# Effect of Calcination Temperatures and Mo Modification on Nanocrystalline (γ-χ)-Al2O3 Catalysts for Catalytic Ethanol Dehydration

Authors: Tharmmanoon Inmanee; Piriya Pinthong; Bunjerd Jongsomjit
Journal: Journal of Nanomaterials
 (2017)

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## Abstract

The mixed gamma and chi crystalline phase alumina (M-Al) catalysts prepared by the solvothermal method were investigated for catalytic ethanol dehydration. The effects of calcination temperatures and Mo modification were elucidated. The catalysts were characterized by X-ray diffraction (XRD), N2 physisorption, transmission electron microscopy (TEM), and NH3-temperature programmed desorption (NH3-TPD). The catalytic activity was tested for ethylene production by dehydration reaction of ethanol in gas phase at atmospheric pressure and temperature between 200°C and 400°C. It was found that the calcination temperatures and Mo modification have effects on acidity of the catalysts. The increase in calcination temperature resulted in decreased acidity, while the Mo modification on the mixed phase alumina catalyst yielded increased acidity, especially in medium to strong acids. In this study, the catalytic activity of ethanol dehydration to ethylene apparently depends on the medium to strong acid. The mixed phase alumina catalyst calcined at 600°C (M-Al-600) exhibits the complete ethanol conversion having ethylene yield of 98.8% (at 350°C) and the Mo-modified catalysts promoted dehydrogenation reaction to acetaldehyde. This can be attributed to the enhancement of medium to strong acid with metal sites of catalyst.


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## Body

## 1. Introduction

Ethylene is intermediate in the petroleum industry and used as feedstocks to produce a variety of polymers in petrochemical industry such as polyethylene, polyvinyl chloride, and polystyrene. Therefore, the demand of ethylene continually increases. The total consumption of ethylene and other light olefins was around 174 millions of tons in 2004. It continuously increased up to 205 million tons in 2010 and it is predicted to grow up to 259 million tons in 2016 [1]. Moreover, ethylene is used as the precursor for synthesis of ethylene oxide, ethylene dichloride, ethylbenzene, and so on [2–5]. Traditionally, ethylene is obtained from the thermal catalytic cracking of petroleum and natural gas upon an endothermic reaction requiring high temperatures (600°C–1000°C) [2]. Since petroleum is nonrenewable resource, the new suitable way to produce ethylene from renewable resource is considered [6]. Hence, the dehydration of ethanol has been considered as a promising alternative approach to produce ethylene instead of using petroleum as feedstock.Dehydration of ethanol over solid acid catalysts requires lower temperature compared to the thermal cracking, leading to the reduction of energy cost. Therefore, many researchers have developed the ethanol dehydration for producing ethylene using solid catalysts. The main product from this reaction is ethylene, whereas diethyl ether, acetaldehyde, and light olefins are byproducts. The acid nature of solid catalyst has direct influence on the dehydration activity. The common solid catalysts such as zeolites [2, 7, 8] and alumina (Al2O3) [3, 9] have been applied to study the effect of acidity of catalyst on the dehydration ability. Lu et al. (2011) [7] found that HZSM-5 zeolite catalyst exhibits the highest selectivity of ethylene when it was carried out at low temperature (200°C–300°C). However, HZSM-5 zeolites have too high acidity, which can be rapidly deactivated by coke formation. The formation of coke on the catalyst causes lower stability. Previous works have been reported that acidity not only strongly affected the dehydration ability but also influenced the reaction stability of catalyst. For γ-Al2O3 catalyst, the dehydration reaction must be applied at higher temperature (400–450°C) to achieve high activity. Therefore, many attempts have been tried to modify γ-Al2O3 by adding metal oxide on solid support such as iron oxide and titanium oxide [10, 11]. Chen et al. (2007) [11] found that the modification of γ-Al2O3 with TiO2 can improve acidity. The conversion of ethanol is reached to 99.96%, whereas ethylene selectivity is about 99.4% at 440°C. Although the modified γ-Al2O3 catalyst required higher temperature than HZSM-5 zeolite catalyst, it is easy to synthesize and the stability of modified γ-Al2O3 catalyst is better.γ-Al2O3 catalyst is interesting because of its excellent thermal stability, fine particle size, high surface area, and side reaction inhibition. Khom-in et al. (2008) [12] studied the synthesis of mixed γ- and χ-phase Al2O3 catalysts and applied for methanol dehydration. They reported that the acidity of mixed γ- and χ-phase Al2O3 is higher than γ-Al2O3 and χ-Al2O3 [13, 14]. The mixed γ- and χ-phase Al2O3 catalysts can be directly synthesized via solvothermal method by using the suitable solvent in order to control structures, grain sizes, and morphologies by varying process conditions. In this research, we focused on the development of the alumina-based solid acid catalysts for ethanol dehydration. The catalysts were synthesized, characterized, and tested at a specified reaction condition. The synthesis parameters, such as calcination temperature and Mo modification influencing dehydration reaction, were varied in order to explore the suitable catalysts for ethanol dehydration.


## 2. Experimental

### 2.1. Preparation of Mixed Phase Alumina Catalyst

The mixedγ- and χ-crystalline phase alumina (M-Al) were prepared by the solvothermal method as reported by Janlamool and Jongsomjit [15]. The obtained powders were calcined in a tube furnace at different temperatures including 400°C (M-Al-400), 600°C (M-Al-600), 800°C (M-Al-800), and 1000°C (M-Al-1000) with a heating rate of 10°C/min in air for 6 h.


### 2.2. Preparation of Mo-Modified M-Al Catalysts

The Mo-modified M-Al catalysts were prepared by impregnation of the mixed phase alumina with an aqueous solution of ammonium heptamolybdate-tetrahydrate [(NH4)5Mo7O34·4H2O] with various loadings of Mo (5, 10, 15, and 20 wt%). The procedure for preparation catalyst as mentioned above was calculated based on 1 g of catalyst used. First, ammonium heptamolybdate-tetrahydrate was dissolved in 0.6 mL of deionized water. Then, the solution was added dropwise into approximately 1 g of dried solid catalyst. The obtained catalyst was dried in air at room temperature for 24 h, dried in oven at 110°C for 6 h, and calcined in air at 500°C for 2 h.


### 2.3. Catalyst Characterization

#### 2.3.1. X-Ray Diffraction (XRD)

The X-ray diffraction (XRD) patterns relating to bulk crystal structure of the catalysts were determined by the SIEMENS D5000 X-ray diffractometer. The experiment was carried out using Cu Kα radiation source (λ = 1.54439 Å) with Ni filter in the 2θ range of 20 to 80° with a resolution of 0.02°.


#### 2.3.2. Nitrogen Physisorption

The BET surface area, pore volume, and pore diameter of catalysts were determined by nitrogen gas adsorption at liquid nitrogen temperature (−196°C) using Micromeritics ChemiSorb 2750 Pulse chemisorption system instrument.


#### 2.3.3. Transmission Electron Microscopy (TEM)

The morphology and crystallite size of all catalysts were observed by using JEOL-JEM 200CX transmission electron microscope operated at 100 kV.


#### 2.3.4. Temperature Programmed Adsorption (NH3-TPD)

The acid properties of catalysts were investigated by temperature-programmed desorption of ammonia (NH3-TPD) equipment using Micromeritics ChemiSorb 2750 Pulse Chemisorption System. 0.1 g of catalyst was loaded in a quartz tube and pretreated at 500°C under helium flow. The sample was saturated with 15% NH3/He. After saturation, the physisorbed ammonia was desorbed under helium gas flow about 30 min, and then it was heated from 40°C to 800°C at heating rate of 10°C/min.


### 2.4. Reaction Test

The dehydration of ethanol was carried out in a fixed-bed continuous flow reactor with an inner diameter of 7 mm. In the experiment, 0.05 g of catalyst was loaded into the reactor and pretreated in argon (50 mL/min) at 200°C for 1 h under atmospheric pressure. To start the reaction, ethanol was delivered by bubbling argon as a carrier gas through the saturator at 45°C to control the vapor pressure of ethanol with WHSV of 8.4 (gethanolgcat-1·h−1). The reaction was carried out in temperature ranging from 200°C to 400°C. The products were analyzed by a Shimadzu GC8A gas chromatograph with FID using capillary column (DB-5) at 150°C.


