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High-Throughput Screening of Heterogeneous Catalysts for the Conversion of Furfural to Bio-Based Fuel Components

Section Industrial Chemistry, Università di Messina, V.le F. Stagno D’Alcontres 31, 98166 Messina, Italy
Avantium Chemicals, Zekeringstraat 29, 1014 BV Amsterdam, The Netherlands
Author to whom correspondence should be addressed.
Catalysts 2015, 5(4), 2244-2257;
Submission received: 15 November 2015 / Revised: 7 December 2015 / Accepted: 8 December 2015 / Published: 16 December 2015
(This article belongs to the Special Issue Catalytic Conversion of Biomass)


The one-pot catalytic reductive etherification of furfural to 2-methoxymethylfuran (furfuryl methyl ether, FME), a valuable bio-based chemical or fuel, is reported. A large number of commercially available hydrogenation heterogeneous catalysts based on nickel, copper, cobalt, iridium, palladium and platinum catalysts on various support were evaluated by a high-throughput screening approach. The reaction was carried out in liquid phase with a 10% w/w furfural in methanol solution at 50 bar of hydrogen. Among all the samples tested, carbon-supported noble metal catalysts were found to be the most promising in terms of productivity and selectivity. In particular, palladium on charcoal catalysts show high selectivity (up to 77%) to FME. Significant amounts of furfuryl alcohol (FA) and 2-methylfuran (2-MF) are observed as the major by-products.

Graphical Abstract

1. Introduction

The increase in energy consumption and the effects of global climate change on the environment has driven the effort of the scientific community towards the energetic emancipation from fossil fuels. Indeed, the promotion of new, energy-efficient processes to produce fuels and chemicals from more sustainable sources are under constant investigation. For this reason biomass is seen as a potential source of energy and, more specifically, transportation fuels [1].
Since biomass is over-functionalized it requires selective oxygen removal reactions (e.g., hydrogenation, hydrogenolysis, dehydration, decarboxylation) to obtain platform chemicals [2,3,4]. Etherification is an important reaction for the production of biofuels, as it reduces the amount of hygroscopic alcohol groups, and increases both the energy content and cetane number [5,6]. In contrast, the petrochemical industry employs catalytic processes to introduce oxygen in hydrocarbons [7]. Advanced tools such as high-throughput screening and conceptual process development techniques, advanced data mining and computational chemistry can play a pivotal role in quickly finding economically attractive catalysts and/or process conditions [8,9,10].
Hoydonxcs et al. [11] have given an excellent overview of the current industrial production and application of those products. The most relevant of these is furfuryl alcohol, which has its application in foundry resins. Other specialty chemicals are furoic acid, tetrahydrofurfuryl alcohol and 2-methyl furan. Furfural production is a widely established and long existing industry. In fact, the oldest furfural process uses sulfuric acid to convert oat hulls was started in 1921 in Iowa (United States) by the Quaker Oats Company. Today, corncobs and bagasse are the major feedstock for furfural production [11,12]. Furfural is also considered an excellent platform molecule to produce biofuels [13,14]. The production of furfuryl ethers is part of Avantium’s YXY process, which deals with the catalytic conversion of plant based materials into bio-based chemicals and bio-plastics [15].
The current state of the art route for the production of furfuryl ethers is a two-step process. Furfural is first hydrogenated to furfuryl alcohol. This step is followed by a classical Williamson’s reaction, involving an alkali-metal salt of the hydroxyl compound and an alkyl halide [16]. Especially this last step is hazardous and quite expensive. In this work, the focus is to develop a sustainable route to 2-metoxymethylfuran (furfuryl methylether, FME) by reductive etherification of furfural (Scheme 1) and identify the preferable class of heterogeneous catalysts selective in the one pot process. The direct reductive etherification of furfural has not been described in literature, but Bethmont et al. [17,18] have reported this route for several aldehydes to ethers in the presence of hydrogen, using catalysts from the platinum group. Various studies have also reported on the catalytic reductive etherification of chemicals using homogeneous catalysts [19,20,21].
Scheme 1. The direct reductive etherification of furfural to FME.
Scheme 1. The direct reductive etherification of furfural to FME.
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Very few reports refer to the use of heterogeneous catalysts for furanic compounds. Balakrishnan et al. [22] used Pt and Pt/Sn supported on alumina catalysts for the etherification and reductive etherification of 5-hydroxymethyl furfural (HMF). Promising yields up to 60% were reported, but a wider catalyst screening was missing. In order to obtain more knowledge of the reductive etherification and preferably improve the yields, an in-depth catalyst screening is required. Modern advanced tools such as high-throughput screening offer significant potential in this direction [8,9,10].
Given the complexity of the final reaction mixture, as side-products are also detected, two reaction pathways are considered (Scheme 2). The first pathway consists of the formation of furfuryl alcohol (FA) as the intermediate. The FA then undergoes an acid-catalyzed nucleophilic attack by methanol to form the desired ether. This etherification reaction typically requires a strong acid; therefore, the presence of this kind of active site on the support of the catalyst is imperative. The second pathway consists of the formation of the furfural hemiacetal as intermediate, followed by the hydrogenolysis of the formed hemiacetal to obtain the desired ether. This pathway is similar to the pathway suggested by Bethmont et al. [18] for the synthesis of aliphatic ethers from aliphatic aldehydes and alcohols. The furfural acetal is also detected in the reaction mixture and is formed as a consequence of two equilibrium reaction steps (see Scheme 2). It is important to note that the furfural acetal is not considered to be involved in the formation of FME. Bethmont et al. [18] demonstrated that the formation of the ether does not occur by direct hydrogenolysis of the ketal or acetal. Indeed, they postulated that the hemiketal or hemiacetal is dehydrated to the enol ether and the latter is subsequently hydrogenated to the desired ether.
Scheme 2. The two proposed pathways for the reductive etherification of furfural.
Scheme 2. The two proposed pathways for the reductive etherification of furfural.
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Since no efficient catalyst for furfural has been described in literature, a wide range of hydrogenation catalysts was evaluated at several reaction conditions using a high-throughput screening approach. The reductive etherification of furfural to FME is carried out at 50 bar hydrogen pressure for 1 h at 80 to 120 °C. In order to ascertain that the best possible metal catalysts were used in the screening campaign, only commercially available cobalt, nickel, copper, platinum, palladium and iridium-based catalysts on various supports were tested. For each metal, the widest available selection of supports was selected between the commercially available catalysts. Carbon, alumina, silica, titania, calcium carbonate and diatomaceous earths were tested (see Table 1).

