Heteropolyacid Salt Catalysts for Methanol Conversion to Hydrocarbons and Dimethyl Ether: Effect of Reaction Temperature

Abstract

Phosphotungstic and silicotungstic acid salt catalysts (CuPW, CuSiW, FePW, FeSiW) were synthesized by substitution of protons with ferric and copper ions through a simple replacement reaction. The structure and thermal stability were characterized by IR, XRD and TG, and the salts showed a keggin structure and a thermal tolerance near 450 °C. Temperature programmed reactions indicated that the four catalysts showed similar trends in the change of methanol conversion, DME selectivity, and light olefins selectivity at 100–400 °C. Copper salt catalysts showed a 100% DME selectivity at temperatures ranging from 100–250 °C, while FeSiW and FePW catalysts had a 100% DME selectivity near 250 °C. Moreover, the heteropolyacid salt catalysts also produced a certain number of light olefins at the temperature ranging from 250–350 °C, and the CuSiW catalyst exhibited the highest ethylene and propylene selectivity of 44%. In the stability test evaluated at 200 °C, the catalysts showed different tendencies during the induction period and the same trends during the reduction period for the methanol conversion to DME, due to the differences in the strengths of the strong acid sites. Finally, the silicotungstic acid salt catalysts showed the longest lifetime of 120 h, much longer than the heteropolyacids. This approach provides an effective way to synthesize hydrocarbons through methanol, especially DME, at different temperatures using one catalyst.

1. Introduction

Methanol is among the top 10 commercial chemicals with wide applications, including chemical intermediates and fuels [1]. Among them, the most important are the reactions of methanol conversion to hydrocarbons, especially dimethyl ether (DME) and light olefins. Dimethyl ether is one of the most promising compounds because of its mild physical and chemical properties and wide application in energy and environmental fields [2,3]. Dimethyl ether has no corrosiveness to metals, skin irritation, or carcinogenicity, and has low-environmental harm due to its low level of nitrous oxides during its particulates emission combustion process, hence, it was honored as a clean energy in the 21st century [3,4,5]. Currently, DME is mainly used as an aerosol propellant and refrigerating fluid, as well as a substitution for diesel due to its high-octane value, burning properties, and low emissions [6,7,8]. Dimethyl ether can also be a substitution for liquefied petroleum gas (LPG) for civil use because its readily compressible and has a high heat of combustion [8,9]. Moreover, DME is also a useful chemical stock for many important reactions such as high-selective synthesis of propylene [10,11], methylation reaction for dimethyl sulfate [12], carbonylation reaction for ethyl acetate and acetic anhydride [13], and oxidation reaction for formaldehyde [14]. On account of the ever-increasing demand, more attention is paid to the synthesis of DME.

Currently, there are two main routes for DME synthesis in industrial production [15,16]. One is the one-step synthesis of syngas to DME over a high-activity and high-stability bi-functional catalyst which combines the formation and dehydration of the methanol process, the typical catalyst is a mixture of a Cu/Zn-based catalyst with a solid-acid catalyst like γ-Al₂O₃ [17,18,19,20]. Another route is the direct synthesis of DME through methanol dehydration over a solid-acid catalyst [8,21]. The main solid-acid catalysts used are γ-Al₂O₃, composite oxides like SiO₂–Al₂O₃, TiO₂–ZrO₂, and SiO₂–TiO₂, sulfated ZrO₂, metal salts like AlPO₄, Al₂(SO₄)₃, and zeolites [17,22,23,24,25,26,27,28,29]. Despite the high methanol conversion capacity, they need high operation temperatures due to the low acid concentration, which results in undesired by-products such as light hydrocarbons and coke that will reduce the DME production and deactivate the catalysts [30,31,32].