## 2.1. Preparation of Mixed Phase Alumina Catalyst

The mixedγ- and χ-crystalline phase alumina (M-Al) were prepared by the solvothermal method as reported by Janlamool and Jongsomjit [15]. The obtained powders were calcined in a tube furnace at different temperatures including 400°C (M-Al-400), 600°C (M-Al-600), 800°C (M-Al-800), and 1000°C (M-Al-1000) with a heating rate of 10°C/min in air for 6 h.


## 2.2. Preparation of Mo-Modified M-Al Catalysts

The Mo-modified M-Al catalysts were prepared by impregnation of the mixed phase alumina with an aqueous solution of ammonium heptamolybdate-tetrahydrate [(NH4)5Mo7O34·4H2O] with various loadings of Mo (5, 10, 15, and 20 wt%). The procedure for preparation catalyst as mentioned above was calculated based on 1 g of catalyst used. First, ammonium heptamolybdate-tetrahydrate was dissolved in 0.6 mL of deionized water. Then, the solution was added dropwise into approximately 1 g of dried solid catalyst. The obtained catalyst was dried in air at room temperature for 24 h, dried in oven at 110°C for 6 h, and calcined in air at 500°C for 2 h.


## 2.3. Catalyst Characterization

### 2.3.1. X-Ray Diffraction (XRD)

The X-ray diffraction (XRD) patterns relating to bulk crystal structure of the catalysts were determined by the SIEMENS D5000 X-ray diffractometer. The experiment was carried out using Cu Kα radiation source (λ = 1.54439 Å) with Ni filter in the 2θ range of 20 to 80° with a resolution of 0.02°.


### 2.3.2. Nitrogen Physisorption

The BET surface area, pore volume, and pore diameter of catalysts were determined by nitrogen gas adsorption at liquid nitrogen temperature (−196°C) using Micromeritics ChemiSorb 2750 Pulse chemisorption system instrument.


### 2.3.3. Transmission Electron Microscopy (TEM)

The morphology and crystallite size of all catalysts were observed by using JEOL-JEM 200CX transmission electron microscope operated at 100 kV.


### 2.3.4. Temperature Programmed Adsorption (NH3-TPD)

The acid properties of catalysts were investigated by temperature-programmed desorption of ammonia (NH3-TPD) equipment using Micromeritics ChemiSorb 2750 Pulse Chemisorption System. 0.1 g of catalyst was loaded in a quartz tube and pretreated at 500°C under helium flow. The sample was saturated with 15% NH3/He. After saturation, the physisorbed ammonia was desorbed under helium gas flow about 30 min, and then it was heated from 40°C to 800°C at heating rate of 10°C/min.


## 2.3.1. X-Ray Diffraction (XRD)

The X-ray diffraction (XRD) patterns relating to bulk crystal structure of the catalysts were determined by the SIEMENS D5000 X-ray diffractometer. The experiment was carried out using Cu Kα radiation source (λ = 1.54439 Å) with Ni filter in the 2θ range of 20 to 80° with a resolution of 0.02°.


## 2.3.2. Nitrogen Physisorption

The BET surface area, pore volume, and pore diameter of catalysts were determined by nitrogen gas adsorption at liquid nitrogen temperature (−196°C) using Micromeritics ChemiSorb 2750 Pulse chemisorption system instrument.


## 2.3.3. Transmission Electron Microscopy (TEM)

The morphology and crystallite size of all catalysts were observed by using JEOL-JEM 200CX transmission electron microscope operated at 100 kV.


## 2.3.4. Temperature Programmed Adsorption (NH3-TPD)

The acid properties of catalysts were investigated by temperature-programmed desorption of ammonia (NH3-TPD) equipment using Micromeritics ChemiSorb 2750 Pulse Chemisorption System. 0.1 g of catalyst was loaded in a quartz tube and pretreated at 500°C under helium flow. The sample was saturated with 15% NH3/He. After saturation, the physisorbed ammonia was desorbed under helium gas flow about 30 min, and then it was heated from 40°C to 800°C at heating rate of 10°C/min.


## 2.4. Reaction Test

The dehydration of ethanol was carried out in a fixed-bed continuous flow reactor with an inner diameter of 7 mm. In the experiment, 0.05 g of catalyst was loaded into the reactor and pretreated in argon (50 mL/min) at 200°C for 1 h under atmospheric pressure. To start the reaction, ethanol was delivered by bubbling argon as a carrier gas through the saturator at 45°C to control the vapor pressure of ethanol with WHSV of 8.4 (gethanolgcat-1·h−1). The reaction was carried out in temperature ranging from 200°C to 400°C. The products were analyzed by a Shimadzu GC8A gas chromatograph with FID using capillary column (DB-5) at 150°C.


## 3. Results and Discussion

### 3.1. Effect of Calcination Temperature

#### 3.1.1. Characteristics

The mixed phase alumina catalysts, calcined at different temperatures, were confirmed by XRD results (Figure1). It was found that the XRD patterns of M-Al-400, M-Al-500, M-Al-600, M-Al-700, M-Al-800, and M-Al-900 (calcined at 400°C to 900°C) were similar. These patterns indicated the presence of γ-crystalline (32°, 37°, 39°, 45°, 61°, and 66°) and χ-crystalline (37°, 40°, 43°, 46°, 60°, and 67°) phases of alumina [12]. However, the M-Al-1000 catalyst (calcined at 1000°C) exhibits the different XRD pattern due to phase transformation to delta and theta phases [16].Figure 1
XRD patterns of mixedγ- and χ-crystalline phase alumina catalysts with various calcination temperatures; (○) gamma-alumina, (●) chi-alumina, (□) theta-alumina, and (■) delta-alumina.BET surface area, pore volume, and pore size diameter of catalysts with various calcination temperatures are summarized in Table1. The BET surface area slightly decreased with increasing calcination temperature. Surface area decreased from 233 to 144 m2/g with calcination temperature from 400°C to 1000°C. The pore volume of alumina catalysts seems to be constant with an increase in the calcination temperature. The M-Al-600 shows the highest pore volume (0.57 cm3/g). All catalysts exhibited increased pore size diameter from 5.9 to 9.1 nm with increasing calcination temperature. It is suggested that an increase in calcination temperature aggregated the catalyst resulting in losing the surface area, increasing the pore sizes diameter, and decreasing the pore volume.Table 1
BET surface area, pore volume, and pore size diameter of the mixedγ- and χ-crystalline phase alumina.
Sample BET surface area (m2/g) Pore volume (cm3/g) Pore size diameter (nm) M-Al-400 233 0.53 5.94 M-Al-500 191 0.54 7.29 M-Al-600 187 0.57 8.09 M-Al-700 157 0.51 8.39 M-Al-800 149 0.51 8.51 M-Al-900 142 0.49 8.98 M-Al-1000 114 0.42 9.41From the previous work, it was suggested that an increase of calcination temperature insignificantly affects the morphologies of mixedγ- and χ-crystalline phase alumina catalysts. However, Pansanga et al. [13] reported the morphology of mixed phase alumina, which was obtained by transmission electron microscopy (TEM) technique. They found that the morphology of alumina with different phases presented different structure. The morphologies of mixed γ- and χ-crystalline-phase alumina exhibited wrinkled sheets and spherical particles of γ- and χ-crystalline phase alumina, respectively.Figure2 shows the TEM micrographs of the M-Al-400 and M-Al-1000. It confirms that the obtained catalysts contain the mixed γ- and χ-crystalline-phase alumina indicating wrinkled sheets and spherical particles, according to Pansanga et al. [13]. The calcination temperature significantly affects the phase transformation as seen from XRD and TEM. Figure 2(a) shows two types of morphologies, which is mixed phase of γ- and χ-alumina calcined at 400°C. When the calcination temperature was increased to 1000°C, XRD suggested that the phase transformation occurred. It was proven by TEM as seen in Figure 2(b) that it appears as spherical particles and scarcely wrinkled sheets. It is suggested that the wrinkled sheets (γ-phase alumina) were transformed to other phase, while the spherical particles (χ-phase alumina) remain unchanged. It is in good agreement with the XRD result as seen for the peaks of M-Al-1000 at 43°. This indicated that χ-phase alumina was still observed. On the other hand, the peaks of γ-phase alumina were observed differently.Figure 2
TEM micrographs of the (a) M-Al-400 and (b) M-Al-1000.
(a) (b)The total acidity was significantly decreased with increasing the calcination temperature (Table2). This is because the hydroxyl group on catalyst surface was released with increasing the calcination temperature, leading to lower acidity. Besides, the total acidity can be divided into two types of acidic sites: weak acid sites and medium to strong acid sites. For weak acid sites, the position of weak acid sites exhibited the amount of NH3 desorption in the range from 215 to 109 μmol NH3/g cat. The M-Al-400 exhibited the highest acidity. However, the position of medium to strong acid sites was presented in the range from 705 to 337 μmol NH3/g cat.Table 2
The amount of acidity of mixedγ- and χ-crystalline-phase alumina catalysts with various calcination temperatures.
Sample NH3 desorption (µmol NH3/g cat.) Total acidity (µmol NH3/g cat.) Weak Medium to strong M-Al-400 215 489 705 M-Al-500 195 494 689 M-Al-600 148 513 661 M-Al-700 155 387 542 M-Al-800 109 364 473 M-Al-900 172 230 402 M-Al-1000 146 191 337