2. Results and Discussion

The aim of this research is to identify the most promising family of metal catalysts and reaction conditions for the one-step production of 2-methoxymethylfuran (furfuryl methylether, FME) from furfural, thereby avoiding the synthetic efficiency loss that generally occurs in multistep processes [23]. A high-throughput program screening 35 commercial catalysts at three temperatures and a fixed reaction time, using GC for analysis was conducted. From the reaction scheme in Scheme 2 it can be argued that, in the single step reductive etherification of furfural to FME, a multifunctional catalyst is needed with both a hydrogenation and an acidic function. In particular, the acid centers require special attention as they can also catalyze polymerization processes of furfural and furfuryl alcohol [12,24], leading to fast deactivation of the catalyst.
It is clear that a fair comparison of the catalysts needs to be based on turn-over-frequencies per active metal (TOF). However, to calculate this TOF one needs to determine the available catalytic surface area or, less preferably, the amount of metal. Due to non-analysis agreements this was not possible for all catalysts. The catalysts were therefore compared using the furfural conversion rate, which was expressed in mmol/g metal/h (see Table 1). Within the experimental design, nickel, palladium and platinum catalysts showed high conversion rates and variable yields in the desired FME. Copper and nickel catalysts also gave significant conversions, but minimal amounts of FME were observed. The cobalt molybdenum catalysts showed hardly any activity.
Table 1. Supplier specification and conversion rate of furfural (mmol/g metal/h) for each catalyst tested in the reductive etherification of furfural. “Pre-red” indicates catalysts already present in a “pre-reduced” state.
Table 1. Supplier specification and conversion rate of furfural (mmol/g metal/h) for each catalyst tested in the reductive etherification of furfural. “Pre-red” indicates catalysts already present in a “pre-reduced” state.
No.CatalystSupplier NameSupplier IDFurfural Conversion Rate (mmol/g metal/h)
80 °C100 °C120 °C
1Co/Mo on aluminaCriterionDC2004708701030
2CoO/MoO3 on aluminaUnicatHT-75400570770
3Cu-Zn on aluminaEngelhardA-002409090
4Cu-ZnO on aluminaUnicatMS-900506090
6CuJohnson MattheyPricat Cu 60/35T Copper oxide on an inert carrier50110100
7CuJohnson Matthey40/18 P100170190
8Cu-Cr-BaCRI KataLeunaKL1970-T3130120210
9Ir on active carbonDegussa aL 1082 BB/W 5%138014601720
10Ir on charcoalJohnson Matthey5% Ir on charcoal13601500940
11Ir on calcium carbonate (Pre-Red)Alfa Aesar41305122014601080
12Ir on calcium carbonateAlfa Aesar41305124011401420
13Ni on aluminaCRI KataLeunaKL6562-TL1.270100230
14Ni on special aluminaCRI KataLeunaKL6527-CY1.290100110
15Ni on silicaCRI KataLeunaKL6503-T708060
16Ni on special silicaCRI KataLeunaKL6580110120120
17Ni/MoO3 on silica-aluminaCRI KataLeunaKL9514-CY690800860
18Nysofact 120 catalyst on inert supportEngelhard120605050
19Ni on diatomaceous earthNikki Chemical Co., Ltd.NU1101807090
20Nickel catalyst EngelhardA201507080
21PricatJohnson MattheyPricat NI 55/5 P303030
22PricatJohnson MattheyPricat NI 55/5 T (inert carrier)307090
23HTCJohnson MattheyHTC NI 200 RPS 2.5 mm6080130
24NiMo catalystUnicatHT-86530600730
25Platinum on activated CDegussa aF 1002 RE/W 5% Pt144015601580
26Platinum on titaniaDegussa an.a. b10809801000
27Pt on aluminaDegussa aF 1002 XKYA/W 5%880580520
28Pt(S) on carbon 5% PtJohnson MattheyPt/C Sulfided, 5% Pt Type B106032-5460380440
29Pd on activated carbonDegussa aE 1002 XU/W 5% Pd136013001560
30Pd on CaCO3 powderDegussa aE 407 R/D 5%440840520
31Pd on alumina, JCAT001 (Pre-Red)Johnson MattheyJCAT001149011001160
32Pd on alumina, JCAT001Johnson MattheyJCAT001160160240
33Palladium on graphite (Pre-Red)Johnson MattheyJCAT010178017001630
34Palladium on graphiteJohnson MattheyJCAT0109308701330
35Pd on charcoal powderJohnson Matthey5R87L142014501520
a Degussa, now Evonik; b not available, catalyst prepared on request.
The Space Time Yield (STY) of 2-metoxymethylfuran for all catalysts tested is shown in Figure 1. From Figure 1 it is clear that only palladium, platinum and iridium give a significant STY to the desired FME ether. Palladium based catalysts appear to be the most promising in converting furfural to FME. With charcoal as support a STY of 1125 mmol/g supported metal/h at 100 °C was obtained. Among the platinum catalysts the best STY was also obtained with activated carbon as the support (305 mmol/g supported metal/h at 120 °C). The iridium catalysts gave the lowest STYs to FME, with a maximum value of 162 mmol/g supported metal/h, again with charcoal as the support.
Figure 1. 2-metoxymethyl furan (FME) Space Time Yield (mmol/g supported metal/h) vs. catalyst ID number (see Table 1). Different color marks were used in the figure for the six active metal catalysts: pink (cobalt), grey (iridium), black (palladium), light blue (copper), green (nickel), violet (platinum).
