2.1. Prophase Research on n-Decane Hydrocracking
At the start of this study, the conversion of n-decane hydrocracking at different temperatures was evaluated over the Z–100 catalyst, as shown in
Figure 1. Zeolite ZSM-5 shows a good hydrocracking ability, especially at a higher temperature. As the temperature increases, zeolite ZSM-5 becomes more markedly active in the n-decane hydrocracking process. This indicates that it is thermodynamically advantageous at higher temperatures. The conversion of n-decane rises from 48.2% (300 °C) to 79.8% (400 °C). Zeolite ZSM-5 has a good stability and activity at a high temperature according to its specific structure. Hence, 400 °C is implemented as the reaction condition in the following research.
Then, three types of ZSM-5 zeolites with different Si/Al molar ratios are compared and evaluated in the n-decane hydrocracking reaction. The SiO2/Al2O3 ratio of the catalysts are 24, 100 and 1500, denoted as Z–24, Z–100 and Z–1500, respectively.
Figure 2 and
Table 1 show the conversion and selectivity of Z–24, Z–100 and Z–1500 in the n-decane cracking reaction. There is no activity of the Z–1500 catalyst in the reaction. This is because Z–1500 has no hydroisomerization and hydrogenation ability for cracking n-decane, according to its relatively low acidity, which is similar to SiO
2. In comparison, the highest n-decane conversion, at 82.1%, is obtained over the Z–24 catalyst. Meanwhile, the selectivity of olefin is only 6.7%, as shown in
Figure 2a. It is concluded that Z–24 has the highest hydrogenation ability. In the products distribution, shorter carbon chains and fewer olefins are obtained on zeolite Z–24 than on the other two catalysts. In
Figure 2b, the catalyst of Z–100 also provides a good catalytic performance in n-decane. Nevertheless, the n-decane conversion of 79.8% over the Z–100 catalyst is slightly lower than that over the Z–24 catalyst. The selectivity of olefins (11.2%) is much higher. Among the products, olefins seem to be a more valuable product. Thus, the Z–100 catalyst with a SiO
2/Al
2O
3 ratio of 100 is used below due to its good catalytic performance in n-decane.
The crystalline structure of catalysts can be confirmed using X-ray analysis.
Figure 3 shows the X-ray diffraction (XRD) patterns of the ZSM-5 zeolites with different SiO
2/Al
2O
3 molar ratios. The typical sole presence of the MFI framework is observed on the three samples. All samples give similar XRD patterns, which agrees well with those reported in the references. No other phase is found in all of the samples, confirming that the structure and crystallinity has not changed. Even though the crystalline structure and components are same in the three catalysts, they show obviously different catalytic performances in the n-decane hydrocracking reaction, suggesting that the different acidities supplied by the ZSM-5 zeolites of different SiO
2/Al
2O
3 molar ratios might be a crucial factor in the n-decane cracking reaction.
The texture parameters of ZSM-5 zeolites with different SiO
2/Al
2O
3 molar ratios are listed in
Table 2, and the N
2 sorption isotherms of the various catalysts are displayed in
Figure 4. Interestingly, for these three catalysts, mesopores appeared. These might be the piled mesopores caused by the crystal packing between the Si and Al in the ZSM-5 zeolites. Based on
Table 1, by increasing the SiO
2/Al
2O
3 molar ratio of the samples, the surface areas of the micropores increase. The surface areas of the piled mesopores decrease a lot from 283.9 to 77.1 m
2/g because of the Al amount being extremely low in the Z–1500 catalyst. For the Z–1500 catalyst, the Al element is too low to be detected, so the detailed SiO
2/Al
2O
3 ratio of Z–1500 could not be provided by the EDX.
In brief, zeolite ZSM-5 exhibits a good catalytic performance in the hydrocracking of n-decane. By increasing of SiO2/Al2O3 molar ratio, the total acid sites of ZSM-5 may decrease. The dehydrogenation ability increases and hydrocracking ability decreases. From the reaction results above, it is inferred that the ZSM-5 with a moderate higher SiO2/Al2O3 molar ratio is helpful for obtaining olefins; a low SiO2/Al2O3 molar ratio for the catalyst favors the cracking of the carbon-carbon bond of the n-decane, because the acidity of the catalyst plays a crucial role in the hydrocracking of the n-decane reaction.
