [26] [29] [30] , the MTO reaction requires reasonable cooperation between strong acid center and weak acid center, among which the strong acid sites are beneficial for the coke deposit. S-48 has more weak acid content than S-36, but its strong acid center is enhanced and

Reaction conditions: T = 400˚C, WHSV = 0.725 h⁻¹.

its strong acid content is reduced than S-36 (in Table 1). Therefore, we believe that S-36 has the most suitable acid strength and acid content. The internal hierarchical structure could greatly increase the diffusion of the product to suppress the coke formation. S-48 has stronger acid centers than S-36 and S-W. Its crystal size is large with few mesoporous in it. These characteristics make it easy to deposit coke. But its coke content (9.53%) is lower than that of S-36 (14.19%) and S-W (16.51%). This is because it is easy to deposit coke, which causes rapid blockage of superficial pores and makes the inner active centers difficult to participate in the reaction. This reduces the utilization rate of active sites while reducing the production of coke. S-36 and S-W have similar acid environment, and the crystal size of S-36 is much larger than S-W, but the coke content of S-36 (14.19%) is much lower than S-W (16.51%), and the conversion of DME is also much higher than the latter. This result can be attributed to the fact that the hierarchical structure can effectively increase the diffusion efficiency of products, inhibit the occurrence of secondary reactions and thus reduce the production of coke.

The product distribution of each sample is showed in Table 3. The methane content in the product increased greatly, and the conversion of dimethyl ether decreased greatly on S-24 and S-48. It indicated that they have been seriously inactivated. Although the crystal size of S-36 is much larger than S-W, the introduction of hierarchical holes in the crystal can significantly enhance the product diffusion efficiency, so the selectivity of olefins on S-36 (86.64%) is higher than that on S-W (84.02%). The good diffusion efficiency can effectively suppress the occurrence of the secondary reaction, such as the hydrogen-transfer reaction [31] . This can also effectively inhibit the formation of alkanes while increasing the selectivity of the light olefins. It is known that the increase of diffusion efficiency is more advantageous to long chain products. And the structure of SAPO-34 determines there are very few C⁴⁺ products. So the increase of propylene selectivity is most obvious on S-36. Table 3 shows that S-36 (51.29%) has a 0.24% increasement in the ethylene selectivity over S-W (51.05%) and the propylene selectivity increased from 32.97% to 35.35% and by 2.38%. In conclusion, the hierarchical SAPO-34 synthesized by this method has higher catalytic stability, higher selectivity for low olefins and higher selectivity for propylene

Reaction conditions: T = 400˚C, WHSV = 0.725 h^-1, t = 4 h.

than the microporous SAPO-34. Its catalytic performance is superior to that of microporous SAPO-34 zeolite.