Figure 1. 2-metoxymethyl furan (FME) Space Time Yield (mmol/g supported metal/h) vs. catalyst ID number (see Table 1). Different color marks were used in the figure for the six active metal catalysts: pink (cobalt), grey (iridium), black (palladium), light blue (copper), green (nickel), violet (platinum).
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The variation in activity within one group of metal catalysts can be explained by a number of variables, such as metal loading, support, promoters and/or impurities present. This is inherent to the use of commercial materials from different sources, but using these ascertains that a good activity for the particular metal loading on a support is actually available. Despite the different metal loadings, the results reported in Table 1 strongly indicate that the observed variations are due to specific metal-support interactions. To clarify this, the conversion of furfural for catalysts with 5% w/w metal loading is shown in Figure 2. It can be clearly seen that palladium, platinum and iridium on carbonaceous supports, such as charcoal, graphite and activated carbon, showed the highest activity.
Figure 2. Conversion rate of furfural (mmol/g metal/h) for noble metals at 5% w/w metal loading.
Figure 2. Conversion rate of furfural (mmol/g metal/h) for noble metals at 5% w/w metal loading.
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Figure 3 shows the Space Time Yield (STY) for 2-methoxymethylfuran for 5% w/w palladium, platinum and iridium on various supports. It can be seen that among all carbon supported catalysts, palladium on charcoal had the best performance, both in terms yield and activity. With this catalyst up to 1125 mmol/g metal/h of FME was produced at 100 °C while the furfural conversion rate reached 1450 mmol/g metal/h. Palladium on graphite also showed good results, producing 800 mmol/g metal/h of FME at 120 °C with a furfural conversion rate of 1330 mmol/g metal/h. Instead, iridium and platinum catalysts, although showing high conversions, did not demonstrate significant selectivity to the desired FME.
Figure 3. Space Time Yields (mmol/g metal/h) for 2-methoxymethylfuran production for noble metals with 5% w/w metal loading.
Figure 3. Space Time Yields (mmol/g metal/h) for 2-methoxymethylfuran production for noble metals with 5% w/w metal loading.
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Figure 4 shows the yield percentage to FME versus the conversion of furfural. The line represents 100% selectivity. With palladium on charcoal catalysts a maximum selectivity of 77% was achieved.
Figure 4. Yield percentage to 2-methoxymethylfuran vs. conversion of furfural for noble metals with 5% w/w metal loading. Dashed line represents 100% selectivity to FME.
Figure 4. Yield percentage to 2-methoxymethylfuran vs. conversion of furfural for noble metals with 5% w/w metal loading. Dashed line represents 100% selectivity to FME.
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The reduced palladium on graphite catalysts show a higher selectivity to FME than the equivalent pre-reduced ones, although the conversion rate of furfural is lower (see Table 1). This shows that the reduction procedure with hydrogen promotes the formation of the aimed FME with respect to the other products detected in the case of palladium on graphite catalysts. Iridium and platinum catalysts, although showing significant conversion of furfural, do not have sufficiently high productivity/selectivity to FME.
Our results show poor performance of the Pt/Al2O3 catalyst, which was reported to have good performance in HMF etherification by Balakrishnan et al. [22], albeit in combination with Amberlyst-15, a strongly acidic ion exchange resin. The use of a single catalyst, instead of a combination of two catalysts (especially a combination of an organic resin and an alumina-based catalyst) is preferable from an industrial perspective. The deposition of acid-catalyzed furfural polymerization products on the catalyst surface is expected in long-term operation and the catalyst will require periodic regeneration.
The findings in this screening study are in agreement with those of Bethmont et al. [17] who describe palladium on charcoal catalysts in the direct synthesis of ethers from aliphatic aldehydes and ketones, and primary and secondary alcohols. In their work the good catalytic properties of palladium on charcoal were ascribed to its low efficiency of palladium for the competitive carbonyl reduction into further hydrogenation products. However, they also stated that this synthesis method is limited by the impossibility of using an aromatic aldehyde due to the fast reduction of the carbonyl group to alcohols [18]. This suggests that the reactivity of the carbonyl group plays a crucial role in the one-step reductive etherification of aldehydes. In this respect furfural appears to be an interesting molecule in the reductive etherification to FME. The formation of furfuryl alcohol confirms the aromatic nature of the six electrons on the furan ring. However, furfural is also able to react as an aliphatic aldehyde under our reaction conditions, giving the desired ether in good yields.