Recently, some researchers began to focus on the catalytic performance of heteropolyacids (HPAs) in methanol conversion to DME reaction and obtained excellent performance, they exhibit high reaction rates at much lower reaction temperatures [30,33,34,35,36,37,38,39,40]. The main drawbacks of HPAs are the low surface area and high acid strength, which cause strong interactions between H₂O molecules and the acid sites of the HPAs [33]. The commonly used solution is to disperse the catalyst on the high surface area carrier, and these catalysts are more active and resistant than the corresponding bulk HPAs for the dehydration of methanol to DME [33,41,42]. The conversion of methanol to hydrocarbons over heteropolyacid salt catalysts were studied [43,44]. The catalyst activities of different metal salts of heteropolyacids were also compared, and copper salt and ferric salt catalysts showed high activities [44]. In this article, we synthesized a series heteropolyacid salt catalysts which substitute protons with Cu²⁺ and Fe³⁺ ions using a simple method to decrease the acid density. Then, we studied the catalytic performance for the methanol conversion to hydrocarbons in a temperature programmed process and the stability performance of the methanol to DME reaction for the first time. Temperature programmed reactions showed an extremely high DME selectivity (100%) and a certain amount of light olefins production at different reaction temperatures. Meanwhile, the catalysts showed a 120-h lifespan for the methanol to DME reaction at 200 °C, which is a quite low reaction temperature for the reaction of methanol to DME.

2. Results and Discussion

2.1. Characterization of the Catalysts

2.1.1. Structure and Thermal Stability of Heteropolyacid Salts

Fourier transform infrared spectroscopy (FTIR) was applied to study the structure of heteropolyacid salts and the results are shown in Figure 1a–c. There were four typical peaks for phosphotungstic acid and silicotungstic acid, respectively. In Figure 1a, the four characterization peaks 1080 cm⁻¹, 984 cm⁻¹, 888 cm⁻¹, and 803 cm⁻¹ could be assigned as a P–Oa asymmetric stretch, W=Ot asymmetric stretch, W–Ob–W asymmetric stretch, and a W–Oc–W asymmetric stretch [45,46,47]. The peaks in Figure 1b can be assigned as 980 cm⁻¹ (W=Ot asymmetric stretch), 927 cm⁻¹ (Si–Oa asymmetric stretch), 878 cm⁻¹ (W–Ob–W asymmetric stretch), and 789 cm⁻¹ (W–Oc–W asymmetric stretch), while the peak at 1020 cm⁻¹ is still difficult to be assigned [48]. Figure 1a,b indicate that the heteropolyacid ions retain the characteristic of keggin structure after the reaction with salts. The thermal stability of the CuPW and CuSiW were then studied to check the thermal tolerance of keggin structure. The IR results are shown in Figure 1c,d, and the typical peaks for the phosphotungstic structure remain clear until 450 °C. However, they thoroughly disappear upon 500 °C treatment, which manifest a thermal tolerance at temperatures ranging from 450 °C to 500 °C for the keggin structure. The result is consistent with the results reported in Reference [33]. As for the silicotungstic structure, the typical peaks began to disappear when subjected to the treatment at 450 °C, indicating a thermal tolerance ranging from 400 °C to 450 °C.

XRD (X-ray diffraction) patterns were recorded to characterize the phase composition of synthesized heteropolyacid salts, and the results are presented in Figure 2a,b. The peaks of the salts were different with corresponding acids, indicating the formation of salts. The typical peaks of HPW can be seen in the phosphotungstic acid salt while the no-acid phase existed in the silicotungstic acid salt, implying that the phosphotungstic acid salts existed with more acid impurities than the silicotungstic acid salts catalyst.

The TG (Thermogravimetry) analyses were carried out to confirm the weight change during the heating process and the results are shown in Figure 2c, all the samples show a light weight loss (<5%) till 900 °C. The sharp weight loss stage of CuPW and CuSiW ended at 350 °C while the sharp stage for ferric salts ended at 250 °C, whilst the mild step for both salts ended near 600 °C. The platform till 150 °C indicated the successful removal of the physically adsorbed water during the pre-treatment process. The stage between 150 °C to 350 °C can be assigned to the chemically crystalline water, which ends at different temperature indicating the different ability of affinity to water for copper and ferric salts. The second weight loss stage between 500 °C to 600 °C represents the destruction of keggin structure to oxides [30], being consistent with the IR results.

2.1.2. Composition and Textural Properties of Heteropolyacid Salt Catalysts

Nitrogen adsorption–desorption measurement was applied to characterize the textual properties of the heteropolyacid salt samples, and the results are shown in

Table 1. Compositions and textural properties of the as-synthesized heteropolyacid salt samples.