2.2. Design of Mesoporous ZSM-5 Zeolite
To improve the catalytic activity and produce more valuable products in the n-decane hydrocracking reaction, the mesoporous ZSM-5 zeolite is synthesized via acid and alkali leaching, denoted as Z–100-M.
Figure 5 shows the XRD patterns of the ZSM-5 zeolite treated by acid and alkali leaching. Similar X-ray diffraction patterns can be found for the two catalysts. In comparison to the Z–100 catalyst, no new phases appeared in the Z–100-M catalyst. The results of the XRD patterns point out that the Z–100-M catalyst bulk structure is not obviously changed and that the crystalline structure is not destroyed.
Owing to the fact that XRD only verifies the structure of bulk phases, SEM technology is further operated to investigate the microstructure of the catalysts’ surface (
Figure 6). As shown in
Figure 6a–d, the particle sizes of the Z–100 and Z–100–M catalysts are similar. In the higher magnification images of
Figure 6b,d, the surface of the Z–100–M catalyst is clean and intact, confirming that the Z–100–M catalyst is not corroded by acid and alkali leaching during the process of mesopore generation. However, it is still difficult to distinguish from these images whether the mesopores are successful forming or not. Therefore, further studying of the characterization must be conducted in this research.
TEM is a sensitive characterization technology for visually identifying the microstructure of catalysts.
Figure 7a shows the TEM picture of Z–100, and there are no mesopores or mesoporous channels in the Z–100 catalyst. As illustrated in
Figure 7b, several rifts appear at Z–100–M, which are ascribed to the mesoporous channels. In the enlarged image of
Figure 7c, plenty of mesoporous channels are formed in the Z–100–M catalyst. It is also clearly found that the formed mesopores are relatively uniform in the Z–100–M catalyst, and they are presented by the nearly transparent drop-like dots (
Figure 7d). The results indicate that the mesopores are successfully formed in the Z–100–M catalyst by our catalyst preparation method. Moreover, the sizes of most mesopores are close to 20 nm, as shown in the insert of
Figure 7d. From our perspective, the generated mesopores and mesoporous channels will boost the n-decane hydrocracking process due to the supplied larger channels for reactant diffusion and more active sites in the Z–100–M catalyst.
The BET analysis also gives more evidences for successful forming mesopores in the Z–100–M catalyst, as shown in
Figure 8 and
Table 3. For Z–100, mesopores appeared. These might be the piled mesopores caused by the crystal packing in Z–100. For Z–100–M, the surface area of the mesopores increases, differing from the piled mesopores in Z–100. This is because the amount of micropores decreases (
Table 3) and a peak corresponding to the mesopores at about 20 nm is observed (
Figure 8b). It is believed that the acid leaching, together with the alkali leaching, is more effective for generating the inner mesopores on the zeolite ZSM-5. Moreover, the average pores’ size for Z–100–M is also enlarged from 3.47 to 3.99 nm, indicating that the new mesopores are formed in the Z–100–M catalysts.
In the previous reaction results of different SiO
2/Al
2O
3 molar ratio catalysts, it was inferred that the acidity of the catalyst plays a crucial role in the n-decane hydrocracking reaction. Thus, the NH
3-TPD characterization is performed to confirm the relationship between the acidity and catalytic performance over the two catalysts.
Figure 9 shows the acidity of the Z–100 and Z–100–M catalysts. There is a downshift tendency of the temperature of the peaks in the Z–100–M catalyst, indicating that the acid strength of Z–100–M is weaker than that of the Z–100 catalyst. Meanwhile, the amount of acidity also decreases in the Z–100–M in comparison to the Z–100 catalyst according to its lower intensity of peaks. The reason for this is that the Al and Si of the ZSM-5 zeolite can be partially removed by acid leaching, together with alkali leaching, during the process of the mesopores’ generation. Furthermore, the acidity of the zeolite is supplied by the strong interaction of the Si and Al components. As shown in
Figure 9, the acidity of Z–100–M is only weakened a little by the acid and alkali leaching. Moreover, the moderately weaker acidity of the catalyst is beneficial for producing olefins in the n-decance hydrocracking reaction, rendering the products more valuable.