Selectivity to Different Product Groups

Regarding the selectivity to different product groups for each type of metal, several trends are observed. The only metal that gave significant amounts of FME was palladium. This metal, however, also showed signs of consecutive hydrogenolysis of the aldehyde group (Figure S1, Supplementary Information). In particular 5% w/w Pd/charcoal, recognized as the most promising catalyst in the reductive etherification of furfural, showed significant selectivity to furfuryl alcohol (FA) as well (around 25%). Moreover, at high temperature (120 °C) the selectivity to 2-methylfuran (2-MF), obtained by further hydrogenolysis of FA, becomes important (always < 10%). 2-MF represents a highly attractive product due to its unique fuel properties and it has recently been proposed as a promising biofuel component, mixed with gasoline [25,26].
The other metal catalysts (iridium, nickel, copper and to a lesser extent platinum) give FA as the main reaction product. These results are in agreement with the industrial use of both copper chromite and Raney nickel catalysts in the synthesis of FA in the gas-phase reaction [27]. In particular, Cu-based catalysts (copper chromite, Raney copper, Cu/Al2O3) have been widely employed, as they do not cleave the C–O bond and only show minor activity in C–C cleavage and ring hydrogenation. However, the use of the toxic chromium based catalyst has serious environmental concerns in its preparation, handling and disposal [26].
Ultimately our data are in accordance with the previous study of Bethmont et al. [17,18] on the synthesis of ethers from aliphatic aldehydes and alcohols, stating the difficulty of obtaining ethers from an aromatic aldehyde. Palladium catalysts on carbonaceous supports were demonstrated to convert the aromatic aldehyde furfural to the desired ether in good yield. Palladium on charcoal showed the highest activity and selectivity to 2-methoxymethylfuran (77%) of all catalysts under the conditions tested.