Sample Name	W/M a	W/Mtheo		SBET b (m2/g)	Smicro c (m2/g)	Sext c (m2/g)	Vmicro c (cm3/g)	Vmeso d (cm3/g)	RMeso e %	RMacro e %	Average Pore Size (nm)
CuPW	6.75	8	3.05		0.56	2.49	2.34·10−4	1.03·10−2	62.5	37.5	13.48
CuSiW	5.56	6	3.48		0.22	3.26	5.10·10−5	1.20·10−2	62.1	37.9	13.73
FePW	9.44	12	3.41		0.91	2.50	3.69·10−4	6.42·10−3	76.0	24.0	7.28
FeSiW	8.35	9	1.21		0.31	0.90	1.05·10−4	3.51·10−3	38.8	61.2	11.42

^a Measured by inductively coupled plasma (ICP), W/Cu or W/Fe. ^b S_BET (total surface area) calculated by applying the BET equation using the linear part (0.05 < P/Po < 0.30) of the adsorption isotherm. ^c S_micro (micropore area), S_ext (external surface area), and V_micro (micropore volume) calculated using the t-plot method. ^d V_meso (mesopore volume) calculated using the BJH method (from desorption). ^e R_meso and R_macro calculated the ratio of mesopore and macropore by the BJH method (from desorption) [49].

and Figure 3. All samples have a hysteresis loop in the high relative pressure region (type-IV isotherms) and scarcely any type I isotherms which increase rapidly under low-relative pressure, proving the main existence of mesopores, which corresponds with the micropore volume and mesopore volume shown in Table 1. The DFT (Density functional theory) pore-size distribution indicates that the mesopore mainly ranged between 5–50 nm. The ratios of mesopore volume and macropore volume are also shown in Table 1. The average pore diameter for copper salts were very close, while the values for ferric salts were smaller. All heteropolyacid salt samples had a quite low BET surface area (<5 m²·g⁻¹) due to the low volume of pores. The ICP-OES (Inductively coupled plasma optical emission spectrometry) was used to characterize the ratio of W/M (W/Cu or W/Fe) and the results are shown in Table 1. The experimental results are less than the theoretical W/M ratio, implying that the hydrogen ions were not completely substituted by metal ions. The substitution ratios of metal ion for CuPW and FePW were smaller than the CuSiW and FeSiW catalysts, which corresponds with the XRD results in Figure 2.

2.1.3. Acid Properties of Heteropolyacid Salt Catalysts

The acidic properties of the samples were confirmed by NH₃-TPD analyses and the results are presented in Figure 4 and

Table 2. Acid sites distribution of the as-synthesized heteropolyacid salt samples.

Sample Name	Weak Acid Sites (mmol/g) (100–250 °C)	Medium Acid Sites (mmol/g) (250–450 °C)	Strong Acid Sites (mmol/g) (Above 450 °C)	Total (mmol/g)
CuPW	0.28	0.20	1.19	1.67
CuSiW	1.02	0.07	1.03	2.12
FePW	0.15	0.16	1.29	1.60
FeSiW	0.39	0.47	0.82	1.68

. The number of acid sites represents the acid concentration of the catalyst, while the position of the peaks represents the strength of the acid sites. CuPW, FePW, and FeSiW have a similar amount of total acid sites of about 1.60 mmol·g⁻¹, while CuSiW has a much higher number of total acid sites (2.12 mmol·g⁻¹) because of the prominent high quantity of weak acid sites. For phosphotungstic acid salts, copper, and ferric salts have similar ratio of three kinds of acid sites. Copper silicotungstic has a high amount of weak acid sites (1.02 mmol·g⁻¹) and a low amount of medium acid sites (0.07 mmol·g⁻¹), while ferric silicotungstic has a similar amount of weak acid sites (0.39 mmol·g⁻¹) and medium acid sites (0.47 mmol·g⁻¹). Considering the strength of strong acid sites, it can be seen that the four catalysts show different behaviors. The peak values of CuSiW and FeSiW catalyst are 500 °C and 497 °C, while the results are 522 °C and 560 °C for CuPW and FePW catalysts, respectively. This indicates that the as-synthesized silicotungstic catalysts show similar acid strengths, which are weaker than that of phosphotungstic catalysts, especially for the FePW catalyst. The acid strength shows a correlation with the metal ion substitution obtained from the ICP-OES results, and the smaller substitution ratio of metal ion will leave more protons and result in stronger acid strength.