#### 3.1.2. Reaction Study

The catalytic performance of all catalysts was tested in ethanol dehydration. The reaction was carried out in the temperature ranging from 200°C to 400°C. The catalytic activity depends on the operating temperature, according to previous reports [7, 8, 10]. The results of catalytic activity were reported in terms of conversion and selectivity versus temperature profile. Besides the operating temperature, the catalyst acidity is an important factor influencing the conversion and selectivity of ethanol.The acidity results are summarized in Table2. The M-Al-600 exhibited the highest medium to strong acidity, followed by the M-Al-500 and M-Al-400. This result is in agreement with the previous report [17], in which the dehydration of ethanol over acid catalyst was studied and it was found that the products of ethanol dehydration reaction are ethylene (main product), diethyl ether, and acetaldehyde. The ethylene formation is favored by medium to strong acid sites, whereas diethyl ether requires only weak acid sites. At low temperature, diethyl ether is the major product, while, at high temperature, ethylene prevails. For the M-Al-1000, it exhibited the lowest medium to strong acidity.The ethanol conversion increased with increasing reaction temperature (Figure3). Similar trend was observed for all catalysts. The M-Al-400, M-Al-500, and M-Al-600 catalysts showed good performance with near complete ethanol conversion. However, at temperature higher than 400°C, deactivation can occur and products can be further converted to other products [16]. Considering the relationship between acidity and ethanol conversion, it was found that the medium to strong acidity plays an important role in the ethanol conversion. At high temperature, the selectivity of ethylene for all catalysts was higher than that at low temperature as shown in Figure 4.Figure 3
Ethanol conversion profiles in ethanol dehydration at different temperatures.Figure 4
Selectivity of ethylene profiles in ethanol dehydration at different temperatures.On the contrary, the selectivity of diethyl ether apparently decreased with increasing temperature as seen in Figure5. This result can be ascribed by thermodynamic properties. The reaction of ethanol to ethylene is endothermic reaction. Thus, it requires high temperature. On the other hand, the reaction of ethanol to diethyl ether is exothermic reaction; therefore diethyl ether is favored at the lower temperature. For the selectivity of acetaldehyde, it is presented in Figure 6. It was found that acetaldehyde selectivity was almost similar for all catalysts except for the M-Al-900 and M-Al-1000. In summary, the M-Al-600 catalyst shows the highest ethanol conversion (99.98%) and ethylene selectivity of 98.76% at 350°C having the ethylene yield of 98.75% (Table 3) at this temperature.Table 3
The yield of ethylene of M-Al-600 catalyst.
Reaction temperature (°C) Ethanol conversion (%) Ethylene selectivity (%) Ethylene yield (%) 200 64.38 78.65 50.63 250 93.68 92.59 86.74 300 99.74 98.67 98.41 350 99.98 98.76 98.75 400 100.00 95.57 98.57Figure 5
Selectivity of diethyl ether profiles in ethanol dehydration at different temperatures.Figure 6
Selectivity of acetaldehyde profiles in ethanol dehydration at different temperatures.


### 3.2. Effect of Mo Modification

#### 3.2.1. Characteristics

X-ray diffraction patterns of Mo-modified M-Al-600 catalyst are shown in Figure7. It can be seen for 5Mo/M-Al-600 and 10Mo/M-Al-600 that no distinguishable peaks of Mo species were observed in XRD patterns. Only XRD peaks for the mixed γ- and χ-crystalline-phase alumina were observed. It indicates that, at low Mo loading (<10 wt%), Mo was well dispersed on alumina surface. The sample with high amount of Mo (15 wt%–20 wt%), showed XRD peaks at 2θ of 27.3°, 25.7°, and 23.3°, which are characteristics of MoO3 [12]. The intensity of the diffraction peak can be attributed to an increase of MoO3 species indicating the formation of crystalline MoO3 on alumina surface.Figure 7
XRD patterns of mixedγ- and χ-crystalline phase alumina, MoO3-modified alumina, and MoO3.BET surface area, pore volume, and pore size diameter of Mo-modified catalysts are summarized in Table4. The BET surface area and pore volume were decreased with an increase of MoO3 loading. This may be due to the accumulation of the MoO3 on alumina surface. Although the 5Mo/M-Al-600 and 10Mo/M-Al-600 did not reveal the MoO3 species, the BET surface area, pore volume, and pore size diameter of both catalysts were decreased. In addition, from Table 4, the impregnation with MoO3 apparently lowered BET surface area and pore volume of support but did not significantly change the porous structure. The reduction of surface area was caused by blockage of smaller pore by MoO3 particles, while it did not affect the larger pore. As a result, the average pore size diameter of modified catalyst was not significantly changed. It was in the range of 6.74 to 7.20 nm. This indicated that, at lower loading, MoO3 was well dispersed on the support surface probably as the monolayer [18]. However, at higher MoO3 loading (20Mo/M-Al-600), the decrease of the BET surface area and pore volume because the formation of MoO3 crystallites obstructs the small pores and/or surface of catalysts is clearly seen. The pore size diameter of modified catalyst was in the range of 6.74 to 7.20 nm, which was lower than M-Al-600. This result is due to the covering of MoO3 crystallites on surface and pore of catalysts.Table 4
BET surface area, pore volume, and pore size diameter of the MoO3-modified catalysts.
Sample BET surface area (m2/g) Pore volume (cm3/g) Pore size diameter (nm) M-Al-600 187 0.57 8.09 5Mo/M-Al-600 185 0.45 6.88 10Mo/M-Al-600 164 0.43 7.20 15Mo/M-Al-600 134 0.35 7.12 20Mo/M-Al-600 131 0.35 6.74The total acidity was enhanced explicitly with an increase in the MoO3 loading (Table 5), especially the medium to strong acid sites (634 μmol NH3/g cat. for the 5Mo/M-Al-600 compared to 851 μmol NH3/g cat. for the 20Mo/M-Al-600). This is suggested that the addition of MoO3 has a significant effect on the acidity of the mixed phase alumina catalysts. Although, the increased acidity with the MoO3 loading cannot be identified in terms of Lewis and Brønsted acidity, Heracleous et al. [19] suggested that the new acid sites generated from the introduction of Mo are of Brønsted species, while only Lewis acid sites were identified on the alumina support [20–22].Table 5
The amount of acidity of MoO3-modified catalysts.
Sample NH3 desorption  (µmol NH3/g cat.) Total acidity (µmol NH3/g cat.) Weak Medium to strong M-Al-600 148 513 661 5Mo/M-Al-600 289 634 923 10Mo/M-Al-600 249 727 977 15Mo/M-Al-600 220 795 1015 20Mo/M-Al-600 263 851 1114