3. Experimental Section

3.1. Chemicals

Methanol (HPLC gradient grade) was purchased from Biosolve BV (Valkenswaard, The Netherlands). Furfural (99%) and 1,4-Dioxane were purchased from Sigma-Aldrich Chemie BV (Zwijndrecht, The Netherlands).

3.2. Catalysts

The selection of catalysts for the reductive etherification of furfural to FME was focused on traditional active metal catalysts used in industrial hydrogenation. Commercial availability was taken into account. A library of 35 catalysts was composed (see Table 1).
The catalysts were reduced prior to the experiments. The reduction procedure was performed in a tubular oven. Around 0.5–1.0 g of catalyst was reduced using a 7% v/v hydrogen in nitrogen flow of 100 mL/min. The nickel and cobalt catalysts were heated to 350 °C with a ramp of 2 °C/min, then with a rate of 5 °C/min to 450 °C. The catalysts were subsequently kept at 450 °C for 4 h. The copper, iridium, platinum and palladium catalysts were reduced under the same flow composition, but heated up to 200 °C with a ramp of 2 °C/min. The catalysts were then kept at 200 °C for 4 h. After the reduction, all the catalysts were stored under nitrogen in a glove box. Some catalysts were already present in a “pre-reduced” state and were also tested in this form in order to investigate the influence of the reduction procedure on the synthesis of FME.

3.3. Catalytic Testing Procedure

The reductive etherification of furfural was carried out using the Avantium Quick Catalyst Screening (QCS) apparatus (Avantium, Amsterdam, The Netherlands). The QCS is a high-throughput batch system which is capable of running 72 batch reactions simultaneously using 6 blocks consisting of 12 stainless steel autoclaves each. For each experiment 10–20 mg of catalyst was weighted under air followed by the immediate addition of 1 mL 10% w/w furfural in methanol and a small amount of dioxane as internal standard. The QCS blocks were flushed 3 times with nitrogen at 5 bar to remove the oxygen from the reactors, followed by pressurizing with hydrogen to 50 bar at room temperature. The reactor blocks were subsequently placed in the pre-heated heating block. The stirring speed was set at 1000 rpm. The experiments were performed with a fixed reaction time of 1 h at 80, 100 and 120 °C. After completion the reactor blocks were removed from the QCS apparatus and immediately cooled in an ice bath. The samples from the reactors were fully transferred to glass vials and centrifuged. The clear liquid was transferred to vials for GC analysis. A total of 192 reactions were performed, including blanks, duplicates and repeats.
Non-analysis agreements prohibited the determination of the exact metal surface area of the catalysts, preventing the determination of turn-over frequencies. In order to compare the activity of the catalysts, the conversion rate of furfural is normalized per gram of supported metal and expressed as follows:
Conversion rate = mmoles of furfural converted g of supported metal   h
The percentage conversion of furfural is expressed as follows:
Conversion % = mmoles of furfural converted mmoles of furfural in the feed 100
The amount of 2-metoxymethyl furan (FME) formed is expressed in terms of Space Time Yield (STY):
Space Time Yield (STY) = mmoles of FME produced g of supported metal   h
The selectivity of a product is expressed as follows:
Selectivity % = mmoles of FME produced mmoles of furfural converted 100

3.4. Analysis by Gas Chromatography

All standards and samples were analyzed by gas chromatography using a Trace 1310 GC-FID system equipped with a TriPlus RSH autosampler (Thermo Scientific, Bremen, Germany). Samples were injected undiluted with an injection volume of 0.5 μL using a 5 μL syringe (Thermo Scientific, Bremen, Germany). Injection was performed at a temperature of 250 °C and with a split ratio of 1:100. Separation was achieved on a DB-624UI Ultra Inert analytical column (30 m × 0.25 mm × 1.4 μm, Agilent Technologies, Palo Alto, CA, USA). Helium was used as a carrier gas with a constant flow rate of 2.5 mL/min. The GC oven was held at 50 °C for 1 min, then ramped to 250 °C at 40 °C/min and finally held at 250 °C for 1 min. The FID was operated at 250 °C, with a H2/air ratio of 10% and an air flow of 350 mL/min. A representative chromatogram of the final reaction mixture is shown in Figure S2 (Supplementary Information).