2.2. Temperature Programmed Reaction of Methanol Conversion

The product distribution of the temperature programmed methanol conversion using heteropolyacid salt and heteropolyacid catalysts were performed to explore their catalytic behavior and the results are shown in Figure 5. The evaluation temperature ends at 400 °C for the keggin structure will be destroyed at higher temperatures according to the IR results. These catalysts exhibit similar trend for the products distribution with increasing reaction temperature. Methanol conversion is very low at temperatures lower than 125 °C, then it increases rapidly with the increase of reaction temperature. During this period, DME is the predominant product (almost 100%), the methanol conversion keeps at same high limits due to the equilibrium of methanol to DME reaction. Thereafter, DME selectivity decreases and hydrocarbons begin to form in the effluent when reaction temperature reaches 250 °C. This is because higher reaction temperature will push the equilibrium of methanol to DME reaction to the methanol side [35]. What’s more, the formation of hydrocarbon pool species [50] at this temperature will consume methanol and DME, then produce light olefins and other hydrocarbon by-products. Therefore, at this temperature, light olefins such as ethylene and propylene can be obtained. When temperature is higher than about 350 °C, it is interesting that the main product changes to methane with much higher methanol conversion during this period. Higher reaction temperature will lead to bigger conjugated structure hydrocarbon pool species [50], which will deactivate the catalyst. The formation of methane in the methanol conversion to hydrocarbons reaction is favored by high temperature and weak acid sites dominated on deactivated catalyst [51].

Figure 6a–c give out the methanol conversion, DME and light olefins selectivity of the temperature programmed conversion of methanol over different catalysts. FeSiW catalyst has a relative high methanol conversion at low temperature ranging from 100 °C to 175 °C, but lower conversion at temperatures higher than 225 °C. CuPW shows a completely methanol conversion at temperatures of 325 °C till 375 °C, while CuSiW has a completely methanol conversion at temperatures of 375 °C till 400 °C. Methanol conversion of HPW and HSiW catalysts are lower than FeSiW, but higher than other 3 salts before 200 °C. It was noticeable that they exhibit higher methanol conversion during 200-300 °C than heteropolyacid salt catalysts. The DME selectivity retains almost at 100% from 125 °C to 250 °C for HPW, HSiW, CuPW, CuSiW and FeSiW, while the DME selectivity for FePW is lower than 90% at 125-170 °C due to the formation of propane and low methanol conversion. Light olefins selectivity also shows similar trend at temperatures of 250-375 °C. CuPW has the highest light olefins selectivity of 34% at 280 °C. FeSiW and FePW have the highest light olefins selectivity of 28% at 315 °C, whilst CuSiW has the highest light olefins selectivity of 44% at 310 °C. The light olefins selectivity for HPW is higher than its salts and the selectivity for HSiW are between the two salts.

2.3. Catalytic Performance of Heteropolyacid Salts for Methanol to DME

Figure 7 shows the catalytic performance of heteropolyacid salts and heteropolyacids for the methanol conversion to DME at 200 °C in the fixed bed reactor with a space velocity of 2 h⁻¹. The selectivity of DME for all catalysts are almost 100% at this temperature. Heteropolyacid salt catalysts have a much longer lifetime than the heteropolyacids. The catalysts show different tendencies in the initial 10 h, but exhibit the same trend after 20 h. The methanol conversion of CuSiW and FeSiW catalysts increase rapidly in the initial 20 h, and then decrease slowly to ~66% at a lifetime of 120 h. Methanol conversion of CuPW catalyst increases slightly in the initial 3 h, and then decreases slowly thereafter. The highest methanol conversion was 72% and the final rate was 48% after 100 h reaction. However, the methanol conversion of FePW catalysts was as high as 91% at the instant that methanol contacted the catalyst surface, but decreased rapidly to the lowest one of all the catalysts after 20 h. HPW and HSiW catalysts showed the same trend with FePW, but with a faster decreasing rate. Thus, we can conclude that the silicotungstic acid salt catalysts have a quite long induction period, while the phosphotungstic acid salt catalysts have a very short induction time, especially for the FePW catalyst. Presumably, this is because the four catalysts possess different acid strengths according to the NH₃-TPD results. Generally, higher acid site strength results in faster induction and higher methanol conversion in the beginning of the reaction. Heteropolyacids and FePW catalysts have the highest acid strength and the shortest induction period, while CuPW has a lower acid strength and longer induction period. Both FeSiW and CuSiW exhibited similar acid strengths lower than phosphotungstic acid salts, therefore, they show similar induction time and the same changing trend of methanol conversion, demonstrating that methanol conversion and lifetime are related to the strength of acid sites.

