Chinese Journal of Chemical Physics   2016, Vol. 29 Issue (5): 617-622

The article information

Tang Wen-wu, Zhang Xing-hua, Zhang Qi, Wang Tie-jun, Ma Long-long
汤文武, 张兴华, 张琦, 王铁军, 马隆龙
Hydrodeoxygenation of Anisole over Ni/α-Al2O3 Catalyst
Ni/α-Al2O3催化剂作用下苯甲醚的加氢脱氧
Chinese Journal of Chemical Physics , 2016, 29(5): 617-622
化学物理学报, 2016, 29(5): 617-622
http://dx.doi.org/10.1063/1674-0068/29/cjcp1603062

Article history

Received on: March 30, 2016
Accepted on: April 22, 2016
Hydrodeoxygenation of Anisole over Ni/α-Al2O3 Catalyst
Tang Wen-wua,c, Zhang Xing-huab,c, Zhang Qib,c, Wang Tie-junb,c, Ma Long-longb,c     
Dated: Received on March 30, 2016; Accepted on April 22, 2016
a. Department of Chemistry, University of Science and Technology of China, Hefei 230026, China;
b. Key Laboratory of Renewable Energy, Chinese Academy of Sciences, Guangzhou 510640, China;
c. Guangzhou Institute of Energy Conversion, Chinese Academy of Sciences, Guangzhou 510640, China
Author: zhangxh@ms.giec.ac.Tel, Tel: +86-20-87057673, FAX: +86-20-87057789; mall@ms.giec.ac.cn, Tel: +86-20-87057673, FAX: +86-20-87057789
Abstract: Ni-based catalysts supported on di erent supports (α-Al2O3, γ-Al2O3, SiO2, TiO2, and ZrO2) were prepared by impregnation. Effects of supports on catalytic performance were tested using hydrodeoxygenation reaction (HDO) of anisole as model reaction. Ni/α-Al2O3 was found to be the highest active catalyst for HDO of anisole. Under the optimal conditions, the anisole conversion is 93.25% and the hydrocarbon yield is 90.47%. Catalyst characteriza-tion using H2-TPD method demonstrates that Ni/α-Al2O3 catalyst possesses more amount of active metal Ni than those of other investigated catalysts, which can enhance the cat-alytic activity for hydrogenation. Furthermore, it is found that the Ni/α-Al2O3 catalyst has excellent repeatability, and the carbon deposited on the surface of catalyst is negligible.
Key words: Anisole     Hydrodeoxygenation     Ni/α-Al2O3     Hydrocarbons    
I. INTRODUCTION

Lignin, a three-dimensional amorphous polymer consisting of methoxylated phenylpropane structures, is contained in plant biomass with high proportion [1-3]. It can be transformed into phenolic compounds via depolymerization [4, 5]. It has been reported that yield of 13.2% phenolic monomers was obtained from organosolv pine lignin via catalytic depolymerization in the presence of MgO and THF [6]. However, obtained phenolic products were complex mixtures with high oxygen content [7, 8]. The high oxygen content led to many undesirable properties, such as high viscosity, thermal instability, corrosiveness, poor heating value and immiscibility with hydrocarbon fuels [9, 10]. Hence, the removal of oxygen is required to obtain hydrocarbons as high-graded fuels.

Hydrodeoxygenation (HDO) is an effective method for the production of hydrocarbons from lignin-derived phenolic compounds [11-13]. Bifunctional catalyst comprised by active metal and solid acid exhibits excellent activity for HDO reaction. For example, guaiacol was completely converted with high selectivity for cyclohexane over Ni/SiO$_2$-ZrO$_2$ catalyst [10]. Normally, it is considered that the metal Ni acts as hydrogenation activity center while the support SiO$_2$-ZrO$_2$ provides acidic sites for the HDO reaction.

