1. Introduction
Para-xylene (PX) is of great value since it is useful in manufacturing terephthalic acid, which is an intermediate in the manufacture of synthetic fibers. The catalytic process for producing PX has been paid much attention and become a quite competitive subject in the petrochemical industry [1,2]. The reactions of toluene disproportionation [3,4], transalkylation of benzene with trimethylbenzene [5,6] and toluene methylation [7,8,9] were used to produce PX. However, it is imperative to develop new technologies because of the depletion of oil. The conversion of methanol to hydrocarbons over acidic zeolite catalysts is now considered an important and feasible non-petroleum route to obtain valuable chemicals [10,11,12,13,14,15,16,17,18]. Therefore, it is a significative work to design a shape selectivity catalyst for high PX selectivity in methanol to aromatics conversion (MTA). The reaction of methanol to para-xylene (MTPX) is a new technology for the upgrading of coal, biomass or natural gas into liquid fuels, which makes the production process of PX less reliant on crude oil resource.
In recent decades, the selective production of PX via alkylation or disproportionation of toluene has been studied over various zeolites catalysts, such as ZSM-5, MCM-22, mordenite and Y zeolite [19,20,21,22,23]. Among these zeolite catalysts, ZSM-5 zeolite has attracted more attention because of the well-defined 10 membered-ring channels that are much more favorable to the diffusion of PX than that of OX (ortho-xylene) or MX (meta-xylene). Therefore, an excellent PX selectivity could be expected by modifying ZSM-5 zeolite appropriately. It is found that the para-selectivity and external surface acidity are usually inversely related [10]. Meanwhile, zeolites are known as shape-selective catalysts due to the presence of micropores with a pore diameter close to the molecular diameter of the products. Hence, in order to obtain high PX selectivity, it is important to reduce the acid sites, decrease the external surface area or modify the pore-openings by post synthesis modification. A number of modification methods are reported to improve para-selectivity, including silanation [24,25], precooking [26] and metal/non-metal oxide impregnation [27,28]. Among them, the impregnation of phosphate species on ZSM-5 has been shown to be convenient and effective to achieve a high PX selectivity [3,29,30]. The earlier study by Kaeding and coworkers [27,31] showed that the oxides of phosphorus species in zeolite pores imparted a diffusion barrier in the micropores exhibiting an increase in the para selectivity. Védrine et al. [32] found that phosphorus species passivated acid sites primarily at the entrance of the channels of the zeolite and the strong acid sites remained unmodified. They concluded that the high selectivity for para isomers of xylene (X) were assumed to be related to the narrowing of the pore size and the zeolite framework phosphorus species, rather than to the modification of acid sites’ strength. Janardhan and coworkers [30] reported that the introduction of phosphorous into ZSM-5 zeolite generated new acid sites with pore narrowing, which were formed by the interaction of phosphates with bridging hydroxyl groups of ZSM-5 zeolites in the micropores. The active sites generated monolayer islands over zeolite surface and narrowed the pore opening, leading to a high selectivity of PX for alkylation and disproportionation reactions. Recently, the non-petroleum route to produce PX through MTA reaction has been increasingly investigated. Miyake et al. [33] reported a Zn/ZSM-5@silicalite-1 core-shell zeolite catalyst which showed a high xylene yield and PX selectivity, and the yield of PX could reach 40.7%. Wei et al. [34] designed a Zn–P–Si–ZSM-5 catalyst which showed increased selectivity PX (89.6%) in X for MTA reaction. The catalyst was impregnated with a Zn and P over the ZSM-5 sample, and then SiO2 was loaded by chemical liquid phase deposition (CLD) modification. Zhu et al. [2] prepared Mg–Zn–Si-HZSM-5 catalyst by using the CLD method with polyphenylmethylsiloxane and then introducing Zn and Mg through vacuum impregnation. The prepared catalyst showed a high selectivity of PX in X (98.9%) and a relatively long lifetime for the MTA.