3. Experimental

3.1. Chemical Reagents

The heteropolyacids used were phosphotungstic acid (H₃PW₁₂O₄₀·xH₂O, abbreviated as HPW, AR, Aladdin Biochemical Technology Co., Shanghai, China) and silicotungstic acid (H₄SiW₁₂O₄₀ ·xH₂O, abbreviated as HSiW, AR, Aladdin Biochemical Technology Co., Shanghai, China), while the salts used were CuCl₂·2H₂O (AR, 99%, Guangzhou Chemical Reagent, Guangzhou, China) and FeCl₃·6H₂O (AR, 99%, Aladdin Biochemical Technology Co., Shanghai, China). The raw material used for catalyst evaluation was anhydrous methanol (AR, 99.5%, Guangzhou Chemical Reagent, Guangzhou, China) which dehydrated with 4 Å molecular sieves for more than 2 days, and SiC (AR, 99%, Aladdin Biochemical Technology Co., Shanghai, China) was used as dispersing agent.

3.2. Measurement

Fourier transform infrared spectroscopy (FTIR) was conducted on a Perkin Elmer spectrum 100 spectrometer (PerkinElmer Inc., Waltham, Massachusetts, USA) equipped with a transmission infrared attachment to confirm the typical peaks of keggin structure of heteropolyacid salts. The IR spectrum was obtained by tableted KBr powder and tested at room temperature in the region from 4000 to 400 cm⁻¹ at a step of 4 cm⁻¹. Samples that calcined at different temperatures for IR test were prepared in muffle furnace (SX2, Shanghai Laboratory Instrument Works Co., Ltd., Shanghai, China) under air atmosphere for 2 h. X-ray powder diffraction pattern (XRD) was collected to determine the crystalline phase of the samples on a RIGAKU D-MAX 2200 VPC diffractometer (Rigaku Corporation, Tokyo, Japan) operated at 40 kV and 26 mA with a Cu-Kα radiation (λ = 1.5406 Å). Thermogravimetric (TG) analysis was performed to study the thermal performance of the samples on a PerkinElmer Pyris Diamond TG/DTA instrument (PerkinElmer Inc., Waltham, MA, USA). The sample was pretreated at 120 °C for 30 min to remove the physically adsorbed water and followed by a decrease of the temperature to 50 °C, then heated to 900 °C with a heating rate of 10 K/min under air atmosphere. The acid properties of the as-synthesized heteropolyacid salts were studied by temperature programmed desorption of ammonia (NH₃-TPD) with a Micromeritics Autochem II 2920 device (Micromeritics, Norcross, GA, USA). The as-synthesized samples (100 mg) were pre-treated under pure He at 200 °C for 1 h to remove the adsorbed gas and water, then stabled at 100 °C to saturate the sample with gaseous NH₃ under NH₃/He with a flow of 50 mL·min⁻¹ and kept for 0.5 h, removed the physically adsorbed NH₃ under He flow for 0.5 h, finally measured the amount of desorbed NH₃ with a temperature programming process at a heating rate of 10 K/min from 100 °C to 600 °C under He flow (50 mL/min). A Micromeritics ASAP 2460 analyzer (Micromeritics, Norcross, GA, USA) was applied to measure the Nitrogen adsorption–desorption isotherms at 77.15 K, the sample (about 0.5 g) were degassed at 100 °C under vacuum overnight. The total surface area was calculated based on the Brunauer–Emmett–Teller (BET) equation according to the linear part (0.05 < P/P0 < 0.30) of the adsorption curves. The micropore volume, external surface area, and micropore surface area were evaluated by the t-plot method using the linear part of 0.35 < P/P0 < 0.50 with a principle of minimal slope. The mesopore volume was calculated using the Barrett–Joyner–Halenda (BJH) method from the desorption curve. The pore volume distribution was obtained from the density functional theory (DFT) method. Elemental compositions of the catalyst were confirmed by inductively coupled plasma optical emission spectrometry (ICP-OES) analyses on a Perkin–Elmer Optima 8300 instrument (PerkinElmer Inc., Waltham, MA, USA). The catalyst was dissolved by concentrated nitric acid and drops of HF solution with hydrothermal treatment at 70 °C overnight in an autoclave, then diluted with deionized water to keep a 5 wt. % acidity.