#### 3.2.2. Reaction Study

The Mo-modified M-Al-600 catalysts with various Mo loadings were tested in ethanol dehydration reaction. The ethanol conversion over different catalysts is shown in Figure8. It displays the similar trend to the ethanol conversion of the M-Al-600, where it increased with increasing operating temperatures. When comparing the Mo-modified alumina series with the unmodified catalysts (M-Al-600), it was found that the ethanol conversion of modified alumina was lower than that of the M-Al-600, although the modified alumina had more amount of acidity than the M-Al-600 catalyst. The reason why the higher total acidity did not render high ethanol conversion can be proposed upon Scheme 1. From Scheme 1, it is assumed that the acid site converts the ethanol molecule faster than the Mo site resulting in ethanol consumption of 1 > 2. The catalysts without MoO3 consist of acid sites acting as active phase on surface, while, for the Mo-modified catalysts, some acid sites had taken place by MoO3. Thus, the surface of catalysts actually contains two types of active phase (acid sites and Mo sites). According to previous study, it suggests that the acid site plays an important role for the dehydration reaction (ethanol to ethylene and diethyl ether). Ethanol was consumed very fast by acid site. In contrast, the Mo sites dominantly acted as the active site for dehydrogenation of ethanol to acetaldehyde. The rate of ethanol consumption was slower than the acid site.Scheme 1
Ethanol consumption phenomena on active site.Figure 8
Ethanol conversion profiles in ethanol dehydration of the MoO3 over mixed γ- and χ-crystalline phase alumina catalysts.As mentioned above, the ethanol conversion of modified catalyst would be causes from the Mo site. To confirm the rate of ethanol consumption by acid site and Mo site, the turnover frequency (TOF) or turnover number, which describes in the number of molecules reacting per active site per time, was calculated as shown in Table6.Table 6
Turnover frequency of the acid and Mo sites.
Turnover frequency (s-1) A c i d  s i t e s a M o  s i t e s b 84.4 4.70 × 10 - 3 B a s e d   a on dehydration reaction of ethanol to ethylene of the M-Al-600 at 200°C. B a s e d   b on dehydrogenation reaction of ethanol to acetaldehyde of the 5Mo/M-Al-600 at 200°C.As seen in Table6, the TOF of acid site was 84.4 s−1. It means that the 84.4 ethanol molecules were converted to ethylene on each acid site per second. However, only 4.70×10-3 molecules of ethanol are converted to acetaldehyde on each Mo site per second. The TOF of acid sites was higher than that of Mo sites. Therefore, when the MoO3 was added, the acid site and generated new sites (Mo sites) were formed in catalyst. The Mo slowly converted the ethanol molecule resulting in decreasing of overall ethanol consumption.The selectivity of ethylene, diethyl ether, and acetaldehyde of all catalysts is shown in Figures9–11, respectively. Both ethylene and diethyl ether selectivity showed the similar trend as seen from M-Al-600 catalysts. Ethylene favors high temperature, whereas diethyl ether requires lower temperature. An enhancement in acetaldehyde selectivity was observed with introduction of MoO3. The increase in selectivity of acetaldehyde was due to the fact that Mo species promoted dehydrogenation pathway. The MoO3 added into the mixed phase alumina substituted the acid sites on catalyst surface, resulting in formation of new sites. This result is corresponding to the NH3-TPD data, which explained that the acidity on surface of catalysts consists of two types (conventional acid sites and new sites from Mo species). Ethylene and diethyl ether were produced from the conventional acid sites on catalyst surface, whereas the acetaldehyde results from dehydrogenation reaction generated from Mo species.Figure 9
Selectivity of ethylene profiles in ethanol dehydration at different temperatures.Figure 10
Selectivity of diethyl ether profiles in ethanol dehydration at different temperatures.Figure 11
Selectivity of acetaldehyde profiles in ethanol dehydration at different temperatures.The selectivity of ethylene was decreased with an increase of Mo loading as shown in Figure9. In contrast, the selectivity of acetaldehyde was increased with an increase of Mo loading as shown in Figure 10. Although the 20Mo/M-Al-600 exhibits higher amount of the MoO3 than the 15Mo/M-Al-600, the selectivity of ethylene is not the lowest or the selectivity of acetaldehyde is not the highest. This was due to the fact that accumulation in catalyst pores was observed when Mo loading is more than 15 wt%. Thus, it leads to loss of Mo species. For the selectivity of ethylene, the 5Mo/M-Al-600 exhibited the highest ethylene selectivity (88.85% selectivity of ethylene at 350°C). However, it was lower compared to the M-Al-600 (98.76% selectivity of ethylene at 350°C). The 15Mo/M-Al-600 had the highest selectivity of acetaldehyde and the selectivity of acetaldehyde was enhanced up to 56.35% at 200°C. In order to compare the catalyst performance in this study with other researches, the ethanol conversion and ethylene yield of various catalysts are summarized in Table 7. It was found that the mixed phase alumina (M-Al-600) is quite competitive among other catalysts and promising for further study in ethanol dehydration to ethylene.Table 7
Comparison of catalytic activity of various catalysts for ethanol dehydration to ethylene.
Catalyst Reaction temperature(°C) Ethanol conversion(%) Ethylene yield(%) Ref. M-Al-600 350 99.98 98.75 This work 5Mo/M-Al-600 300 97.64 86.75 This work Fe/Al2O3 350 75.2 34.29 [9] Fe2O3 350 82.18 28.76 [10] Mn2O3 350 68.16 15.00 [10] Fe2O3/Mn2O3 (1 : 1) 350 76.00 30.40 [10] TiO2/γ-Al2O3 (microreactor) 360–550 95–99.96 91–99.30 [11] SiO2 350 2.5 0.89 [23] MgO-Al2O3 350 11.2 4.62 [23] ZrO2 350 45.4 36.00 [23] TiO2 350 80.1 11.29 [23] Commercial Al2O3 450 85 66.90 [24]


## 3.1. Effect of Calcination Temperature

### 3.1.1. Characteristics

The mixed phase alumina catalysts, calcined at different temperatures, were confirmed by XRD results (Figure1). It was found that the XRD patterns of M-Al-400, M-Al-500, M-Al-600, M-Al-700, M-Al-800, and M-Al-900 (calcined at 400°C to 900°C) were similar. These patterns indicated the presence of γ-crystalline (32°, 37°, 39°, 45°, 61°, and 66°) and χ-crystalline (37°, 40°, 43°, 46°, 60°, and 67°) phases of alumina [12]. However, the M-Al-1000 catalyst (calcined at 1000°C) exhibits the different XRD pattern due to phase transformation to delta and theta phases [16].Figure 1
XRD patterns of mixedγ- and χ-crystalline phase alumina catalysts with various calcination temperatures; (○) gamma-alumina, (●) chi-alumina, (□) theta-alumina, and (■) delta-alumina.BET surface area, pore volume, and pore size diameter of catalysts with various calcination temperatures are summarized in Table1. The BET surface area slightly decreased with increasing calcination temperature. Surface area decreased from 233 to 144 m2/g with calcination temperature from 400°C to 1000°C. The pore volume of alumina catalysts seems to be constant with an increase in the calcination temperature. The M-Al-600 shows the highest pore volume (0.57 cm3/g). All catalysts exhibited increased pore size diameter from 5.9 to 9.1 nm with increasing calcination temperature. It is suggested that an increase in calcination temperature aggregated the catalyst resulting in losing the surface area, increasing the pore sizes diameter, and decreasing the pore volume.Table 1
BET surface area, pore volume, and pore size diameter of the mixedγ- and χ-crystalline phase alumina.
Sample BET surface area (m2/g) Pore volume (cm3/g) Pore size diameter (nm) M-Al-400 233 0.53 5.94 M-Al-500 191 0.54 7.29 M-Al-600 187 0.57 8.09 M-Al-700 157 0.51 8.39 M-Al-800 149 0.51 8.51 M-Al-900 142 0.49 8.98 M-Al-1000 114 0.42 9.41From the previous work, it was suggested that an increase of calcination temperature insignificantly affects the morphologies of mixedγ- and χ-crystalline phase alumina catalysts. However, Pansanga et al. [13] reported the morphology of mixed phase alumina, which was obtained by transmission electron microscopy (TEM) technique. They found that the morphology of alumina with different phases presented different structure. The morphologies of mixed γ- and χ-crystalline-phase alumina exhibited wrinkled sheets and spherical particles of γ- and χ-crystalline phase alumina, respectively.Figure2 shows the TEM micrographs of the M-Al-400 and M-Al-1000. It confirms that the obtained catalysts contain the mixed γ- and χ-crystalline-phase alumina indicating wrinkled sheets and spherical particles, according to Pansanga et al. [13]. The calcination temperature significantly affects the phase transformation as seen from XRD and TEM. Figure 2(a) shows two types of morphologies, which is mixed phase of γ- and χ-alumina calcined at 400°C. When the calcination temperature was increased to 1000°C, XRD suggested that the phase transformation occurred. It was proven by TEM as seen in Figure 2(b) that it appears as spherical particles and scarcely wrinkled sheets. It is suggested that the wrinkled sheets (γ-phase alumina) were transformed to other phase, while the spherical particles (χ-phase alumina) remain unchanged. It is in good agreement with the XRD result as seen for the peaks of M-Al-1000 at 43°. This indicated that χ-phase alumina was still observed. On the other hand, the peaks of γ-phase alumina were observed differently.Figure 2
TEM micrographs of the (a) M-Al-400 and (b) M-Al-1000.
(a) (b)The total acidity was significantly decreased with increasing the calcination temperature (Table2). This is because the hydroxyl group on catalyst surface was released with increasing the calcination temperature, leading to lower acidity. Besides, the total acidity can be divided into two types of acidic sites: weak acid sites and medium to strong acid sites. For weak acid sites, the position of weak acid sites exhibited the amount of NH3 desorption in the range from 215 to 109 μmol NH3/g cat. The M-Al-400 exhibited the highest acidity. However, the position of medium to strong acid sites was presented in the range from 705 to 337 μmol NH3/g cat.Table 2
The amount of acidity of mixedγ- and χ-crystalline-phase alumina catalysts with various calcination temperatures.
Sample NH3 desorption (µmol NH3/g cat.) Total acidity (µmol NH3/g cat.) Weak Medium to strong M-Al-400 215 489 705 M-Al-500 195 494 689 M-Al-600 148 513 661 M-Al-700 155 387 542 M-Al-800 109 364 473 M-Al-900 172 230 402 M-Al-1000 146 191 337


