Cellulose Conversion to 5 Hydroxymethyl Furfural (5-HMF) Using Al-Incorporated SBA-15 as Highly Efficient Catalyst

Pham, Son Tung; Nguyen, Manh B.; Le, Giang H.; Pham, Trang T. T.; Quan, Trang T. T.; Nguyen, Trinh Duy; Son, Thanh Le; Vu, Tuan Anh

doi:https://doi.org/10.1155/2019/5785621

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Advanced Nanomaterials for Green Growth

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Volume 2019 | Article ID 5785621 | https://doi.org/10.1155/2019/5785621

Cellulose Conversion to 5 Hydroxymethyl Furfural (5-HMF) Using Al-Incorporated SBA-15 as Highly Efficient Catalyst

Son Tung Pham,^1,2Manh B. Nguyen,^1,3Giang H. Le,¹Trang T. T. Pham,^1,4Trang T. T. Quan,¹Trinh Duy Nguyen,⁵Thanh Le Son,²and Tuan Anh Vu^1,4

Academic Editor: Elena Gomez

Received14 Mar 2019

Revised01 Jun 2019

Accepted02 Jul 2019

Published07 Aug 2019

Abstract

Al-incorporated SBA-15 samples (xAl/SBA-15) were successfully prepared by “atomic implantation” method. The samples were characterized by X-ray diffraction spectroscopy (XRD), transmission electron microscopy (TEM), energy-dispersive X-ray spectroscopy (EDX), N₂ adsorption-desorption isotherms (BET), and temperature-programmed desorption (NH₃-TPD). In this catalyst, metal oxide species were highly dispersed on the SBA-15 surface and existed as isolated atoms. It was shown that the Al incorporation lead to the formation of medium and strong acid sites. The catalytic activity and selectivity were tested in a mild hydrothermal process for degradation of cotton cellulose to 5-hydroxymethyl furfural (5-HMF). A cellulose conversion of 68.5% and 5-HMF selectivity of 62.1% after 2 h of reaction at 170°C were achieved. The very high 5-HMF yield (42.57%) obtained in this paper is much higher than that was reported in the literature.

1. Introduction

In recent years, the process of biomass conversion to hydrocarbon fuels has received much attention due to the limited fossil fuels resource, demanding the alternatives to obtain biofuels. Biomass is as well known as carbon renewable energy resources for the production of bio-oil by the fast pyrolysis technology. However, bio-oil is composed of different compounds with high oxygen content and low chemical stability and, therefore, cannot be used as biofuels. Recently, great efforts have been made to develop practical pathways to transform biomass-derived carbohydrates into chemicals and fuels. 5-Hydroxymethyl furfural (5-HMF) has a versatile range of applications and can be obtained from the chemical conversion of C₆ carbohydrates. The conversion of cellulosic biomass to valuable chemicals such as 5-hydroxymethyl furfural, which is often termed the “sleeping giants,” is currently one of the most interests of worldwide research and developments to foster a biobased economy [1]. Therefore, considerable efforts devoted to the depolymerization of cellulose to obtain 5-HMF as a promising bio-oil.

Due to its high degree of crystallinity and stability, hydrolysis of cellulose was often carried out in acidic medium using acids like H₂SO₄, HCl, and HF. In the rigorous reaction condition, the experimental equipment must have high corrosion resistance. Besides, high concentration of inorganic acid used in the reaction can cause extremely negative impacts on surrounding environment. Conversion of cellulose to 5-HMF by using solid acid catalysts under hydrothermal conditions is an environment-friendly chemical process, and it is easy to separate products by filtration. Interestingly, after the reaction, the catalyst can be easily recovered and reused. The SO₄²⁻/ZrO₂-Al₂O₃ catalysts were employed in glucose hydrolysis in hot water which led to a 5-HMF conversion 39% [2]. Zhang et al. stated the preparation of SO₄²⁻/ZrO₂ on TiO₂ and showed high conversion of glucose into 5-HMF [3]. The combined yield of 5-HMF and levulinic acid reached 28.8% in the presence of SO₄²⁻/ZrO₂-TiO₂ when the Zr : Ti molar ratio was 5 : 5 after 2 h of reaction at 170°C.

The advantage of the use of SBA-15 material as catalyst support includes its well-ordered hexagonal mesoporous silica structure with high surface-to-volume ratio, high permeability, variable framework compositions, and high thermal stability [4–6]. However, the electrically neutral framework of purely siliceous SBA-15 gives a rise to its lack of functionality. As a result, it normally plays a role of adsorbent, not acidic or redox catalysts [7, 8]. In order to be used as acidic or redox catalysts, SBA-15 should be modified by incorporation of transition metals into framework using direct and/or postsynthesis [9–17]. Aluminium ions (Al³⁺) insertion into the SBA-15 creates acid sites in the structure which is extremely important for acid-catalyzed reaction. However, the incorporation of aluminium into Al/SBA-15 is difficult because of the difference in hydrolysis rates of Al and Si in low pH medium during the SBA-15 synthesis process [18]. Various synthetic methods have been devoted for the incorporation of higher amounts of aluminium to achieve higher acid sites [14, 16, 17].