Support material is a crucial factor determining the catalytic performance. In the past years, $\gamma$-Al$_2$O$_3$ was widely used as catalyst support for HDO catalyst due to its cheap cost, excellent texture, and suitable acidity. For example, the HDO of guaiacol with conversion of 100% and yield of 88% of cyclohexane was obtained over the Pd-based catalyst supported on $\gamma$-Al$_2$O$_3$ [14]. Oxygen contained in phenolics was also efficiently removed by hydrodeoxygenation with the sulfided NiMo/$\gamma$-Al$_2$O$_3$ and CoMo/$\gamma$-Al$_2$O$_3$ catalysts [7, 15]. However, large amount of coke formed and deposited on the surface of the catalyst during the HDO reaction process [7, 15]. Worse, partial $\gamma$-Al$_2$O$_3$ can be transformed into boehmite under hydrothermal conditions, resulting in a decrease for catalytic activity [16]. To overcome these drawbacks, many support materials such as SiO$_2$ [17], TiO$_2$ [18], and ZrO$_2$ [15] were also explored in the past years, exhibiting impressive catalytic activity for HDO reaction.

$\alpha$-Al$_2$O$_3$ is a type of mesoporous material with excellent hydrothermal stability. However, scarce work has been done to remove oxygen from phenolics with the HDO catalyst supported on $\alpha$-Al$_2$O$_3$. In this work, HDO reaction of anisole with the Ni-based catalyst supported on $\alpha$-Al$_2$O$_3$ was investigated to explore the effect of support on the catalytic properties. For comparison, the Ni-based catalysts supported on $\gamma$-Al$_2$O$_3$, SiO$_2$, TiO$_2$, and ZrO$_2$ were also investigated in the HDO reaction of anisole.

II. EXPERIMENTS A. Catalyst preparation

SiO$_2$ was prepared by chemical precipitation using NH$_4$NO$_3$ and Na$_2$SiO$_3$ as materials. The precipitate was dried at 120 $^{\circ}$C overnight and then calcinated at 500 $^{\circ}$C for 4 h. Similarly, ZrO$_2$ was prepared by chemical precipitation using NH$_3$$\cdot$H$_2$O and ZrOCl$_2$ as material. TiO$_2$ was prepared by hydrolysis of TiCl$_4$. In addition, support materials $\alpha$-Al$_2$O$_3$ and $\gamma$-Al$_2$O$_3$ were purchased from Aladdin Industrial Co. Ltd.

Catalysts Ni/$\alpha$-Al$_2$O$_3$, Ni/$\gamma$-Al$_2$O$_3$, Ni/SiO$_2$, Ni/TiO$_2$ and Ni/ZrO$_2$ with 10 wt% Ni loadings were prepared by wet impregnation using Ni(NO$_3$)$_2$$\cdot$6H$_2$O as nickel precursor. Firstly, supporting material dipped into the nickel nitrate solution. Then the solution was heated with continuous stir until water was evaporated to dryness. The obtained residues were dried at 120 $^{\circ}$C overnight and calcinated at 500 $^{\circ}$C for 4 h. The prepared catalyst was crushed into powder with sizes of 100-200 mesh.

The prepared catalyst Ni/$\alpha$-Al$_2$O$_3$ was reduced at 700 $^{\circ}$C while the other catalysts were reduced at 550 $^{\circ}$C for 5 h in H$_2$ atmosphere before using.

B. Catalyst characterization

Brunauer-Emmett-Teller (BET) surface area ($S_{\textrm{BET}}$), average pore diameter, and pore volume of the catalyst were measured by N$_2$ isothermal (-196 $^{\circ}$C) physisorption through Autosorb-iQ-2 (Qudrasorb SI, Quantachrome Instruments). The catalyst was degassed for 12 h at 250 $^{\circ}$C under vacuum condition before N$_2$ adsorption.

H$_2$-temperature programmed reduction (H$_2$-TPR), NH$_3$-temperature programmed desorption (NH$_3$-TPD), and H$_2$-temperature programmed desorption (H$_2$-TPD) measurements were carried out on an automatic chemical adsorption instrument (CBP-1, Quantachrome Instruments) equipped with a thermal conductivity detector. Dispersity of Ni over different supports was calculated with the following formula:

(1)

X-ray diffraction (XRD) analysis of catalyst was carried out on an equipment (PANalytical, Netherlands) with Cu K$\alpha$ ($\lambda$=0.154 nm) radiation. X-ray photoelectron spectroscopy (XPS) analysis of the catalyst was performed on the instrument of Thermo Scientific ESCALAB 250XI using A1 K${\alpha 1, 2}$ radiation as spectra excitation. Thermogravimetry (TG) analysis of the used catalyst was carried out under a flow of air (50 mL/min) on a thermal analyzer (TGA Q50, US). The heating rate is 15 K/min. Transmission electron microscope (TEM) profiles were obtained on a JEM-2100F (JEOL, Japan) instrument equipped with an EDX spectrometer.

