## 3 Results
### Catalytic Investigations  
The HDO of FAc has a complex reaction network which has recently been investigated by [PERSON] et al. (2019) and whose detailed reaction pathways have not yet been fully understood. The reaction scheme used in this study (Figure 1) has been adapted from a recent investigation of the HDO of FAc in aqueous phase by [PERSON] et al. (2019). Furthermore, some of the reaction products observed are grouped to enable easier data processing of the multicomponent reaction mixture and to better highlight the hydrogenation (redox) and acidic properties of the metal/polymer-silica composite catalysts. In the context of this categorization, the concentration over reaction time profile for the grouped reactants in the HDO of FAc using (1)Pt(13)PSC is given in Figure 2. The results support the reaction mechanism proposed in Figure 1 and can be considered representative for the HDO of FAc using bifunctional metal/polymer-silica composite catalysts as conducted in this study. The allylic double bond of FAc is hydrogenated first to form 4-(2-Furyl)-2-butanone (**A**) which is consistent with literature reports ([PERSON] et al., 2019). Then, (**A**) is further hydrogenated to the products that are considered \"half-hydrogenated (HH)\" in this study. The acid-catalyzed ring-opening reaction then happens in a consecutive reaction step. However, the hydrogenation can also occur before the ring opening. [PERSON] et al. (2019) furthermore pointed out that the acid-catalyzed ring opening of biomass-derived furan rings depends on the substitution pattern of the furan ring. Since this pattern can change during the reaction due to acid-catalyzed isomerization reactions ([PERSON] et al., 2019; [PERSON] et al., 2019), the position of the ring opening is affected by multiple factors. \begin{table}
\begin{tabular}{c c c c c c} \hline \hline
**Catalyst** & **A\({}_{\text{BET}}\)/(m\({}^{2}\) g-1)** & **V\({}_{\text{pore}}\)/(cm\({}^{3}\) g-1)** & **d\({}_{\text{pore}}\)/nm** & **Polymer** & **Metal** \\  & & & & **Content/wt.\%** & **Content/wt.\%** \\ \hline (1)Pt(0)PSC & 182 & 0.40 & 9.1 & 0.0 & 0.91 \\ (1)Pt(6.5)PSC & 168 & 0.38 & 9.0 & 6.3 & 0.95 \\ (13)PSC & 134 & 0.30 & 9.2 & 13.1 & n.d. \\ (0.5)Pt(13)PSC & 125 & 0.29 & 9.0 & 12.7 & 0.43 \\ (1)Pt(13)PSC & 131 & 0.35 & 8.9 & 12.6 & 0.92 \\ (2)Pt(13)PSC & 130 & 0.33 & 9.1 & 12.8 & 1.83 \\ (1)Pt(26)PSC & 105 & 0.24 & 9.5 & 25.1 & 0.95 \\ (1)Pd(13)PSC & 133 & 0.33 & 8.9 & 12.8 & 0.92 \\ (1)Ru(13)PSC & 115 & 0.34 & 9.0 & 12.5 & 0.96 \\ \hline \hline \end{tabular}
\end{table} 
Table 1: Specific surface area \({}_{\text{BET}}\), specific pore volume V\({}_{\text{pore}}\), and average pore width d\({}_{\text{pore}}\) determined from N\({}_{2}\) sorption at \(-\)196 \({}^{\circ}\)C as well as polymer content determined by thermogravimetric analysis (TGA) and metal content determined via inductively coupled plasma optical emission spectrometry (ICP-OES) for different noble metal-loaded polymer–silica composite (PSC) catalysts. Since in the literature the HDO of FAc has been carried out at a wide variety of different H\({}_{2}\) pressures (from 10 [30] to 120 bar [16]), first an investigation of the influence of the hydrogen pressure on the product composition in the HDO of FAc was conducted (Figure 3). Upon increasing the hydrogen pressure from 30 to 60 bar, an increase in \(n\)-octane in the product fraction from 0.20 to 0.68 was observed. This is in agreement with the findings by [PERSON] et al. [30], where also an increase in \(n\)-octane yield with increasing hydrogen pressure for the HDO of FAc using Pd/NbOPO\({}_{4}\) as a catalyst and cyclohexane as a solvent in a fixed-bed reactor was observed in a pressure range from 10 to 20 bar. Above a hydrogen pressure of 60 bar, no influence on the product composition was observed. Thus, to fully exclude an influence of hydrogen pressure on the results obtained, all other reactions were carried out at a hydrogen pressure of 100 bar.