In this paper, we report a novel method to incorporate aluminium ion into the SBA-15 framework by atomic implantation and use it as an efficient catalyst for conversion of cellulose to HMF. Effects of reaction temperature and catalyst dosage were also investigated.

2. Experimental Methods

2.1. Preparation of SBA-15

Synthesis of SBA-15 material was done as follows: 1 g of poly (ethylene glycol)-block-poly (propylene glycol)-block-poly (ethylene glycol) (P123) was dissolved in 60 mL of HCl (2 M) and stirred for few hours until a clearly surfactant solution was obtained. Sodium silicate solution ∼27% SiO₂ (Sigma-aldrich) was added dropwise into the surfactant solution with vigorous stirring for 2 hours; then, the mixture was further stirred for 24 hours at 45°C, and the obtained mixture was poured into Teflon lined and autoclave hydrothermal treatment was performed in an oven at 100°C for 24 h. Finally, the white solid product was washed, dried at 80°C overnight, and calcined at 550°C for 6 h in air.

2.2. Preparation of xAl/SBA-15

Al incorporate was carried out by atomic implantation method using AlCl₃ (99,99%, Sigma-aldrich) as Al source [19]. In order to obtain 1Al/SBA-15 with different Al loading, we deposited Al by repeating the Al deposition time. AlCl₃ first deposited on SBA-15 which was prepared previously (denoted 1Al/SBA-15 sample). Use of 1Al/SBA-15 as starting material, we deposited the second Al layer on 1Al/SBA-15 to obtain 2Al/SBA-15 and use of 2Al/SBA-15 as starting material we deposited the third Al layer (denoted 3Al/SBA-15 sample). The reactor was a quartz tube (2 cm × 25 cm) in which amount of AlCl₃ was introduced on one side and an opposite side placed a determined amount of SBA-15.

Reactor was heated to 350°C, and AlCl₃ evaporated and passed through substrate of SBA-15 by flowing carrier gas (N₂). The reaction time was varied between 0.5 h to 1 h. Then the sample was calcined at 500°C to remove chloride.

2.3. Characterization of Materials and Membrane

The morphology characteristics of the materials were analyzed by transmission electron microscopy (HITACHI-H-7500). The pore structure of all resulting solids was determined by nitrogen adsorption-desorption isotherms at 77 K using TriStar Plus II. The powder X-ray diffraction patterns of the samples were recorded on a D8 Advance analyzer with Cu Kα radiation (l = 1.5417 Å). The chemical composition of the samples was analyzed by EDX, on JED-2300 analysis Station (JEOL) machine. The acid sites were measured by using NH₃-TPD (model: Autochem II). The ammonia concentration in the effluent gases was determined by a thermal conductivity detector.

2.4. Catalytic Test

The investigation of catalytic degradation of cotton cellulose was carried out in a high-pressure batch stainless-steel reactor equipped with a liner of polytetrafluoroethylene (PTFE). The cotton cellulose, solid acid catalysts, and water were thoroughly mixed in the reactor; then, the mixture was heated in the oven. Some effects of operation parameters were mainly investigated such as catalyst type and dosage, reaction temperature, and time on the cellulose saccharification to glucose and the monosaccharide dehydration to 5-HMF. After the reaction, the mixture of solution and solid reactants were separated by filtration.

The cellulose conversion, selectivity, and yield 5-HMF were calculated by the following equation:

3. Results and Discussion

3.1. X-Ray Diffraction Spectroscopy (XRD)

Figure 1(a) shows the low-angle X-ray diffraction patterns of xAl/SBA-15. In the XRD pattern, the one peak with strong intensity in the 2θ angle of∼1.02°, two peaks with weak intensity at 2θ angle of∼1.6° and 2θ∼1.8°, corresponding to the diffraction of (100), (110), and (200) reflection, respectively, which are characteristic for the structure of 2D hexagonal p6 mm symmetry of mesoporous SBA-15 structure [19, 20]. In the wide angle (Figure 1(b)) XRD pattern of the xAl/SBA-15, no diffraction lines of crystalline Al oxide in xAl/SBA-15 samples were observed. This can be explained by the fact that almost all Al incorporated into SBA-15 framework; therefore, the phase of Al₂O₃ could not be detected by [5].