Figure 10 and
Table 4 show the conversion and selectivity of the different types of ZSM-5 zeolites in the n-decane hydrocracking reaction. The results demonstrate that it has a better catalytic performance over the Z–100–M catalyst than over the Z–100 catalyst. In detail, the n-decane conversion of 88.6% over Z–100–M is higher than that of 79.8% over the Z–100 catalyst. Even though the Z–100 catalyst possesses a stronger acidity for a higher hydrocracking ability in the reaction, the generated mesopores and mesoporous channels of the Z–100–M catalyst supply more active sites for activating the reactant, leading to a higher conversion being achieved in the Z–100–M catalyst. Due to its specific characteristics of a better mass transfer and diffusion, the n-decane and long-chain byproducts can more easily be hydrocracked in the mesopores, making the products distribution drift to C
3–C
5. Moreover, the selectivity of the olefins is 33.7% over the mesoporous the ZSM-5 zeolite catalyst, which is much higher than that of 11.2% over the common ZSM-5 zeolite catalyst. This is because the ZSM-5 zeolite is ascribed to a solid acid with Lewis and Bronsted acid sites. The long-chain hydrocarbons can be cracked into short-chain hydrocarbons through its strong acidity, while simultaneously immediately hydrogenating the formed alkenes into corresponding alkanes. In the two acid sites, the Bronsted acid plays a crucial role in this process over the Lewis acid. The removal of Si and Al in the Z–100–M catalyst is beneficial for weakening the acidity of the ZSM-5 zeolite. Hence, the Z–100–M catalyst with a moderate acidity will be in favor of olefin production in comparison to the Z–100 catalyst. The result turns out to prove that designing the mesoporous Z–100–M catalyst is an effective way of improving the n-decane hydrocracking catalytic performance and of enhancing the value of the products.
Briefly, the mesoporous Z–100–M catalyst exhibits a better catalytic performance in the hydrocracking of n-decane. The well-designed mesoporous structure of this new ZSM-5 zeolite can easily accelerate the diffusion of reactants and products, while at the same time providing more effective active sites for hydrocracking n-decane. In the hydrocracking of n-decane under the Z–100–M catalyst, n-decane can easily access the moderate acid sites of zeolite through mesopores for hydrocracking, enhancing the n-decane conversion and producing more valuable products.
2.3. Tuning the Products Distribution by Loading Metallic Promoters
Based on the impact of the acidity in the products distribution, several metallic promoters such as alkaline-earth and noble metals have been introduced to optimize the products distribution, and they are denoted as Z–M–Mg, Z–M–Ca, Z–M–Sr and Z–M–Pd, respectively. The alkaline-earth metals are only used as promoters for the modification of the catalyst by changing its acidity. The alkaline-earth metals can weaken the acidity of the zeolite catalyst to enhance the olefin selectivity in the n-decane hydrocracking reaction. In the process of n-decane hydrocracking, the strong acidity of the catalyst is beneficial for initially cracking the C–C bond. The acidity is also helpful for immediately hydrogenating the formed olefins into alkanes, while at the same time reducing the products value. Hence, the modification of the catalyst by alkaline-earth metals is an effective way of weakening the catalyst acidity to obtain more olefins in the n-decane hydrocracking reaction. The noble metal Pd is used as a catalyst promoter to change the properties of the zeolite catalyst. In addition, adding Pd into the zeolite catalyst is a good method for enhancing the catalyst utilization efficiency according to the H2 spillover on Pd.
Each catalyst has been individually prepared by a typical impregnation method.
Figure 11 shows the XRD patterns of the mesoporous ZSM-5 zeolite (Z–100–M) catalysts modified by different alkaline-earth and noble metals. Similar X-ray diffraction patterns corresponding to MFI can be found for the catalysts modified by these metals. The results of the XRD patterns point out that the catalysts’ bulk structures show no obvious changes, indicating that the introduced promoters do not destroy the structure of the ZSM-5 zeolite. Meanwhile, the amounts of loaded metals are very low, and they are all well-dispersed on the zeolite surface; therefore, the characteristic peaks of the different metals are not observed.
The acidic properties of the different metallic-based mesoporous ZSM-5 zeolite catalysts are measured by NH
3-TPD, as shown in
Figure 12. The results of the NH
3-TPD patterns shows that the acidities of the zeolites become weaker when increasing the atomic number in the alkaline-earth metals. The alkalinity of the alkaline-earth metals partially covers the acid sites of ZSM-5 and effectively weakens the acidity of the mesoporous ZSM-5 zeolite. Among the catalysts of Z–M–Mg, Z–M–Ca and Z–M–Sr, the acidity of Z–M–Sr is the lowest. However, after adding the noble metal Pd, the catalyst Z-Pd still possesses a high acidity, with two marked peaks of weak and strong acid sites.