In this work, the highly shape-selective P/HZSM-5 catalysts for the MTA reaction were prepared by incipient wetness impregnation with H3PO4 as a source of phosphorus and the different amounts of loaded phosphorus were obtained by changing the concentration of H3PO4 solution. Then, the obtained samples were investigated by X-ray powder diffraction (XRD), infrared spectra for pyridine adsorption (Py-IR), N2 adsorption–desorption, temperature programmed desorption of NH3 (NH3-TPD), solid-state magic angle spinning nuclear magnetic resonance (MAS NMR) and thermogravimetric analysis (TG). Due to the fine modification of pore size and acidic properties, the selectivity of PX in X and the selectivity for xylene in aromatics over P/HZSM-5 catalyst both increased. 2. Results and Discussion 2.1. Catalyst Characterization
As shown in Figure 1, all the zeolite catalysts exhibited the similar peaks, which were the typical MFI structure. (JCPDS no. 73–1138) No new diffraction peak could be observed after the introduction of P species, even at the loadings of 5 wt.% P. The results indicated that the introduction of P did not destroy the structure of ZSM-5 framework severely and P was highly dispersed in ZSM-5 zeolite. Also, the relative crystallinities of prepared catalysts as shown in Table 1 decreased evidently. The crystallinity of the ZSM-5 zeolite was reduced to 76.4% after the loading of 5 wt.% P, which was most likely due to the framework defects caused by a certain degree of dealumination of the framework [2], as illustrated in the following 27Al MAS NMR results (Figure 6A). The surface area and pore volume of HZSM-5 and P/HZSM-5 samples calculated by nitrogen adsorption–desorption were shown in Table 1. The BET surface area, external surface area and micropore volume all obviously decreased with the increase in P doping concentration, while the mesopore volume was almost constant, which could be ascribed to the fact that the loadings of P species blocked or destroyed some micropores in HZSM-5 during the process of phosphorus modification [35]. This indicated that the phosphorus species were not only doped on the external surface but also in the ZSM-5 channels. Compared with the total surface area, the external surface area decreased more obviously. The external surface area had decreased by more than 57% with 5 wt.% P loading.
The incorporation of phosphorus obviously influenced the porous structure of HZSM-5, as illustrated in Figure 2. The loading of P made the pore size distribution of HZSM-5 a little narrow and the pore size become remarkably smaller. The shrinkage of pore size in P modified HZSM-5 zeolites may be attributed to the formation of hydroxy-bridged P species in ZSM-5 zeolites or the accumulation of P species in the channels of ZSM-5 zeolites, which may impart a diffusion barrier and influence product diffusion in the micropores resulting in an increase in shape selectivity [30]. In order to reveal the probable relationship between the pore size and the catalytic properties, the adsorption isotherms of PX and MX on HZSM-5 and 5% P/HZSM-5 are shown in Figure 3. The adsorption results verified that m-xylene was more diffusion-limited than p-xylene on P modified HZSM-5 catalyst. This indicated that the introduction of P was beneficial to enhance the competitive adsorption of p-xylene because of pore narrowing. A similar phenomenon was found when SiO2 was loaded on the surface of the ZSM-5 catalyst. Compared with the unmodified ZSM-5 catalyst, the Si-modified catalyst enhanced the diffusion barrier in the mouth or channel of the zeolite and significantly inhibited the adsorption and diffusion of m-xylene [6].
The total acid quantity and strength of acid sites in parent and P-modified HZSM-5 zeolites were obtained by NH3-TPD, as shown in Figure 4. The HZSM-5 zeolite exhibited a typical NH3- TPD profile with two characteristic peaks at about 190 and 380 °C, representing the ammonia adsorbed on the weak acid sites and strong acid sites, respectively [36]. After the doping with P, the evident changes in the peak temperature and area of the strong acid sites were observed. The peak temperature of the strong acid sites shifted towards a low temperature and the peak area decreased obviously. The more P doping was used, the smaller the peak area became, indicating that the decrease in the amount and strength of strong acid sites was due to the doping with P. The low-temperature peak also slightly shifted toward a low temperature, demonstrating that the loading of P also reduced weak acid strength. The difference was that the density of weak acid sites in low temperature was less affected with the increase in P loadings (as listed in Table 2).