### 3.1.2. Reaction Study

The catalytic performance of all catalysts was tested in ethanol dehydration. The reaction was carried out in the temperature ranging from 200°C to 400°C. The catalytic activity depends on the operating temperature, according to previous reports [7, 8, 10]. The results of catalytic activity were reported in terms of conversion and selectivity versus temperature profile. Besides the operating temperature, the catalyst acidity is an important factor influencing the conversion and selectivity of ethanol.The acidity results are summarized in Table2. The M-Al-600 exhibited the highest medium to strong acidity, followed by the M-Al-500 and M-Al-400. This result is in agreement with the previous report [17], in which the dehydration of ethanol over acid catalyst was studied and it was found that the products of ethanol dehydration reaction are ethylene (main product), diethyl ether, and acetaldehyde. The ethylene formation is favored by medium to strong acid sites, whereas diethyl ether requires only weak acid sites. At low temperature, diethyl ether is the major product, while, at high temperature, ethylene prevails. For the M-Al-1000, it exhibited the lowest medium to strong acidity.The ethanol conversion increased with increasing reaction temperature (Figure3). Similar trend was observed for all catalysts. The M-Al-400, M-Al-500, and M-Al-600 catalysts showed good performance with near complete ethanol conversion. However, at temperature higher than 400°C, deactivation can occur and products can be further converted to other products [16]. Considering the relationship between acidity and ethanol conversion, it was found that the medium to strong acidity plays an important role in the ethanol conversion. At high temperature, the selectivity of ethylene for all catalysts was higher than that at low temperature as shown in Figure 4.Figure 3
Ethanol conversion profiles in ethanol dehydration at different temperatures.Figure 4
Selectivity of ethylene profiles in ethanol dehydration at different temperatures.On the contrary, the selectivity of diethyl ether apparently decreased with increasing temperature as seen in Figure5. This result can be ascribed by thermodynamic properties. The reaction of ethanol to ethylene is endothermic reaction. Thus, it requires high temperature. On the other hand, the reaction of ethanol to diethyl ether is exothermic reaction; therefore diethyl ether is favored at the lower temperature. For the selectivity of acetaldehyde, it is presented in Figure 6. It was found that acetaldehyde selectivity was almost similar for all catalysts except for the M-Al-900 and M-Al-1000. In summary, the M-Al-600 catalyst shows the highest ethanol conversion (99.98%) and ethylene selectivity of 98.76% at 350°C having the ethylene yield of 98.75% (Table 3) at this temperature.Table 3
The yield of ethylene of M-Al-600 catalyst.
Reaction temperature (°C) Ethanol conversion (%) Ethylene selectivity (%) Ethylene yield (%) 200 64.38 78.65 50.63 250 93.68 92.59 86.74 300 99.74 98.67 98.41 350 99.98 98.76 98.75 400 100.00 95.57 98.57Figure 5
Selectivity of diethyl ether profiles in ethanol dehydration at different temperatures.Figure 6
Selectivity of acetaldehyde profiles in ethanol dehydration at different temperatures.


## 3.1.1. Characteristics

The mixed phase alumina catalysts, calcined at different temperatures, were confirmed by XRD results (Figure1). It was found that the XRD patterns of M-Al-400, M-Al-500, M-Al-600, M-Al-700, M-Al-800, and M-Al-900 (calcined at 400°C to 900°C) were similar. These patterns indicated the presence of γ-crystalline (32°, 37°, 39°, 45°, 61°, and 66°) and χ-crystalline (37°, 40°, 43°, 46°, 60°, and 67°) phases of alumina [12]. However, the M-Al-1000 catalyst (calcined at 1000°C) exhibits the different XRD pattern due to phase transformation to delta and theta phases [16].Figure 1
XRD patterns of mixedγ- and χ-crystalline phase alumina catalysts with various calcination temperatures; (○) gamma-alumina, (●) chi-alumina, (□) theta-alumina, and (■) delta-alumina.BET surface area, pore volume, and pore size diameter of catalysts with various calcination temperatures are summarized in Table1. The BET surface area slightly decreased with increasing calcination temperature. Surface area decreased from 233 to 144 m2/g with calcination temperature from 400°C to 1000°C. The pore volume of alumina catalysts seems to be constant with an increase in the calcination temperature. The M-Al-600 shows the highest pore volume (0.57 cm3/g). All catalysts exhibited increased pore size diameter from 5.9 to 9.1 nm with increasing calcination temperature. It is suggested that an increase in calcination temperature aggregated the catalyst resulting in losing the surface area, increasing the pore sizes diameter, and decreasing the pore volume.Table 1
BET surface area, pore volume, and pore size diameter of the mixedγ- and χ-crystalline phase alumina.
Sample BET surface area (m2/g) Pore volume (cm3/g) Pore size diameter (nm) M-Al-400 233 0.53 5.94 M-Al-500 191 0.54 7.29 M-Al-600 187 0.57 8.09 M-Al-700 157 0.51 8.39 M-Al-800 149 0.51 8.51 M-Al-900 142 0.49 8.98 M-Al-1000 114 0.42 9.41From the previous work, it was suggested that an increase of calcination temperature insignificantly affects the morphologies of mixedγ- and χ-crystalline phase alumina catalysts. However, Pansanga et al. [13] reported the morphology of mixed phase alumina, which was obtained by transmission electron microscopy (TEM) technique. They found that the morphology of alumina with different phases presented different structure. The morphologies of mixed γ- and χ-crystalline-phase alumina exhibited wrinkled sheets and spherical particles of γ- and χ-crystalline phase alumina, respectively.Figure2 shows the TEM micrographs of the M-Al-400 and M-Al-1000. It confirms that the obtained catalysts contain the mixed γ- and χ-crystalline-phase alumina indicating wrinkled sheets and spherical particles, according to Pansanga et al. [13]. The calcination temperature significantly affects the phase transformation as seen from XRD and TEM. Figure 2(a) shows two types of morphologies, which is mixed phase of γ- and χ-alumina calcined at 400°C. When the calcination temperature was increased to 1000°C, XRD suggested that the phase transformation occurred. It was proven by TEM as seen in Figure 2(b) that it appears as spherical particles and scarcely wrinkled sheets. It is suggested that the wrinkled sheets (γ-phase alumina) were transformed to other phase, while the spherical particles (χ-phase alumina) remain unchanged. It is in good agreement with the XRD result as seen for the peaks of M-Al-1000 at 43°. This indicated that χ-phase alumina was still observed. On the other hand, the peaks of γ-phase alumina were observed differently.Figure 2
TEM micrographs of the (a) M-Al-400 and (b) M-Al-1000.
(a) (b)The total acidity was significantly decreased with increasing the calcination temperature (Table2). This is because the hydroxyl group on catalyst surface was released with increasing the calcination temperature, leading to lower acidity. Besides, the total acidity can be divided into two types of acidic sites: weak acid sites and medium to strong acid sites. For weak acid sites, the position of weak acid sites exhibited the amount of NH3 desorption in the range from 215 to 109 μmol NH3/g cat. The M-Al-400 exhibited the highest acidity. However, the position of medium to strong acid sites was presented in the range from 705 to 337 μmol NH3/g cat.Table 2
The amount of acidity of mixedγ- and χ-crystalline-phase alumina catalysts with various calcination temperatures.
Sample NH3 desorption (µmol NH3/g cat.) Total acidity (µmol NH3/g cat.) Weak Medium to strong M-Al-400 215 489 705 M-Al-500 195 494 689 M-Al-600 148 513 661 M-Al-700 155 387 542 M-Al-800 109 364 473 M-Al-900 172 230 402 M-Al-1000 146 191 337