(a)

(b)

As shown in Table 1, the Rietveld refined parameter of the crystal structure of these samples was slightly changed with different Al incorporated into SBA-15 framework. This is related to the substitution of metal ions (Al) for Si in the SBA-15 framework. Because the ionic radius of Al³⁺ (0.51 Å) is greater than Si⁴⁺ (0.41 Å), the Al-O bond lengths are longer than Si-O bond, leading to increase in d₁₀₀ and a₀ parameters [7, 17, 21]. This result strongly confirms that Al incorporation into SBA-15 framework.

3.2. N₂ Adsorption-Desorption Isotherms (BET)

Figure 2 shows the N₂ isotherms and pore size distribution of calcined SBA-15 and xAl/SBA-15. It can be seen from N₂ isotherms of these samples that the hysteresis loops indicated the typical feature of mesoporous materials owing to the capillary condensation. The increase in N₂ amount adsorbing on the material is clearly observed which is resulted from the multilayer adsorption in the formed mesopore [16, 19]. This indicates that the samples have a large pore size (5.5 nm for SBA-15 and 5.5–5.8 nm for xAl/SBA-15). The high degree of mesopore ordering leads a sharp inflection at relative pressures (P/P₀) between 0.6 and 0.8 which is consistent with well-defined 3 nm mesopores. The BET surface areas of SBA-15 and xAl/SBA-15 (Table 2) were strongly decreased from 668 m²/g to 143 m²/g, respectively. This result can be explained that the new small Al oxides particles were formed and located along to the channels, causing the decrease of surface area. As seen in Table 2, the SBA-15 sample had a pore diameter of 5.50 nm and a wall thickness of 5.51 nm, while xAl/SBA-15 samples showed a slight increase of pore diameter and wall thickness. This result clearly indicated that the new mesopore system was formed and located along to the pore SBA-15 system [11, 22].

(a)

(b)

3.3. Transmission Electron Microscopy (TEM) and Energy-Dispersive X-Ray Spectroscopy (EDX)

The transmission electron microscopy (TEM) images of SBA-15 and xAl/SBA-15 samples are illustrated in Figure 3. The TEM image of SBA-15 display well-ordered hexagonal arrays of mesopore with one-dimensional channels, indicating a 2D hexagonal (p6 mm) mesostructure. The average wall thickness was ∼5-6 nm, with similar width pore diameters determined by BET. As seen in Figures 3(b)–3(d), the pore and wall thickness of Al incorporated SBA-15 were not uniform as compared to those of pure SBA-15. Especially, for the Al-incorporated SBA-15 sample with high Al content (3Al/SBA-15), Al oxide particles covered the surface, no pores and wall of SBA-15 were observed.

(a)

(b)

(c)

(d)

The results of EDX in Figure 4 and Table 3 show that the Al element contents (5.6, 9.7, and 12.5%) deposited on the xAl/SBA-15 were approximately equal to the value calculated. From Figure 4, it was noted that the Al loading was increasing. Thus, at high Al loading (3Al/SBA-15), the intensity of Al peak was higher than that of medium loading sample (2Al/SBA-15). However, when Al content was too high, Al content determined by EDX is lower than calculated amount. This due to the saturation of Al deposited on SBA-15 surface. The 3Al/SBA-15 sample was prepared by deposition the third Al layer on 2Al/SBA-15 sample. In this case, penetration of Al into SBA-15 is hindered by the two Al layers which previously deposited on SBA-15, leading to the saturation.

(a)

(b)

(c)

3.4. Temperature-Programmed Desorption (NH₃-TPD)

It is well known that cellulose hydrolysis is catalysized the by acid catalyst. The cellulose conversion is strongly depended on the acidity of the catalysts. To determine the acidity of Al incorporated SBA-15, we used the NH₃-TPD method [14]. Figure 5 shows NH₃-TPD profiles of Al incorporated SBA-15. Amounts of weak (<200°C), medium (250–300°C), and strong (500–550°C) acid sites are listed in Table 4. As observed in Figure 5 and Table 4, the pure SBA-15 possessed only weak acid sites (max desorption temperature < 200°C), while Al incorporated SBA-15 samples showed large amount of medium and strong acid sites (Table 4). Among them, 2Al/SBA-15 had the highest amount of medium acid sites (T_max∼250–300°C). This may be due to the Al amount incorporated into SBA-15 is suitable, favoring to form medium and strong acid sistes (isolated Al sites formation). In the case of 3Al/SBA-15, amount of acid sites is lower than that of 2Al/SBA-15. This can be explained the formation of Al₂O₃ particles which cover the acid sites created after the second Al layer deposition (2Al/SBA-15 sample).