4. Conclusions

The results of this work clearly indicate that palladium is the metal of choice for the direct formation of 2-metoxymethylfuran (FME) from furfural. Carbon-based supports, i.e., activated carbon, charcoal and graphite are preferred. This was shown by the high activity and selectivity of the commercial catalysts with both these functionalities in the one-pot reductive etherification. Carbon supports generally possess a high specific surface area, a developed pore space and especially controllable chemical surface properties. The functionalities present in the form of surface oxides (e.g., carboxylic, phenolic, lactonic, ether groups) are responsible for both the acid/base and redox properties of the activated carbon, and for the anchoring of the metal particles, resulting in good metal dispersion.
Further optimization of this catalytic system is needed, because 5% w/w Pd on charcoal did not demonstrate sufficient selectivity to 2-metoxymethylfuran (FME), with significant amounts of furfuryl alcohol (FA) and 2-methylfuran (2-MF) as the major by-products. Carbon supports are widely used for noble metal hydrogenation catalysts, including in the hydrogenation furfural [28], due to their wide range of specific surface areas, tailored pore size distributions and controllable chemical surface properties [29].
Since the acidity of the support in the reductive etherification of furfural, as assumed from our work and in the work of Bethmont [17,18], plays a crucial role in the mechanism of FME formation, a further study of the support surface as well as of the size and dispersion of the metal particles is imperative. The acidity of the carbon support is related to the functionalization treatment of the carbon itself, and can be improved by doping and other methods [30].
In conclusion, this study has identified the Pd on charcoal as the preferable catalyst for the direct reductive etherification of furfural, and provides indications on aspects for further improvement. Moreover, it is possible to affirm that furfural, although it is an aromatic molecule, undergoes the direct etherification to FME with 5% w/w Pd on charcoal catalyst in good yields. This aromaticity could be a limitation in the direct synthesis of ethers from aldehydes and alcohols as stated by Bethmont et al. [17,18], because of the competitive reduction of the carbonyl group to furfuryl alcohol. Nevertheless, the actual performances are already largely superior to those for the catalysts earlier reported in literature. This study is an important starting point for the further optimization of this reaction and the required catalysts.

Supplementary Files

Supplementary File 1


The European community IAPP is gratefully acknowledged for funding through the European Project Marie Curie, Industry-Academia Partnerships and Pathways (IAPP), BIOpolymers and BIOfuels from FURan based building blocks “BIOFUR”, FP7-PEOPLE-2012. The authors also gratefully acknowledge the “YXY-Fuels” project, granted by Agentschap NL, The Netherlands.

Author Contributions

The experimental work, data collection and data analysis were performed by Roberto Pizzi under the supervision of Jan Cornelis van der Waal. The manuscript was written by Roberto Pizzi in close collaboration with Jan Cornelis van der Waal and Robert-Jan van Putten. Hanneke Brust was responsible for the analytics and developed the GC method and wrote the corresponding part in the manuscript. Gabriele Centi and Siglinda Perathoner supervised and warranted the scientific scope of the study. All authors fully contributed to the revision of the manuscript.

Conflicts of Interest

The authors declare no conflict of interest.


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MDPI and ACS Style

Pizzi, R.; Van Putten, R.-J.; Brust, H.; Perathoner, S.; Centi, G.; Van der Waal, J.C. High-Throughput Screening of Heterogeneous Catalysts for the Conversion of Furfural to Bio-Based Fuel Components. Catalysts 2015, 5, 2244-2257.

AMA Style

Pizzi R, Van Putten R-J, Brust H, Perathoner S, Centi G, Van der Waal JC. High-Throughput Screening of Heterogeneous Catalysts for the Conversion of Furfural to Bio-Based Fuel Components. Catalysts. 2015; 5(4):2244-2257.

Chicago/Turabian Style

Pizzi, Roberto, Robert-Jan Van Putten, Hanneke Brust, Siglinda Perathoner, Gabriele Centi, and Jan Cornelis Van der Waal. 2015. "High-Throughput Screening of Heterogeneous Catalysts for the Conversion of Furfural to Bio-Based Fuel Components" Catalysts 5, no. 4: 2244-2257.

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