C. Catalytic activity test

HDO process of anisole was carried out in a 50 mL stainless steel autoclave equipped with electric mechanical agitator. For each run, catalyst (0.5 g), solvent $n$-octane (21.5 mL) and anisole were loaded into the autoclave. 5.0 MPa H$_2$ was pressured into the reactor after displacing the air. The reactor was heated to a desired reaction temperature while the reagents were stirred at a rate of 800 r/min. Liquid product was collected for subsequent analysis when the reaction was completed.

D. Products analysis

Liquid products obtained from the HDO of anisole were analyzed by gas chromatography (Shimadzu GC-2010 with a FID detector and a DB-5 column) and GC-MS (Agilent 7890A-5975C with DB-FFAP capillary column). The carrier gas was He (99.995% purity), and the oven temperature program increased from 50 $^{\circ}$C (holding for 1 min) to 260 $^{\circ}$C (holding for 10 min) at a rate of 10 $^{\circ}$C/min.

Anisole conversion ($C$) and hydrocarbon yield ($Y_\textrm{h}$) were determined with the following equation:

(2)
(3)
III. RESULTS AND DISCUSSION A. Catalyst characterization

The parameters of the catalysts are shown in Table Ⅰ and the structures are in Fig.S1 (supplementary materials). It was found that all tested catalysts were mesoporous materials. Their average pore diameter is in the range of 7-29 nm, and the most probable pore diameter is in the range of 3-60 nm. Among the investigated catalysts, the average pore diameter and the most probable pore diameter of Ni/$\alpha$-Al$_2$O$_3$ catalyst were the smallest. They were 7.3 and 3.9 nm, respectively. In addition, TEM image of the Ni/$\alpha$-Al$_2$O$_3$ catalyst was presented in Fig.S2 (supplementary material). It can be clearly seen that the metal Ni was well dispersed on the surface of $\alpha$-Al$_2$O$_3$. The size of Ni particle is about 30-40 nm.

Table 1 Parameters of the catalysts

XRD profiles of different catalysts are shown in Fig. 1. The weak and broad characteristic peaks centered at 2$\theta$ of 37.3$^{\circ}$, 43.3$^{\circ}$, and 62.9$^{\circ}$ were assigned to NiO. When XRD characteristic peak of the samples showed a weak and broad peak of NiO species, it actually indicated that NiO particles were very small and widely dispersed on the catalyst support [19]. Notably, the catalyst supported on $\alpha$-Al$_2$O$_3$ showed the smallest NiO crystallite size among the tested catalysts, as shown in Table Ⅰ. The reason might be that NiO well dispersed on the support, suppressing its aggregation.

FIG. 1 XRD profiles of different catalysts

H$_2$-TPR profiles of catalyst are shown in Fig. 2(a). The peaks positioned at lower reduction temperature (usually below 400 $^{\circ}$C) were ascribed to the superficial NiO, which can be easily reduced to Ni$^0$. The peaks at higher temperature were associated with the reduction of bulk NiO, which weakly interacted with support material. It is noteworthy that the reduction peak of Ni/$\alpha$-Al$_2$O$_3$ was centered at 730 $^{\circ}$C, suggesting a stronger interaction between NiO and the support [20].

FIG. 2 (a) H$_2$-TPR and (b) H$_2$-TPD profiles of different catalyst samples

H$_2$-TPD experiments of different catalysts were also carried out, and the results are shown in Fig. 2(b). H$_2$ desorption peaks stepped from about 320 $^{\circ}$C for all investigated catalysts. The quantitative determination based on the H$_2$-TPD profiles demonstrated that the H$_2$ uptakes of Ni/$\alpha$-Al$_2$O$_3$ (976.33 μmol/g) were far more than that of the Ni-based catalysts supported on $\gamma$-Al$_2$O$_3$, SiO$_2$, ZrO$_2$, and TiO$_2$ (as shown in Table Ⅱ). In addition, Ni dispersion degree of Ni/$\alpha$-Al$_2$O$_3$ (13.5%) was also higher than that of other tested catalysts. This conclusion is in good agreement with that of XRD analysis.