The texture parameters of the impregnated catalysts are listed in
Table 5 and have been characterized by BET technology. After an impregnation with 3 wt% alkaline-earth metals (Mg, Ca, Sr), the specific surface area of the mesopores were reduced by nearly half compared to Z–100–M, suggesting that the mesopores on the zeolite ZSM-5 were blocked by these metallic promoters. There is no big difference among these three alkaline-earth modified catalysts (Z–M–Mg, Z–M–Ca, Z–M–Sr) in the results of the BET analysis either. The catalysts’ activity might also be decreased in the n-decane hydrocracking reaction according to this phenomenon. Unlike the catalysts above, the loading amount of Pd is only 0.3 wt%, so the high surface area of mesopores is observed in the Z–M–Pd catalyst. It shows similar texture parameters to the Z–100–M catalyst, which indicates that the mesopores are not blocked in the Z–M–Pd catalyst.
The catalytic performances of alkaline-earth and noble metallic based catalysts in the n-decane hydrocracking reaction are shown in
Figure 13 and
Table 6. By adding these promoters, the n-decane conversion and products distribution are totally different. For the Z–M–Mg, the n-decane conversion decreases to 52.8% with many olefins being formed (50.7%), which shows a good selectivity of valuable olefins. The decrease of the catalyst activity is affected by the partially blocked mesopores and is somehow influenced by the alkalinity of the metallic Mg. In the n-decane hydrocracking reaction, the supplied acid sites are in favor of cracking the C–C bond of long-chain alkanes. With an increase of the alkalinity in promoters, the n-decane conversion further decreases to 22.5% over the Z–M–Sr. However, the olefins increase to 64.6% at most in the Z–M–Sr catalyst. This further demonstrates our previous views, which were that the alkalinity plays a crucial role in the olefin production rather than the acidity over the catalysts. Thus, in these three alkaline-earth metals modified catalysts, Z–M–Mg seems to be the best catalyst for the n-decane conversion into valuable products. This is because it not only possesses a moderate alkalinity to produce olefins but also has a moderate acidity to crack n-decane at the same time. Surprisingly, it shows diametrically opposite reaction results over the Z–M–Pd catalyst. The n-decane conversion is extremely high at 95.3%; meanwhile, no olefins are produced in the products. The N-alkanes selectivity is as high as 84.5%, especially at 46.7% for propane. It is clearly shown that the products distribution drifts to lower hydrocarbons, as shown in
Figure 13. The noble metal Pd is a sensitive element in many catalytic reactions due to its physicochemical properties. Even though the tiny Pd loading amount of 0.3 wt% is hardly enough to block the mesopores in the ZSM-5 zeolite, the major reason leading to this phenomenon is the occurrence of a H
2 spillover according to the specifics of Pd. A hydrogen spillover is the surface migration of activated hydrogen atoms from a metal catalyst particle, on which they are generated onto the catalyst support [
40,
41,
42,
43]. For the Z–M–Pd catalyst, the activated hydrogen atoms spill to the surface of the mesoporous ZSM-5 zeolite via the promoter Pd. Hence, the chemisorbed hydrogen atoms intensively attack the C–C bond of long-chain alkanes, while at the same time further hydrogenating the formed olefins into alkanes immediately. Based on these reasons, the Z–M–Pd is used as an outstanding catalyst for alkanes synthesis, especially for propane. The low impregnation amount of Pd effectively enhances its economic value for further industrial applications. With regards to its potential for industrial applications, the Z–M–Pd catalyst will significantly reduce the energy consumption and cost of products separation.
In conclusion, after being modified by the noble metal Pd, the process of catalytic hydrocracking becomes more thorough. It exhibits an outstanding n-decane conversion with an excellent propane selectivity in the catalytic hydrocracking reaction. In addition, the mesoporous zeolite ZSM-5 catalysts, modified by alkaline-earth metals, exhibit a good catalytic selectivity of olefins in the hydrocracking of n-decane. Among all olefin products, the amount of propylene is the highest. With the catalysts’ alkalinity increasing, the selectivity of propylene and other olefins increases. We can conclude that the alkalinity of catalysts significantly influences the selectivity of olefins. This is because a strong acidity of catalysts will hydrogenate the formed olefins into alkanes, while at the same time affecting the activity of the hydrocracking reaction.