## 3.1.2. Reaction Study

The catalytic performance of all catalysts was tested in ethanol dehydration. The reaction was carried out in the temperature ranging from 200°C to 400°C. The catalytic activity depends on the operating temperature, according to previous reports [7, 8, 10]. The results of catalytic activity were reported in terms of conversion and selectivity versus temperature profile. Besides the operating temperature, the catalyst acidity is an important factor influencing the conversion and selectivity of ethanol.The acidity results are summarized in Table2. The M-Al-600 exhibited the highest medium to strong acidity, followed by the M-Al-500 and M-Al-400. This result is in agreement with the previous report [17], in which the dehydration of ethanol over acid catalyst was studied and it was found that the products of ethanol dehydration reaction are ethylene (main product), diethyl ether, and acetaldehyde. The ethylene formation is favored by medium to strong acid sites, whereas diethyl ether requires only weak acid sites. At low temperature, diethyl ether is the major product, while, at high temperature, ethylene prevails. For the M-Al-1000, it exhibited the lowest medium to strong acidity.The ethanol conversion increased with increasing reaction temperature (Figure3). Similar trend was observed for all catalysts. The M-Al-400, M-Al-500, and M-Al-600 catalysts showed good performance with near complete ethanol conversion. However, at temperature higher than 400°C, deactivation can occur and products can be further converted to other products [16]. Considering the relationship between acidity and ethanol conversion, it was found that the medium to strong acidity plays an important role in the ethanol conversion. At high temperature, the selectivity of ethylene for all catalysts was higher than that at low temperature as shown in Figure 4.Figure 3
Ethanol conversion profiles in ethanol dehydration at different temperatures.Figure 4
Selectivity of ethylene profiles in ethanol dehydration at different temperatures.On the contrary, the selectivity of diethyl ether apparently decreased with increasing temperature as seen in Figure5. This result can be ascribed by thermodynamic properties. The reaction of ethanol to ethylene is endothermic reaction. Thus, it requires high temperature. On the other hand, the reaction of ethanol to diethyl ether is exothermic reaction; therefore diethyl ether is favored at the lower temperature. For the selectivity of acetaldehyde, it is presented in Figure 6. It was found that acetaldehyde selectivity was almost similar for all catalysts except for the M-Al-900 and M-Al-1000. In summary, the M-Al-600 catalyst shows the highest ethanol conversion (99.98%) and ethylene selectivity of 98.76% at 350°C having the ethylene yield of 98.75% (Table 3) at this temperature.Table 3
The yield of ethylene of M-Al-600 catalyst.
Reaction temperature (°C) Ethanol conversion (%) Ethylene selectivity (%) Ethylene yield (%) 200 64.38 78.65 50.63 250 93.68 92.59 86.74 300 99.74 98.67 98.41 350 99.98 98.76 98.75 400 100.00 95.57 98.57Figure 5
Selectivity of diethyl ether profiles in ethanol dehydration at different temperatures.Figure 6
Selectivity of acetaldehyde profiles in ethanol dehydration at different temperatures.


## 3.2. Effect of Mo Modification

### 3.2.1. Characteristics

X-ray diffraction patterns of Mo-modified M-Al-600 catalyst are shown in Figure7. It can be seen for 5Mo/M-Al-600 and 10Mo/M-Al-600 that no distinguishable peaks of Mo species were observed in XRD patterns. Only XRD peaks for the mixed γ- and χ-crystalline-phase alumina were observed. It indicates that, at low Mo loading (<10 wt%), Mo was well dispersed on alumina surface. The sample with high amount of Mo (15 wt%–20 wt%), showed XRD peaks at 2θ of 27.3°, 25.7°, and 23.3°, which are characteristics of MoO3 [12]. The intensity of the diffraction peak can be attributed to an increase of MoO3 species indicating the formation of crystalline MoO3 on alumina surface.Figure 7
XRD patterns of mixedγ- and χ-crystalline phase alumina, MoO3-modified alumina, and MoO3.BET surface area, pore volume, and pore size diameter of Mo-modified catalysts are summarized in Table4. The BET surface area and pore volume were decreased with an increase of MoO3 loading. This may be due to the accumulation of the MoO3 on alumina surface. Although the 5Mo/M-Al-600 and 10Mo/M-Al-600 did not reveal the MoO3 species, the BET surface area, pore volume, and pore size diameter of both catalysts were decreased. In addition, from Table 4, the impregnation with MoO3 apparently lowered BET surface area and pore volume of support but did not significantly change the porous structure. The reduction of surface area was caused by blockage of smaller pore by MoO3 particles, while it did not affect the larger pore. As a result, the average pore size diameter of modified catalyst was not significantly changed. It was in the range of 6.74 to 7.20 nm. This indicated that, at lower loading, MoO3 was well dispersed on the support surface probably as the monolayer [18]. However, at higher MoO3 loading (20Mo/M-Al-600), the decrease of the BET surface area and pore volume because the formation of MoO3 crystallites obstructs the small pores and/or surface of catalysts is clearly seen. The pore size diameter of modified catalyst was in the range of 6.74 to 7.20 nm, which was lower than M-Al-600. This result is due to the covering of MoO3 crystallites on surface and pore of catalysts.Table 4
BET surface area, pore volume, and pore size diameter of the MoO3-modified catalysts.
Sample BET surface area (m2/g) Pore volume (cm3/g) Pore size diameter (nm) M-Al-600 187 0.57 8.09 5Mo/M-Al-600 185 0.45 6.88 10Mo/M-Al-600 164 0.43 7.20 15Mo/M-Al-600 134 0.35 7.12 20Mo/M-Al-600 131 0.35 6.74The total acidity was enhanced explicitly with an increase in the MoO3 loading (Table 5), especially the medium to strong acid sites (634 μmol NH3/g cat. for the 5Mo/M-Al-600 compared to 851 μmol NH3/g cat. for the 20Mo/M-Al-600). This is suggested that the addition of MoO3 has a significant effect on the acidity of the mixed phase alumina catalysts. Although, the increased acidity with the MoO3 loading cannot be identified in terms of Lewis and Brønsted acidity, Heracleous et al. [19] suggested that the new acid sites generated from the introduction of Mo are of Brønsted species, while only Lewis acid sites were identified on the alumina support [20–22].Table 5
The amount of acidity of MoO3-modified catalysts.
Sample NH3 desorption  (µmol NH3/g cat.) Total acidity (µmol NH3/g cat.) Weak Medium to strong M-Al-600 148 513 661 5Mo/M-Al-600 289 634 923 10Mo/M-Al-600 249 727 977 15Mo/M-Al-600 220 795 1015 20Mo/M-Al-600 263 851 1114