Table 2 dispersion and H2 uptakes of different cata- lysts

NH$_3$-TPD experiment was carried out to investigate the acidity of the catalyst. It is widely accepted that peaks at a temperature range of 100-400 $^{\circ}$C are assigned to desorption of NH$_3$ on weak acidic sites and that peaks at a temperature range of 400-600 $^{\circ}$C are assigned to the desorption of NH$_3$ on strong acidic sites. As shown in Fig. 3, a NH$_3$ desorption band was observed in the pattern of Ni/$\alpha$-Al$_2$O$_3$, suggesting the presence of acidic sites. Normally, $\alpha$-Al$_2$O$_3$ is an inertial material. Detected acidic sites were deemed to be created by the introduction of Ni$^{2+}$ cation [20]. It has been reported that trace Ni could be incorporated into $\alpha$-Al$_2$O$_3$ through ion exchange [20]. A broad NH$_3$ desorption band was also observed as expected in the pattern of Ni/$\gamma$-Al$_2$O$_3$ catalyst. Compared with that of Ni/$\alpha$-Al$_2$O$_3$, NH$_3$ desorption peak of Ni/$\gamma$-Al$_2$O$_3$ moved to higher temperature, suggesting stronger acidity. With regard to catalysts of Ni/SiO$_2$ and Ni/ZrO$_2$, relatively small peaks of NH$_3$ desorption were observed, suggesting a small amount of acidic sites. Notably, no NH$_3$ desorption peak was observed in the case of Ni/TiO$_2$.

FIG. 3 NH$_3$-TPD profiles of the different catalyst samples
B. Catalyst testing

Catalytic performances of catalysts and pure support $\alpha$-Al$_2$O$_3$ were evaluated in HDO reaction process with anisole as substrate. As shown in Table Ⅲ, the highest yield of hydrocarbons (90.47%) was obtained over Ni/$\alpha$-Al$_2$O$_3$ catalyst. Cyclohexane was the main component, and its yield was as high as 90.02% (Table Ⅳ). This result indicates that the catalytic performance of $\alpha$-Al$_2$O$_3$ was obviously superior to other catalysts under the same reaction conditions. This can be explained as: H$_2$ uptake of Ni/$\alpha$-Al$_2$O$_3$ was obviously higher than that of other catalysts as discussed in H$_2$-TPD analysis, suggesting more active nickel, thereby causing a better catalytic activity for hydrogenation. In addition, a large number of acidic sites were observed on the surface of Ni/$\alpha$-Al$_2$O$_3$. These acidic sites could co-work well together with active metal sites, and facilitate the HDO reaction [21]. However, the yield of hydrocarbons was rather low (1.47%) when pure support $\alpha$-Al$_2$O$_3$ was used as catalyst, suggesting a negligible catalytic activity for the HDO reaction.

Table 3 Anisole conversions and product yields over different catalysts
Table 4 Different hydrocarbons yields (%) over different catalysts

The conversion of anisole was as high as 99.62% over the catalyst Ni/$\gamma$-Al$_2$O$_3$. The major reason is that strong acidity of catalyst favors activation of the C-O bond, resulting in the cleavage of C$_{\textrm{Ar}}$O-CH$_3$ bond [22]. It was reported that the phenolic compounds could also be converted over the support of $\gamma$-Al$_2$O$_3$ alone [23]. However, compared with that of Ni/$\alpha$-Al$_2$O$_3$ catalyst, the yield of hydrocarbon products was relatively low (only 73.83%). One of the reasons was ascribed to its inefficient hydrogenation activity. For similar reason, the hydrocarbon yields over Ni/SiO$_2$ and Ni/ZrO$_2$ were also relatively low.

It should be noted that the yield of toluene (Table Ⅳ) was 15.91% over the catalyst Ni/$\gamma$-Al$_2$O$_3$. This may also relate to the acidity of the catalyst. Normally, anisole molecule can be adsorbed on the acidic sites due to its well accessible basic oxygen electronic doublet, resulting in the activation of ArO-CH$_3$ bond. The activated ArO-CH$_3$ bond cleaved heterolytically, and the positively charged methyl group can be transferred to aromatic ring, leading to the formation of methylated products [24]. Therefore, it is plausible that the catalyst Ni/$\gamma$-Al$_2$O$_3$ favors the transmethylation due to its strong acidity, yielding higher methylated products during the HDO process of anisole. Similarly, methylated products were also observed over catalysts of Ni/SiO$_2$ and Ni/ZrO$_2$, although it was minor.