3.3. Synthesis of Heteropolyacid Salts Catalyst

Typically, 0.01 mol heteropolyacids (HPW or HSiW) were dissolved in 100 mL deionized water in a beaker and heated to 80 °C under water bath, then 1.5 or 2 molar equivalents CuCl₂·2H₂O were added to the HPA solution and continuously stirred for 3 hours, while the molar ratio for FeCl₃·6H₂O were 1 and 1.33 for HPW and HSiW, respectively. Then, the solutions were filtered and evaporative crystallized to remove the undissolved and dissolved impurities. Finally, the products were dried at 120 °C overnight and finely ground for further use.

3.4. Catalytic Evaluation

The performance of the catalyst for methanol conversion reaction was carried on a metallic tubular fixed-bed reactor (10-mm inner diameter) under atmospheric pressure; the reaction temperature was confirmed by a K-type thermocouple placed into the catalytic bed directly. Flow rates were controlled by Brooks 5850E (Brooks instrument, Hatfield, PA, USA) mass flow controllers. In a typical process, 3 g of the thoroughly dried heteropolyacid salts catalyst was mixed uniformly with 3 g SiC powder to prevent heat concentration and loaded in the tubular fixed-bed reactor. The species and quantities of the products were confirmed by an online gas chromatograph (Tianmei, GC-7890-Ⅱ, Tianmei Scientific Instrument Co., Shanghai, China) which equipped with a Plot-Q column (RESTEK, Rt®-Q-Bond, 30 m, 0.32 mm ID, 10 um df, Beijing, China) and a flame ionization detector (FID). The effluent distribution of the products were calculated based on the amounts of the CH₂ species. Methanol conversion and product selectivity were calculated by the mass balance method as follows:

$${\mathrm{CH}}_3\mathrm{OH}\mathrm{conversion}\%=\frac{\left[\mathrm{Methanol}\mathrm{consumed}\right]}{\left[\mathrm{Methanol}\mathrm{total}\right]}\times 100\%$$

(1)

$$\mathrm{Product}i\mathrm{selectivity}\%=\frac{\left[\mathrm{Number}\mathrm{of}\mathrm{methanol}\mathrm{turned}\mathrm{into}i\mathrm{product}\right]}{\left[\mathrm{Methanol}\mathrm{consumed}\right]}\times 100\%$$

(2)

Temperature programmed reaction procedure: the stock was fed by bubbling the liquid methanol (at 30 °C) through the flowing carrier gas (N₂) with a rate of 30 mL·min⁻¹, corresponding to a weight hourly space velocity (WHSV) of 0.25 h⁻¹ (confirmed by the weight of the consumed methanol, 17.8 vol.% methanol). The initial temperature was set at 80 °C with methanol flowing during the heating process. The temperature interval was set as 25 °C and stabled for 0.5 h for each temperature point, and the GC spectrum data were collected twice for each temperature point and the run time for each spectrum was 20 min.

In the stability tests of DME production reaction, the catalyst (m_cat = 1.5 g, mixed with 1.5 g SiC) was pre-treated under N₂ atmosphere at 300 °C for 1 h without bubbling methanol, then decreased the reaction temperature to 200 °C and bubbled methanol (at 50 °C) through N₂ with a rate of 30 mL·min⁻¹, corresponding to a weight hourly space velocity (WHSV) of 2.0 h⁻¹ (46.0 vol. % methanol). Mass and heat transfer limitations were ruled out by theoretical calculation (see Supplementary Materials) according to the criteria in the references [52,53,54,55,56].

4. Conclusions

In summary, phosphotungstic and silicotungstic acid salt catalysts were synthesized via a simple replacement reaction. The as-synthesized catalysts showed 100% DME selectivity at 175–225 °C and long lifetime for methanol to DME reaction at 200 °C. They also showed a quite high ethylene and propylene selectivity at higher temperatures. Meanwhile, effluent distribution of methanol conversion to hydrocarbons at different temperatures can be monitored by the temperature programmed reaction. All catalysts exhibited quite different induction behavior in the stability test due to the differences in acid strengths, and the induction period had a positive correlation with the strength of strong acid sites. The heteropolyacid salt catalysts showed much longer lifetimes than their heteropolyacids. This work provides a simple way for effective utilization of heteropolyacid for methanol conversion reaction. The methanol conversion to hydrocarbons, especially DME, can be effectively performed at different temperature using one catalyst.