Chemisorption of pyridine on HZSM-5 and P-modified HZSM-5 zeolites also illustrated the changes in zeolite acidity. As shown in Figure 5, all catalysts showed absorption peaks at about 1545 and 1450 cm−1, which were ascribed to pyridine chemisorbed on Brönsted (B) acid sites and pyridine adsorbed on Lewis (L) acid sites, respectively [37,38]. The incorporation of phosphorus led to a dramatic decline in the amount of both Brönsted and Lewis acidic sites. When small amounts of P were added (≤1 wt.%), the acid amount of the Brönsted acid sites showed a sharp decrease compared to that of the Lewis acid sites (as listed in Table 2). Whereas, further increasing phosphorus content from 1 to 5 wt.% resulted in an evident decrease in the acid amount of the Lewis acid sites and a slight decrease in the amount of the Brönsted acid sites. In summary, the loading of phosphorus reduced both the acid strength and amount of HZSM-5 zeolite, especially strong acid sites.
27Al MAS NMR has been extensively used as an effective technique to identify states of the Al atoms in the zeolite. Figure 6A showed 27Al MAS NMR spectra of HZSM-5 and P/HZSM-5 samples. For the parent HZSM-5 zeolite, a characteristic peak of typical Al species around 53 ppm was detected that could be ascribed to a tetrahedral framework aluminum [32]. A relatively weak signal appeared at 0 ppm which could be assigned to octahedral aluminum species, revealing that there existed a small number of extra-framework aluminum species in the HZSM-5 zeolite. With increasing impregnation degree, new peaks at about −14 and 40 ppm appeared. The signal at −14 ppm was related to octahedral aluminum interacting with a P atom [39]. The peak around 40 ppm was generally assigned to a tetrahedral framework aluminum or extra-framework aluminum species in a distorted environment [40]. With the increase in P loadings, the intensity of signals at −14 and 40 ppm increased while that at 53 ppm decreased, illustrating that the dealumination of the HZSM-5 zeolite framework occurred as a result of the phosphate impregnation, consistent with the XRD, micropore volume and acidity measurement results.
The 31P MAS NMR spectra of P/HZSM-5 zeolites were shown in Figure 6B. The peak at 0 ppm was ascribed to excess P species which did not interact with framework aluminum. The signal around −6 ppm was assigned to P species in pyrophosphoric acid or pyrophosphates, whereas the −12 ppm signal was assigned to P species for intermediate groups in short-chain polyphosphates or pyrophosphates. The signals from −18 to −40 ppm were mainly due to extra-framework aluminophosphate and highly condensed polyphosphate complexes. Another signal appearing at −46 ppm could be assigned to intermediate P4O10 groups [32,41]. As can be seen in Figure 6B, the signals at 0 and −12 ppm increased slightly with the increase in P content, whereas the peaks from −18 to −40 ppm decreased evidently. This indicated that the phosphorus content had a remarkable effect on the existent state of the phosphorus species, which may have an influence on the catalytic performance.
2.2. Influence of Phosphorus on the Catalytic Performance
The effect of phosphorus on the catalytic performance was illustrated in Figure 7 and Table 3. The introduction of phosphorus exhibited a significant impact on the catalytic stability, methanol conversion, and product selectivity. Compared with the unmodified HZSM-5, a small amount of phosphorus (≤1 wt.%) could enhance the catalyst stability at a certain degree. Further increasing the P content, the catalyst stability and methanol conversion both decreased evidently. Equilibrium mixtures of xylene isomers generally contain only 23%–24% PX. As can be seen in Figure 7B, the PX selectivity in xylene was 23.8% on unmodified HZSM-5 zeolite. The introduction of phosphorus to HZSM-5 zeolite appreciably increased the selectivity for PX in xylene in the MTA reaction. The selectivity of PX in xylene increased with the increase in P content and it reached nearly to 90% when P content was 5 wt.%. Meanwhile, the selectivity for xylene in aromatics was enhanced with increasing the P content. The further detailed results were listed in Table 3. The modified catalysts also greatly improved the selectivity of light olefins (C2=~C5=) and decreased the generation of aromatics and alkanes (C1−~C4−).