### 3.2.2. Reaction Study

The Mo-modified M-Al-600 catalysts with various Mo loadings were tested in ethanol dehydration reaction. The ethanol conversion over different catalysts is shown in Figure8. It displays the similar trend to the ethanol conversion of the M-Al-600, where it increased with increasing operating temperatures. When comparing the Mo-modified alumina series with the unmodified catalysts (M-Al-600), it was found that the ethanol conversion of modified alumina was lower than that of the M-Al-600, although the modified alumina had more amount of acidity than the M-Al-600 catalyst. The reason why the higher total acidity did not render high ethanol conversion can be proposed upon Scheme 1. From Scheme 1, it is assumed that the acid site converts the ethanol molecule faster than the Mo site resulting in ethanol consumption of 1 > 2. The catalysts without MoO3 consist of acid sites acting as active phase on surface, while, for the Mo-modified catalysts, some acid sites had taken place by MoO3. Thus, the surface of catalysts actually contains two types of active phase (acid sites and Mo sites). According to previous study, it suggests that the acid site plays an important role for the dehydration reaction (ethanol to ethylene and diethyl ether). Ethanol was consumed very fast by acid site. In contrast, the Mo sites dominantly acted as the active site for dehydrogenation of ethanol to acetaldehyde. The rate of ethanol consumption was slower than the acid site.Scheme 1
Ethanol consumption phenomena on active site.Figure 8
Ethanol conversion profiles in ethanol dehydration of the MoO3 over mixed γ- and χ-crystalline phase alumina catalysts.As mentioned above, the ethanol conversion of modified catalyst would be causes from the Mo site. To confirm the rate of ethanol consumption by acid site and Mo site, the turnover frequency (TOF) or turnover number, which describes in the number of molecules reacting per active site per time, was calculated as shown in Table6.Table 6
Turnover frequency of the acid and Mo sites.
Turnover frequency (s-1) A c i d  s i t e s a M o  s i t e s b 84.4 4.70 × 10 - 3 B a s e d   a on dehydration reaction of ethanol to ethylene of the M-Al-600 at 200°C. B a s e d   b on dehydrogenation reaction of ethanol to acetaldehyde of the 5Mo/M-Al-600 at 200°C.As seen in Table6, the TOF of acid site was 84.4 s−1. It means that the 84.4 ethanol molecules were converted to ethylene on each acid site per second. However, only 4.70×10-3 molecules of ethanol are converted to acetaldehyde on each Mo site per second. The TOF of acid sites was higher than that of Mo sites. Therefore, when the MoO3 was added, the acid site and generated new sites (Mo sites) were formed in catalyst. The Mo slowly converted the ethanol molecule resulting in decreasing of overall ethanol consumption.The selectivity of ethylene, diethyl ether, and acetaldehyde of all catalysts is shown in Figures9–11, respectively. Both ethylene and diethyl ether selectivity showed the similar trend as seen from M-Al-600 catalysts. Ethylene favors high temperature, whereas diethyl ether requires lower temperature. An enhancement in acetaldehyde selectivity was observed with introduction of MoO3. The increase in selectivity of acetaldehyde was due to the fact that Mo species promoted dehydrogenation pathway. The MoO3 added into the mixed phase alumina substituted the acid sites on catalyst surface, resulting in formation of new sites. This result is corresponding to the NH3-TPD data, which explained that the acidity on surface of catalysts consists of two types (conventional acid sites and new sites from Mo species). Ethylene and diethyl ether were produced from the conventional acid sites on catalyst surface, whereas the acetaldehyde results from dehydrogenation reaction generated from Mo species.Figure 9
Selectivity of ethylene profiles in ethanol dehydration at different temperatures.Figure 10
Selectivity of diethyl ether profiles in ethanol dehydration at different temperatures.Figure 11
Selectivity of acetaldehyde profiles in ethanol dehydration at different temperatures.The selectivity of ethylene was decreased with an increase of Mo loading as shown in Figure9. In contrast, the selectivity of acetaldehyde was increased with an increase of Mo loading as shown in Figure 10. Although the 20Mo/M-Al-600 exhibits higher amount of the MoO3 than the 15Mo/M-Al-600, the selectivity of ethylene is not the lowest or the selectivity of acetaldehyde is not the highest. This was due to the fact that accumulation in catalyst pores was observed when Mo loading is more than 15 wt%. Thus, it leads to loss of Mo species. For the selectivity of ethylene, the 5Mo/M-Al-600 exhibited the highest ethylene selectivity (88.85% selectivity of ethylene at 350°C). However, it was lower compared to the M-Al-600 (98.76% selectivity of ethylene at 350°C). The 15Mo/M-Al-600 had the highest selectivity of acetaldehyde and the selectivity of acetaldehyde was enhanced up to 56.35% at 200°C. In order to compare the catalyst performance in this study with other researches, the ethanol conversion and ethylene yield of various catalysts are summarized in Table 7. It was found that the mixed phase alumina (M-Al-600) is quite competitive among other catalysts and promising for further study in ethanol dehydration to ethylene.Table 7
Comparison of catalytic activity of various catalysts for ethanol dehydration to ethylene.
Catalyst Reaction temperature(°C) Ethanol conversion(%) Ethylene yield(%) Ref. M-Al-600 350 99.98 98.75 This work 5Mo/M-Al-600 300 97.64 86.75 This work Fe/Al2O3 350 75.2 34.29 [9] Fe2O3 350 82.18 28.76 [10] Mn2O3 350 68.16 15.00 [10] Fe2O3/Mn2O3 (1 : 1) 350 76.00 30.40 [10] TiO2/γ-Al2O3 (microreactor) 360–550 95–99.96 91–99.30 [11] SiO2 350 2.5 0.89 [23] MgO-Al2O3 350 11.2 4.62 [23] ZrO2 350 45.4 36.00 [23] TiO2 350 80.1 11.29 [23] Commercial Al2O3 450 85 66.90 [24]


## 3.2.1. Characteristics

X-ray diffraction patterns of Mo-modified M-Al-600 catalyst are shown in Figure7. It can be seen for 5Mo/M-Al-600 and 10Mo/M-Al-600 that no distinguishable peaks of Mo species were observed in XRD patterns. Only XRD peaks for the mixed γ- and χ-crystalline-phase alumina were observed. It indicates that, at low Mo loading (<10 wt%), Mo was well dispersed on alumina surface. The sample with high amount of Mo (15 wt%–20 wt%), showed XRD peaks at 2θ of 27.3°, 25.7°, and 23.3°, which are characteristics of MoO3 [12]. The intensity of the diffraction peak can be attributed to an increase of MoO3 species indicating the formation of crystalline MoO3 on alumina surface.Figure 7
XRD patterns of mixedγ- and χ-crystalline phase alumina, MoO3-modified alumina, and MoO3.BET surface area, pore volume, and pore size diameter of Mo-modified catalysts are summarized in Table4. The BET surface area and pore volume were decreased with an increase of MoO3 loading. This may be due to the accumulation of the MoO3 on alumina surface. Although the 5Mo/M-Al-600 and 10Mo/M-Al-600 did not reveal the MoO3 species, the BET surface area, pore volume, and pore size diameter of both catalysts were decreased. In addition, from Table 4, the impregnation with MoO3 apparently lowered BET surface area and pore volume of support but did not significantly change the porous structure. The reduction of surface area was caused by blockage of smaller pore by MoO3 particles, while it did not affect the larger pore. As a result, the average pore size diameter of modified catalyst was not significantly changed. It was in the range of 6.74 to 7.20 nm. This indicated that, at lower loading, MoO3 was well dispersed on the support surface probably as the monolayer [18]. However, at higher MoO3 loading (20Mo/M-Al-600), the decrease of the BET surface area and pore volume because the formation of MoO3 crystallites obstructs the small pores and/or surface of catalysts is clearly seen. The pore size diameter of modified catalyst was in the range of 6.74 to 7.20 nm, which was lower than M-Al-600. This result is due to the covering of MoO3 crystallites on surface and pore of catalysts.Table 4
BET surface area, pore volume, and pore size diameter of the MoO3-modified catalysts.
Sample BET surface area (m2/g) Pore volume (cm3/g) Pore size diameter (nm) M-Al-600 187 0.57 8.09 5Mo/M-Al-600 185 0.45 6.88 10Mo/M-Al-600 164 0.43 7.20 15Mo/M-Al-600 134 0.35 7.12 20Mo/M-Al-600 131 0.35 6.74The total acidity was enhanced explicitly with an increase in the MoO3 loading (Table 5), especially the medium to strong acid sites (634 μmol NH3/g cat. for the 5Mo/M-Al-600 compared to 851 μmol NH3/g cat. for the 20Mo/M-Al-600). This is suggested that the addition of MoO3 has a significant effect on the acidity of the mixed phase alumina catalysts. Although, the increased acidity with the MoO3 loading cannot be identified in terms of Lewis and Brønsted acidity, Heracleous et al. [19] suggested that the new acid sites generated from the introduction of Mo are of Brønsted species, while only Lewis acid sites were identified on the alumina support [20–22].Table 5
The amount of acidity of MoO3-modified catalysts.
Sample NH3 desorption  (µmol NH3/g cat.) Total acidity (µmol NH3/g cat.) Weak Medium to strong M-Al-600 148 513 661 5Mo/M-Al-600 289 634 923 10Mo/M-Al-600 249 727 977 15Mo/M-Al-600 220 795 1015 20Mo/M-Al-600 263 851 1114