In addition, anisole conversion and hydrocarbon yield were relatively poor over the catalyst Ni/TiO$_2$. There are two possible reasons accounting for this. Firstly, H$_2$ uptake of Ni/TiO$_2$ is far less than that of other catalysts as discussed in H$_2$-TPD experiments, suggesting less active nickel. Moreover, the acidity of Ni/TiO$_2$ is almost negligible as discussed in NH$_3$-TPD experiments. Two handicaps resulted in an inferior catalytic activity for HDO reaction. Secondly, the BET surface area, Ni dispersion and porous structure of Ni/TiO$_2$ are clearly inferior to those of other investigated catalysts, which are also unfavorable for the improvement of catalytic activity.

Effects of reaction temperature, time and catalyst dosage on HDO of anisole were investigated carefully using Ni/$\alpha$-Al$_2$O$_3$ as a representative catalyst. As shown in Fig. 4(a), the anisole conversion gradually increased with the increased temperature. The yield of hydrocarbons also increased gradually from 38.90% to 90.47% when the reaction temperature increased from 220 $^{\circ}$C to 300 $^{\circ}$C. However, yield of hydrocarbons swiftly decreased as the reaction temperature further increased from 300 $^{\circ}$C to 340 $^{\circ}$C. In addition, bicyclic compound (phenylcyclohexane) noticeably increased in the products at 340 $^{\circ}$C, suggesting that the intermolecular polymerization took place at a higher temperature. Detailed product distribution was presented in Table S1 (supplementary materials).

FIG. 4 Anisole conversion and hydrocarbon yield varied with (a) temperature, (b) time, and (c) catalyst dosage over Ni/$\alpha$-Al$_2$O$_3$ catalyst. Reaction conditions: (a) catalyst of 0.5 g, anisole of 2.5 g, octane of 21.5 mL, $P_{\textrm{H}_2}$=5.0 MPa, $t$=16 h; (b) catalyst of 0.5 g, anisole of 2.5 g, octane of 21.5 mL, $P_{\textrm{H}_2}$=5.0 MPa, $T$=300 $^{\circ}$C; (c) anisole of 2.5 g, octane of 21.5 mL, $P_{\textrm{H}_2}$=5.0 MPa, $T$=300 $^{\circ}$C, $t$=16 h

Reaction time significantly influenced the HDO reaction of anisole. As shown in Fig. 4(b) and Table S2 (supplementary material), the conversion of anisole and the yield of hydrocarbons gradually increased with reaction time over Ni/$\alpha$-Al$_2$O$_3$. At the beginning of the reaction, the yield of phenol is considerably high, and gradually reduced with reaction time being lengthened. According to this result, it can be speculated that anisole was converted to phenol via demethylation firstly, followed by hydrogenation of aromatic ring to form cyclohexanol and then cyclohexane. The detected cyclohexanol and cyclohexene were other evidences for this presumption. Interestingly, methoxycyclohexane was detected in the products obtained over Ni/$\alpha$-Al$_2$O$_3$, suggesting that hydrogenation of the aromatic ring of anisole could occur prior to the demethylation. Generally, methoxycyclohexane was only mentioned as a reaction intermediate or product over noble metal catalyst due to its efficient hydrogenation activity [25].

The effect of catalyst dosage on the HDO of anisole was also investigated in detail. As shown in Fig. 4(c), the anisole conversion and the hydrocarbons yield gradually increased with the increased catalyst dosage in the investigated range. Generally, higher catalyst dosage implies more catalytic active sites, thereby resulting in better catalytic performance [26]. Therefore, it is plausible that this process is of high catalyst dosage dependence.

The repeatability of Ni/$\alpha$-Al$_2$O$_3$ was also tested. The catalyst was reused directly without any retexture (such as calcination and reduction). As shown in Fig. 5(a), anisole was efficiently converted with high hydrocarbons yield when the catalyst Ni/$\alpha$-Al$_2$O$_3$ was repeatedly used. This result implied that the catalyst Ni/$\alpha$-Al$_2$O$_3$ had a stable catalytic activity for the HDO of anisole. To examine the extent of coke formed during the HDO process, TG analysis of reused catalyst was carried out and the result was exhibited in Fig.S3 (supplementary materials). Only a slight weight loss was observed even if the catalyst was repeatedly reused for five times. This result suggests that the catalyst Ni/$\alpha$-Al$_2$O$_3$ possesses excellent resistance to coking. However, as shown in the XPS patterns of catalysts (Fig. 5(b)), the peak of Ni$^0$ positioned at 852.54 eV became small when the catalyst was repeatedly used for five times. Conversely, the peak of Ni$^{2+}$ positioned at about 856 eV intensified obviously. This result suggests that active metal Ni$^0$ would be oxidized to Ni$^{2+}$ during the HDO process of anisole.