Generally, in the MTA reaction, methanol is dehydrated to form dimethyl ether with the action of protons, which can be converted to light olefins by further dehydration and methylation. The light olefins are further developed into C5+ non-aromatic hydrocarbons by polymerization and cyclization. Then the aromatics and alkanes are generated by hydrogen transfer and dehydro–cyclization reactions under the action of Brönsted acid sites [14,42]. The results of acidity measurement showed that the amount of the Brönsted acid sites decreased obviously after the doping of P, which was consist with the changes in the selectivity of aromatics and alkanes. In addition, because phosphorus can enter the channels of catalyst and cover the strong acid sites of the inner surface, the amount and strength of strong acid sites decreased significantly with P doping, resulting in the poor methanol conversion [43].
The spent catalysts were studied using thermogravimetric analysis. The weight loss of the samples on the range of 300–750 °C revealed the decomposition of coke deposition [9]. As shown in Figure 8, the amounts of coke deposition in the used P/HZSM-5 catalysts decreased to a certain extent. Especially, increasing P content to more than 1% resulted in an obvious decrease in coke amounts. As can be seen from the catalytic performance (Figure 7 and Table 3), when P content was above 1%, the catalyst stability and methanol conversion both decreased evidently, whereas the selectivity of PX in X improved greatly. The phenomenon may be due to the fact that high level loadings of P blocked more pore volume and external surface area, which reduced the resistance of coke deposition of the catalyst. The narrowed pore size lead by the introduction of P limited the diffusion of products and made the micropore entrance block quickly, resulting in a fast coke deposition rate and deactivation of the catalyst.
Meanwhile, the introduction of P reduced external surface area and narrowed the pore size, leading to an increase in the selectivity of xylene and PX. It is reported that the narrowing of the pore openings and the poisoning of external acid sites can enhance the PX selectivity in X isomers in MTA reaction [2]. Firstly, the narrowed pore size made the generation of PX easier than that of other X isomers and C9+ aromatics, and the small amount of other X isomers and C9+ aromatics formed was also difficult to diffuse out the zeolite channel. Moreover, the isomerization reaction of PX was inhibited after PX diffusing to the external surface which was poisoned by P species [42]. Therefore, the P/HZSM-5 was highly shape-selective for PX in the MTA reaction. However, the PX yield did not increase significantly as expected because of the decrease in the selectivity of aromatics and methanol conversion. The previous work found that the introduction of Zn species could generate the Zn-Lewis acid sites, which was beneficial to the formation of aromatics through the dehydration and cyclization reactions of light olefins [14]. Therefore, it is suggested that the catalyst with a high aromatics selectivity and high PX selectivity could be obtained by loading Zn over 5% P/HZSM-5.
3. Materials and Methods 3.1. Catalyst Preparation
To obtain the sample with uniform crystal size, ZSM-5 zeolite was synthesized by seed-induction synthesis. The silicalite-1 seed was synthesized by modifying the procedures reported in reference [44]. The obtained colloidal silicalite-1 was directly used as a seed to prepare ZSM-5 zeolites. ZSM-5 samples were synthesized with the molar composition: SiO2:0.011Al2O3:0.02Na2O:0.15TPAOH:30H2O prepared from silica sol (30 wt.% SiO2), sodium aluminate (NaAlO2, Al2O3 ≥ 41 wt.%), tetrapropylammonium hydroxide (TPAOH, 48.67 wt.% in aqueous solution). The synthesis mixture was conducted at 170 °C in a teflon-lined, stainless-steel autoclave under rotation (20 r/min). The obtained samples were recovered by centrifugation and repeatedly re-suspended in distilled water to remove physically attached templates. The recovered samples were dried at 100 °C overnight and calcined at 560 °C for 10 h in air, repeatedly ion-exchanging Na+ with aqueous NH4NO3 solution (1 M, m(liquid)/m(solid) = 40) at 80 °C for 6 h, and subsequently calcined at 560 °C for 6 h.