3.5. Catalytic Activity

Table 5 shows that the conversion, selectivity, and yield of 5 HMF over SBA-15 and xAl/SBA-15 catalysts. We have tested the SBA-15 and this showed almost no catalytic activity. Conversion of cellulose to 5-HMF is catalyzed by acid sites since only small amount of weak acid sites in SBA-15 was noted (Table 4). Among Al-incorporated SBA-15 samples, 2Al/SBA-15 catalyst exhibited the highest yield of 5-HMF (42%). This value was higher than that reported in the literature [23–26]. Some previous works stated the low 5-HMF yield (10–20%). According to the proposed mechanism, cellulose hydrolyzed under the action of a catalyst will be converted into glucose and then isomerized to fructose and fructose followed the hydration convered into 5-HMF [27, 28]. The process of converting cellulose into glucose requires strong acidic centers, while the isomerization and dehydration process requires medium acidic centers. Therefore, in order to obtain the high 5-HMF from cellulose hydrolysis it needs both the medium and strong acid sites. However, for the sample contained high amount of very strong acid sites like ZrO₂ sulfated SBA-15, the cellulose conversion was very high but the 5-HMF selectivity was low due to the formation of intermediate products (result unpublished). This also occurred for Al-incorporated SBA-15. Thus, Figures 6(a) and 6(b) illustrate the formation of by-products such as pentanoic acid (C₅H₈O₃), 1,2,4-cyclopentanetriol (C₅H₁₀O₃); cyclotrtrasiloxane, and octamethyl (C₈H₂₄O₄Si₄).

(a)

(b)

To investigate the effect of catalyst dosage and reaction temperature on cellulose conversion, catalyst dosage raging from 0.2 g to 0.4 g and reaction temperature ranging from 150°C to 190°C were tested. As seen in Figure 7, catalyst dosage of 0.2 g (Figure 7(a)) and reaction temperature at 170°C (Figure 7(b)) are optimal condition for cellulose conversion. The dosage of 0.2 g is sufficient for converting cellulose to 5-HMF, introduction of high dosage of 0.3 g-0.4 g leads to the catalyst excess which cause the further conversion of 5-HMF to the by product like levulinic, formic acid. The 4-HMF yield in the cellulose conversion to 5-HMF at 150°C increased with increasing reaction time from 0 to 4 h and then maintained unchanged for prolongation time to 6 h. At higher temperature (170°C), 5-HMF yield increased because the reaction is thermodynamically favored at a high temperature. Further increase of temperature (190°C) did not lead to the increase of 5-HMF yield but it decreased. This can be explained at very high temperature, glucose formed from cellulose hydrolysis is dehydrated forward the anhydroglucose which is thermodynamically favored at very high reaction temperature [29]. Moreover, prolongation of reaction time favored the formation of by-products including formic, acetic, levulinic, and glycollic acid [27].

(a)

(b)

4. Conclusions

Al-incorporated SBA-15 samples were successfully prepared by atomic implantation method. From XRD result, it revealed the mesoporous structure of Al-incorporated SBA-15. TEM images showed that aluminium oxide species were well dispersed and located along the SBA-15 channels. Al incorporation into SBA-15 framework created the weak, medium, and strong acid sites.

Among Al-incorporated SBA-15 samples, 2Al/SBA-15 exhibited the highest yield of 5-HMF (yield 42%). The yield obtained in this study is much higher to that reported in the literature.

Data Availability

The data used to support the findings of this study are available from the corresponding author upon request.

Conflicts of Interest

The authors declare that they have no conflicts of interest.

Acknowledgments

The authors thank the Vietnam Academy of Science and Technology (VAST) for financial support project (TĐPCCC.03/18–20).

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Copyright © 2019 Son Tung Pham et al. This is an open access article distributed under the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.

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Journal of Chemistry

Advanced Nanomaterials for Green Growth

Cellulose Conversion to 5 Hydroxymethyl Furfural (5-HMF) Using Al-Incorporated SBA-15 as Highly Efficient Catalyst

Abstract

1. Introduction

2. Experimental Methods

2.1. Preparation of SBA-15

2.2. Preparation of xAl/SBA-15

2.3. Characterization of Materials and Membrane

2.4. Catalytic Test

3. Results and Discussion

3.1. X-Ray Diffraction Spectroscopy (XRD)

3.2. N2 Adsorption-Desorption Isotherms (BET)

3.3. Transmission Electron Microscopy (TEM) and Energy-Dispersive X-Ray Spectroscopy (EDX)

3.4. Temperature-Programmed Desorption (NH3-TPD)

3.5. Catalytic Activity

4. Conclusions

Data Availability

Conflicts of Interest

Acknowledgments

References

Copyright

3.2. N₂ Adsorption-Desorption Isotherms (BET)

3.4. Temperature-Programmed Desorption (NH₃-TPD)