## 3.2.2. Reaction Study

The Mo-modified M-Al-600 catalysts with various Mo loadings were tested in ethanol dehydration reaction. The ethanol conversion over different catalysts is shown in Figure8. It displays the similar trend to the ethanol conversion of the M-Al-600, where it increased with increasing operating temperatures. When comparing the Mo-modified alumina series with the unmodified catalysts (M-Al-600), it was found that the ethanol conversion of modified alumina was lower than that of the M-Al-600, although the modified alumina had more amount of acidity than the M-Al-600 catalyst. The reason why the higher total acidity did not render high ethanol conversion can be proposed upon Scheme 1. From Scheme 1, it is assumed that the acid site converts the ethanol molecule faster than the Mo site resulting in ethanol consumption of 1 > 2. The catalysts without MoO3 consist of acid sites acting as active phase on surface, while, for the Mo-modified catalysts, some acid sites had taken place by MoO3. Thus, the surface of catalysts actually contains two types of active phase (acid sites and Mo sites). According to previous study, it suggests that the acid site plays an important role for the dehydration reaction (ethanol to ethylene and diethyl ether). Ethanol was consumed very fast by acid site. In contrast, the Mo sites dominantly acted as the active site for dehydrogenation of ethanol to acetaldehyde. The rate of ethanol consumption was slower than the acid site.Scheme 1
Ethanol consumption phenomena on active site.Figure 8
Ethanol conversion profiles in ethanol dehydration of the MoO3 over mixed γ- and χ-crystalline phase alumina catalysts.As mentioned above, the ethanol conversion of modified catalyst would be causes from the Mo site. To confirm the rate of ethanol consumption by acid site and Mo site, the turnover frequency (TOF) or turnover number, which describes in the number of molecules reacting per active site per time, was calculated as shown in Table6.Table 6
Turnover frequency of the acid and Mo sites.
Turnover frequency (s-1) A c i d  s i t e s a M o  s i t e s b 84.4 4.70 × 10 - 3 B a s e d   a on dehydration reaction of ethanol to ethylene of the M-Al-600 at 200°C. B a s e d   b on dehydrogenation reaction of ethanol to acetaldehyde of the 5Mo/M-Al-600 at 200°C.As seen in Table6, the TOF of acid site was 84.4 s−1. It means that the 84.4 ethanol molecules were converted to ethylene on each acid site per second. However, only 4.70×10-3 molecules of ethanol are converted to acetaldehyde on each Mo site per second. The TOF of acid sites was higher than that of Mo sites. Therefore, when the MoO3 was added, the acid site and generated new sites (Mo sites) were formed in catalyst. The Mo slowly converted the ethanol molecule resulting in decreasing of overall ethanol consumption.The selectivity of ethylene, diethyl ether, and acetaldehyde of all catalysts is shown in Figures9–11, respectively. Both ethylene and diethyl ether selectivity showed the similar trend as seen from M-Al-600 catalysts. Ethylene favors high temperature, whereas diethyl ether requires lower temperature. An enhancement in acetaldehyde selectivity was observed with introduction of MoO3. The increase in selectivity of acetaldehyde was due to the fact that Mo species promoted dehydrogenation pathway. The MoO3 added into the mixed phase alumina substituted the acid sites on catalyst surface, resulting in formation of new sites. This result is corresponding to the NH3-TPD data, which explained that the acidity on surface of catalysts consists of two types (conventional acid sites and new sites from Mo species). Ethylene and diethyl ether were produced from the conventional acid sites on catalyst surface, whereas the acetaldehyde results from dehydrogenation reaction generated from Mo species.Figure 9
Selectivity of ethylene profiles in ethanol dehydration at different temperatures.Figure 10
Selectivity of diethyl ether profiles in ethanol dehydration at different temperatures.Figure 11
Selectivity of acetaldehyde profiles in ethanol dehydration at different temperatures.The selectivity of ethylene was decreased with an increase of Mo loading as shown in Figure9. In contrast, the selectivity of acetaldehyde was increased with an increase of Mo loading as shown in Figure 10. Although the 20Mo/M-Al-600 exhibits higher amount of the MoO3 than the 15Mo/M-Al-600, the selectivity of ethylene is not the lowest or the selectivity of acetaldehyde is not the highest. This was due to the fact that accumulation in catalyst pores was observed when Mo loading is more than 15 wt%. Thus, it leads to loss of Mo species. For the selectivity of ethylene, the 5Mo/M-Al-600 exhibited the highest ethylene selectivity (88.85% selectivity of ethylene at 350°C). However, it was lower compared to the M-Al-600 (98.76% selectivity of ethylene at 350°C). The 15Mo/M-Al-600 had the highest selectivity of acetaldehyde and the selectivity of acetaldehyde was enhanced up to 56.35% at 200°C. In order to compare the catalyst performance in this study with other researches, the ethanol conversion and ethylene yield of various catalysts are summarized in Table 7. It was found that the mixed phase alumina (M-Al-600) is quite competitive among other catalysts and promising for further study in ethanol dehydration to ethylene.Table 7
Comparison of catalytic activity of various catalysts for ethanol dehydration to ethylene.
Catalyst Reaction temperature(°C) Ethanol conversion(%) Ethylene yield(%) Ref. M-Al-600 350 99.98 98.75 This work 5Mo/M-Al-600 300 97.64 86.75 This work Fe/Al2O3 350 75.2 34.29 [9] Fe2O3 350 82.18 28.76 [10] Mn2O3 350 68.16 15.00 [10] Fe2O3/Mn2O3 (1 : 1) 350 76.00 30.40 [10] TiO2/γ-Al2O3 (microreactor) 360–550 95–99.96 91–99.30 [11] SiO2 350 2.5 0.89 [23] MgO-Al2O3 350 11.2 4.62 [23] ZrO2 350 45.4 36.00 [23] TiO2 350 80.1 11.29 [23] Commercial Al2O3 450 85 66.90 [24]


## 4. Conclusion

It reveals that the calcination temperature has significant effect on acidity of alumina catalysts. The acidity was decreased with increasing calcination temperature especially for medium to strong acid. Moreover, at 1000°C, the mixedγ- and χ-crystalline phase alumina catalysts exhibited significant phase transformation. γ-phase was transformed, while χ-phase remains stable. In the ethanol conversion reaction, both ethanol conversion and ethylene selectivity depend on medium to strong acid. In this study, the mixed γ- and χ-crystalline phase alumina catalyst, which was calcined at 600°C (M-Al-600), exhibited the highest catalytic activity. It shows the highest ethylene yield of 98.75% at 350°C. In addition, with Mo modification, it was found that enhancement of acetaldehyde was observed. However, it is proposed that the active site to produce acetaldehyde was much lower compared with those to produce ethylene.



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*Source: 5018384-2017-01-12.xml*