Incipient wetness impregnation was used to incorporate Phosphorous species into HZSM-5 and the different phosphorous content was obtained by changing the concentration of H3PO4 solution, then dried at 100 °C overnight and calcined at 560 °C for 6 h under ambient condition. 3.2. Catalyst Characterization X-ray powder diffraction (XRD) patterns were collected on a Rigaku MiniFlex II desktop X-ray diffractometer (Rigaku, Tokyo, Japan) with monochromated Cu Kα radiation (30 kV and 15 mA). By assuming that the zeolite sample had the largest peak area in the range of 2θ from 22° to 25° (here, it was the parent HZSM-5), as a reference had a crystallinity of 100%, the relative crystallinity of the P/HZSM-5 catalyst was then estimated by comparing its total peak area in this 2θ range with that of the parent HZSM-5.
Nitrogen adsorption/desorption isotherms were measured at –196 °C on a BELSORP-max gas adsorption analyzer (MicrotracBEL, Osaka, Japan). The adsorption isotherms of p-xylene and m-xylene on the zeolites were measured at 25 °C on the BELSORP-max instrument. The measurement process and result analysis were similar to those described in our previous work [14]. Similarly, temperature-programmed desorption of NH3 (AutoChem II 2920 chemisorption analyzer, Micromeritics, Atlanta, GA, USA) (NH3-TPD, to obtain the amount and strength of acid sites), and infrared spectra for pyridine adsorption (Tensor 27 FT-IR spectrometer, Bruker, Karlsruhe, Germany) (Py-IR, to get the acidity of Brönsted and Lewis acidic sites [45]), were performed by following similar procedures with the same apparatus as reported previously [12,14].
Solid-state NMR investigations were performed on Bruker Avance III 600 spectrometer (Bruker, Karlsruhe, Germany). 31P MAS NMR was recorded with 85% phosphoric acid as the reference at 161.9 MHz with a pulse length of 3 μs (60°) and pulse interval of 60 s. 27Al MAS NMR was carried out with 1.0 M aqueous solution of Al(NO3)3 as the reference at 104.3 MHz, with the pulse of 1.7 μs, and a pulse interval of 60 s. All the data were acquired at a spinning speed of 8 kHz. Coke deposition after MTA reactions was performed by TG on a Rigaku Thermo plus Evo TG 8120 instrument (Rigaku, Tokyo, Japan). The spent catalysts were combusted from room temperature to 800 °C with a heating rate of 10 °C min−1 in air. 3.3. Catalyst Evaluation
The MTA reaction was performed in a fixed-bed micro reactor (Pengxiang, Tianjin, China). The reaction was carried out with methanol WHSV of 3.2 h−1 at 390 °C and 0.5 MPa. The zeolite catalysts were crushed and sieved to 20–40 mesh and pretreated at reaction temperature for 8 h in a nitrogen flow. The gas and liquid products were separated with a cold trap and analyzed by gas chromatographs (7890A, Agilent, Palo alto, CA, USA). The specific parameters of GC were the same values as described previously [14].
4. Conclusions The phosphorous-modified HZSM-5 zeolites were prepared by incipient wetness impregnation. The effect of phosphorous on the structure of HZSM-5 and its relationship with the catalytic performance of P/H-ZSM-5 catalysts in MTA was studied. The results indicated that the introduction of P could reduce micropore volume and external surface area, narrow the pore size and decrease the amount and strength of strong acid sites. The pore size and acid properties of zeolite were finely modified by introducing phosphorous, which resulted in the P/HZSM-5 catalyst enhancing the PX selectivity in X isomers for MTA reaction. The PX selectivity in X and the selectivity for xylene in aromatics both improved significantly with the increase in P content. However, excessive P (>1%) also resulted in the decrease in aromatic selectivity and methanol conversion. The PX selectivity (in xylene) could reach nearly to 90% when P content was 5 wt.%, while the selectivity of xylene in aromatics was enhanced from 41.3% to 60.2%. Owing to the decrease in the selectivity of aromatics and methanol conversion, the yield of PX needs to be further improved. It is suggested that the catalyst with a high PX selectivity in X and high PX yield could be obtained by loading Zn over 5% P/HZSM-5 which can generate the Zn-Lewis acid sites to enhance the formation of aromatics through the dehydration and cyclization reactions of light olefins.