FIG. 5 (a) Catalyst repeatability test and (b) surface chemical state of catalysts. Reaction conditions: catalyst Ni/$\alpha$-Al$_2$O$_3$ of 0.5 g, anisole of 2.5 g, octane of 21.5 mL, $P_{\textrm{H}_2}$=5.0 MPa, $T$=300 $^{\circ}$C, and $t$=16 h
IV. CONCLUSION

Effects of support materials $\alpha$-Al$_2$O$_3$, $\gamma$-Al$_2$O$_3$, SiO$_2$, TiO$_2$, and ZrO$_2$ on catalytic performance of Ni-based catalysts were studied for the HDO of anisole to hydrocarbons. The Ni/$\alpha$-Al$_2$O$_3$ catalyst exhibited the most H$_2$ uptakes and the highest catalytic activity among these investigated catalysts, revealing that the higher hydrogenation activity can promote the HDO of anisole, obtaining higher hydrocarbon yield. Furthermore, the Ni/$\alpha$-Al$_2$O$_3$ catalyst exhibited excellent repeatability for the HDO of anisole. However, the result of XPS analysis of the used catalyst demonstrated that active metal Ni$^0$ was oxidized to Ni$^{2+}$ during the HDO process of anisole when the catalyst was repeatedly used for five times.

Supplementary materials: Table S1 and S2 show the conversion of anisole and product distribution varied with temperature and time, respectively. Figure S1 shows the pore size distribution of the different catalysts. Figure S2 shows the TEM image of Ni/$\alpha$-Al$_2$O$_3$ catalyst. Figure S3 shows the TG curves of Ni/$\alpha$-Al$_2$O$_3$ used in the first and the fifth run.

V. Acknowledgments

This work was supported by the National Natural Science Foundation of China (No.51576198), the National Key Technology R & D Program (No.2014BAD02B01), and the Youth Innovation Promotion Association of Chinese Academy of Sciences (No.2015288).