Enlarge this image.Figure 1. XRD patterns of the different catalysts: (a) HZSM-5, (b) 0.5% P/HZSM-5, (c) 1% P/HZSM-5, (d) 2% P/HZSM-5, (e) 3% P/HZSM-5 and (f) 5% P/HZSM-5.
Enlarge this image.Figure 2. Pore size distribution of parent and P modified HZSM-5 zeolites: (a) HZSM-5, (b) 0.5% P/HZSM-5, (c) 1% P/HZSM-5, (d) 2% P/HZSM-5, (e) 3% P/HZSM-5 and (f) 5% P/HZSM-5.
Enlarge this image.Figure 3. Adsorption isotherms of para-xylene (PX) (A) and meta-xylene (MX) (B) on HZSM-5 (a) and 5% P/HZSM-5 (b).
Enlarge this image.Figure 4. NH3-TPD profiles of parent and P-modified HZSM-5 zeolites: (a) HZSM-5, (b) 0.5% P/HZSM-5, (c) 1% P/HZSM-5, (d) 2% P/HZSM-5, (e) 3% P/HZSM-5 and (f) 5% P/HZSM-5.
Enlarge this image.Figure 5. FT-IR spectra of pyridine adsorption on parent and P-modified HZSM-5 zeolites: (a) HZSM-5, (b) 0.5% P/HZSM-5, (c) 1% P/HZSM-5, (d) 2% P/HZSM-5, (e) 3% P/HZSM-5 and (f) 5% P/HZSM-5.
Enlarge this image.Figure 6. 27Al MAS NMR spectra (A) and 31P MAS NMR spectra (B) of parent and P-modified HZSM-5 zeolites: (a) HZSM-5, (b) 0.5% P/HZSM-5, (c) 1% P/HZSM-5, (d) 2% P/HZSM-5, (e) 3% P/HZSM-5 and (f) 5% P/HZSM-5.
Enlarge this image.Figure 7. Methanol conversion with the time on stream (TOS) (A) and product selectivity at a TOS of 12.5 h (B) over parent and P-modified HZSM-5 zeolites: (a) HZSM-5, (b) 0.5% P/HZSM-5, (c) 1% P/HZSM-5, (d) 2% P/HZSM-5, (e) 3% P/HZSM-5 and (f) 5% P/HZSM-5.
Enlarge this image.Figure 8. Thermogravimetric analysis (TG) curves of the spent HZSM-5 and P/HZSM-5 catalysts.
| Samples | Crystallinity (%) | SBET (m2·g) | Se (m2·g) | Vmes (cm3·g) | Vmic (cm3·g) |
|---|---|---|---|---|---|
| HZSM-5 | 100 | 381 | 13.5 | 0.03 | 0.18 |
| 0.5% P/HZSM-5 | 96.2 | 360 | 12.9 | 0.04 | 0.17 |
| 1% P/HZSM-5 | 94.4 | 333 | 11.8 | 0.03 | 0.15 |
| 2% P/HZSM-5 | 87.6 | 311 | 9.4 | 0.03 | 0.14 |
| 3% P/HZSM-5 | 85.2 | 285 | 8.5 | 0.03 | 0.13 |
| 5% P/HZSM-5 | 76.4 | 246 | 5.8 | 0.04 | 0.10 |
Note: SBET, BET surface area; Se, external surface area, calculated by the t-plot method; Vmes, mesopore volume; Vmic, micropore volume, obtained by the t-plot method; the relative crystallinity is compared with the parent HZSM-5 having the strongest diffraction intensity.
| Samples | Acidity by Strength a (mmol·g) | Acidity by Type b (mmol·g) | ||||
|---|---|---|---|---|---|---|
| Strong | Weak | Total | Brönsted | Lewis | L/B | |
| HZSM-5 | 0.32 | 0.20 | 0.52 | 0.170 | 0.054 | 0.32 |
| 0.5% P/HZSM-5 | 0.24 | 0.17 | 0.41 | 0.082 | 0.046 | 0.56 |
| 1% P/HZSM-5 | 0.18 | 0.19 | 0.37 | 0.079 | 0.033 | 0.42 |
| 2% P/HZSM-5 | 0.15 | 0.18 | 0.33 | 0.075 | 0.020 | 0.27 |
| 3% P/HZSM-5 | 0.13 | 0.20 | 0.33 | 0.073 | 0.009 | 0.12 |
| 5% P/HZSM-5 | 0.05 | 0.26 | 0.31 | 0.072 | 0.005 | 0.07 |
a Determined by NH3-TPD. b Obtained by Py-IR. L/B, the ratio of the amount of Lewis acidic sites to that of Brönsted acidic sites.
| Catalysts | Conv.MeOH | Production Selectivity (wt.%) | Xylene in Aromatics | PX in X | Yield of PX b | ||||
|---|---|---|---|---|---|---|---|---|---|
| C1−~C4− | C2=~C5= | C5+ non-Aromatics | Aromatics | Others a | - | - | - | ||
| HZSM-5 | 99.8 | 37.91 | 7.96 | 18.78 | 33.26 | 2.09 | 43.14 | 23.83 | 3.41 |
| 0.5%P/HZSM-5 | 99.6 | 34.20 | 8.29 | 24.43 | 31.14 | 1.94 | 43.30 | 28.70 | 3.86 |
| 1%P/HZSM-5 | 99.2 | 26.24 | 14.70 | 29.64 | 29.22 | 0.20 | 45.33 | 46.02 | 6.05 |
| 2%P/HZSM-5 | 83.6 | 16.59 | 42.74 | 16.33 | 23.05 | 1.29 | 49.12 | 76.14 | 7.21 |
| 3%P/HZSM-5 | 75.1 | 11.96 | 49.75 | 16.65 | 20.57 | 1.07 | 56.44 | 86.12 | 7.51 |
| 5%P/HZSM-5 | 68.4 | 10.73 | 62.42 | 9.86 | 15.42 | 1.57 | 60.16 | 89.05 | 5.65 |
a Others, H2 and COX; b the yield of PX is calculated through methanol conversion × aromatics selectivity × xylene selectivity in aromatics × PX selectivity in X; Conv.MeOH, methanol conversion. The data were obtained at 12.5 h.
Author Contributions
Conceptualization, X.N., M.D. and W.F.; Data curation, K.W. and Y.-e.D.; Formal analysis, X.N. and K.W.; Funding acquisition, X.N., Y.-e.D. and Y.C.; Investigation, Y.B.; Methodology, X.N.; Writing-original draft, X.N.; Writing-review and editing, X.N., K.W. and Y.C.. All authors have read and agreed to the published version of the manuscript.
Funding
This research received no external funding.
Acknowledgments
This work was financially supported by the Doctor Research Funds of Jinzhong University, Scientific and Technologial Innovation Programs of Higher Education Institutions in Shanxi (No. 2019L0881), the Applied Basic Research Project of Shanxi (No. 201901D111303), Shanxi "1331 Project" Key Innovative Research Team (PY201817), Jinzhong University "1331 Project" Key Innovative Research Team (jzxycxtd2017004 and jzxycxtd2019005) and the Research Project of Science and Technology of the Henan Province (202102310565).
Conflicts of Interest
The authors declare no conflict of interest.
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Xianjun Niu1,2,*, Kai Wang3,*, Yang Bai1, Yi-en Du1, Yongqiang Chen1, Mei Dong2 and Weibin Fan2
1College of Chemistry and Chemical Engineering, Jinzhong University, Jinzhong 030619, China
2State Key Laboratory of Coal Conversion, Institute of Coal Chemistry, Chinese Academy of Sciences, 27 South Taoyuan Road, Taiyuan 030001, China
3College of Chemical and Environmental Engineering, Anyang Institute of Technology, Anyang 455000, China
*Authors to whom correspondence should be addressed.
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; Wang, Kai; Bai, Yang; Yi-en Du; Chen, Yongqiang; Dong, Mei; Fan, Weibin