[1] T. Klein and P. S. Virk M., Energy Fuels. 22 , 2175 (2008). DOI:10.1021/ef800285f
[2] Li X., Xing J., Zhou M., Zhang H., Huang H., Zhang C., Song L.,and Li X., Catal. Commun. 56 , 123 (2014). DOI:10.1016/j.catcom.2014.07.014
[3] Zakzeski J., C. A. Bruijnincx P., L. Jongerius A.,and M. Weckhuysen B., Chem. Rev. 110 , 3552 (2010). DOI:10.1021/cr900354u
[4] L. Kunkes E., A. Simonetti D., M. West R., C. Serrano-Ruiz J., A. Gartner C.,and A. Dumesic J., Sci-ence 322 , 417 (2008). DOI:10.1126/science.1159210
[5] X. Long J., Xu Y., J. Wang T., Q. Yuan Z., Y. Shu R., Zhang Q.,and Ma L., Appl. Energ. 141 , 70 (2015). DOI:10.1016/j.apenergy.2014.12.025
[6] X. Long J., Zhang Q., J. Wang T., H. Zhang X., Xu Y.,and L. Ma L., Bioresour. Technol. 154 , 10 (2014). DOI:10.1016/j.biortech.2013.12.020
[7] X. Long J., F. Wang L., L. Yin B.,and H. Li X., Chem. Eng. Sci. 122 , 24 (2015). DOI:10.1016/j.ces.2014.09.026
[8] H. Zhang X., Zhang Q., A. Chen L., Xu Y., J. Wang T.,and L. Ma L., Chin. J. Catal. 35 , 302 (2014). DOI:10.1016/S1872-2067(12)60733-5
[9] Zhao C., Kou Y., A. Lemonidou A., Li X.,and A. Lercher J., Angew. Chem. Int. Ed. 48 , 3987 (2009). DOI:10.1002/anie.v48:22
[10] H. Zhang X., Zhang Q., J.Wang T., L. Ma L., X. Yu Y.,and G. Chen L., Bioresour. Technol. 134 , 73 (2013). DOI:10.1016/j.biortech.2013.02.039
[11] Zhao and J. A. Lercher C., ChemCatChem. 4 , 64 (2012). DOI:10.1002/cctc.v4.1
[12] Yao G., J. Wu G., L. Dai W., J. Guan N.,and D. Li L., Fuel 150 , 175 (2015). DOI:10.1016/j.fuel.2015.02.035
[13] Q. Yang Y., Luo H., S. Tong G., S. Kevin J.,and T. Tye C., Chin. J. Chem. Eng. 16 , 733 (2008). DOI:10.1016/S1004-9541(08)60148-2
[14] K. Hong Y., W. Lee D., J. Eom H.,and Y. Lee K., Appl. Catal B150 , 438 (2014).
[15] N. Bui V., Laurenti D., Delichere P.,and Geantet C., Appl. Catal B101 , 246 (2011).
[16] Laurent and B. Delmon E., J. Catal. 146 , 281 (1994). DOI:10.1016/0021-9517(94)90032-9
[17] Nie and D. E. Resasco L., J. Catal. 317 , 22 (2014). DOI:10.1016/j.jcat.2014.05.024
[18] C. Xie Z., Wang Y., Wang P.,and Zhang L., Appl. Mech. Mater. 33 , 513 (2014).
[19] B. Qiu S., Zhang X., Y. Liu Q., J. Wang T., Zhang Q.,and L. Ma L., Catal. Commun. 42 , 73 (2013). DOI:10.1016/j.catcom.2013.07.031
[20] M. Sankaranarayanan T., Berenguer A., Ochoa-Hernandez C., Moreno I., Jana P., M. Coronado J., P. Serrano D.,and Pizarro P., Catal. Today 243 , 163 (2015). DOI:10.1016/j.cattod.2014.09.004
[21] Díz E., F. Mohedano A., Calvo L., A. Gilarranz M., A. Casas J.,and J. Rodríguez J., Chem. Eng. J. 131 , 65 (2007). DOI:10.1016/j.cej.2006.12.020
[22] M. de Souza P., C. Rabelo-Neto R., E. P. Borges L., Jacobs G., H. Davis B., Sooknoi T., E. Resasco D.,and B. Noronha F., Acs Catal. 5 , 1318 (2015). DOI:10.1021/cs501853t
[23] Laurent and B. Delmon E., Appl. Catal A109 , 77 (1994).
[24] A. Dwiannoko A., Lee S., C. Ham H., W. Choi J., J. Suh D.,and M. Ha J., Acs Catal. 5 , 433 (2015). DOI:10.1021/cs501567x
[25] Yuan G., L. Lopez J., Louis C., Delannoy L.,and A. Keane M., Catal. Commun. 6 , 555 (2005). DOI:10.1016/j.catcom.2005.05.001
[26] Long J., Shu R., Yuan Z., Wang T., Xu Y., Zhang X., Zhang Q.,and Ma L., Appl. Energ. 157 , 540 (2015). DOI:10.1016/j.apenergy.2015.04.011
Ni/α-Al2O3催化剂作用下苯甲醚的加氢脱氧
汤文武a,c, 张兴华b,c, 张琦b,c, 王铁军b,c, 马隆龙b,c     
a. 中国科学技术大学化学系, 合肥 230026;
b. 中国科学院可再生能源重点实验室, 广州 510640;
c. 中国科学院广州能源研究所, 广州 510640
摘要: 通过化学沉淀法制备了以α-Al2O3、γ-Al2O3、SiO2,TiO2和ZrO2为载体的五种镍基催化剂,以苯甲醚为模型化合物对催化剂进行活性评价,考察载体对加氢脱氧催化反应的影响。实验表明,Ni/α-Al2O3对苯甲醚加氢脱氧反应的催化活性最高。在优化的工况下,苯甲醚的转化率达到93.25%,碳氢化合物收率达到90.47%。H2-TPD测试表明五种镍基催化剂中,Ni/α-Al2O3表面拥有更多的活性金属位,具有更高的加氢催化活性。Ni/α-Al2O3催化剂具有优异的可重复使用性能,反应后催化剂表面的积碳量几乎可以忽略.
关键词: 苯甲醚     加氢脱氧     Ni/α-Al2O3     碳氢化合物