The Transfer Hydrogenation of Cinnamaldehyde Using Homogeneous Cobalt(II) and Nickel(II) (E)-1-(Pyridin-2-yl)-N-(3-(triethoxysilyl)propyl)methanimine and the Complexes Anchored on Fe3O4 Support as Pre-Catalysts: An Experimental and In Silico Approach

The imino pyridine Schiff base cobalt(II) and nickel(II) complexes (C1 and C2) and their functionalised γ-Fe3O4 counterparts (Fe3O4@C1 and Fe3O4@C2) were synthesised and characterised using IR, elemental analysis, and ESI-MS for C1 and C2, and single crystal X-ray diffraction for C1, while the functionalised materials Fe3O4@C1 and Fe3O4@C2 were characterized using IR, XRD, SEM, TEM, EDS, ICP-OES, XPS and TGA. Complexes C1, C2 and the functionalised materials Fe3O4@C1 and Fe3O4@C2 were tested as catalysts for the selective transfer hydrogenation of cinnamaldehyde and all four pre-catalysts showed excellent catalytic activity. Complexes C1 and C2 acted as homogeneous catalysts with high selectivity towards the formation of hydrocinnamaldehyde (88.7% and 92.6%, respectively) while Fe3O4@C1 and Fe3O4@C2 acted as heterogeneous catalysts with high selectivity towards cinnamyl alcohol (89.7% and 87.7%, respectively). Through in silico studies of the adsorption energies, we were able to account for the different products formed using the homogeneous and the heterogeneous catalysts which we attribute to the preferred interaction of the C=C moiety in the substrate with the Ni centre in C2 (−0.79 eV) rather than the C=O (−0.58 eV).


Introduction
The difficulty in separating products from homogeneously catalyzed hydrogenation reactions is a major disadvantage that limits the use of homogeneous catalysts for industrial production, despite their often-high catalytic activities compared to heterogeneous catalysts [1]. The use of water-soluble catalysts and supported catalysts are some of the strategies employed towards improving the recyclability of homogeneous catalysts. Supported catalysts have gained scientific interest as they are intermediates between homogeneous and heterogeneous catalysts [2]. Catalytic systems with a ligand bearing the alkoxy(alkyl)silane moiety offer potential for attaching a solid support to the catalytic system through covalent bonding between the hydroxyl moiety of the support and the alkoxide groups on the ligand [3], which provides sustainable and recyclable active catalysts, as the support improves product isolation and recyclability of the catalysts without the use of solvents [4]. The structure of supported catalysts dictates their activity, and it is hence vital that we study the structure and reactivity of the unsupported catalyst alkoxy(alkyl)silane moiety offer potential for attaching a solid support to the catalytic system through covalent bonding between the hydroxyl moiety of the support and the alkoxide groups on the ligand [3], which provides sustainable and recyclable active catalysts, as the support improves product isolation and recyclability of the catalysts without the use of solvents [4]. The structure of supported catalysts dictates their activity, and it is hence vital that we study the structure and reactivity of the unsupported catalyst in comparison with the supported catalysts to gain better understanding of the activity, selectivity, and other effects of the support [2].
The catalytic hydrogenation of organic compounds possessing multiple unsaturated bonds, such as α, β-unsaturated aldehydes using both homogeneous and heterogeneous catalysts is particularly challenging, which hence requires active catalytic sites that can discriminate between the closely related moieties [5,6]. Cinnamaldehyde (CAL) is an example of an α, β-unsaturated aldehyde which can be converted to valuable chemical intermediates by hydrogenation of either the olefinic or the carbonyl moieties using homogeneous catalysts. Owing to the presence of different chemical moieties in varying chemical environments, it is a better subject for a comparative study on the catalyst activity and selectivity than other substrates such as furfural [7]. Chemoselective hydrogenation of cinnamaldehyde leads to the formation of either hydro-cinnamaldehyde (HCAL), cinnamyl alcohol (COL), or hydro-cinnamyl alcohol (HCOL) (Scheme 1) [6]. HCOL and COL are important intermediates in the production of cosmetics, fragrances and flavourings, while HCAL is used as an intermediate in the production of drugs used for HIV treatment [7][8][9]. The reduction of the unsaturated moieties in cinnamaldehyde by hydrogen molecules proceeds through the 1,2 or 1,4 addition pathways (Scheme 1). Since the 1970s, supported nickel [10], palladium [11,12], and cobalt [13] catalysts have been shown to hydrogenate olefins [14]. Supported cobalt [14][15][16] catalysts in particular are known to be selective in the hydrogenation of the olefinic bond in subtrates that contain both the olefinic and carbonyl bonds [16]. In view of the above, it is critically important to determine the structure of molecular compounds that are used as catalysts, especially if such compounds have bidentate ligands that could render these compounds polymeric, in order to establish how such compounds act as catalysts [17,18]. There are only limited reports in the literature on the use of supported catalysts in the hydrogenation process and comparing their catalytic activity and selectivity to their homogeneous counterparts, either computationally (in silico) or by experimental methods, is therefore highly relevant for progress in this field.
The aim of this study was to employ unsupported and supported catalysts for hydrogenation reactions, and the use of in silico methods to elucidate the selectivity of the supported catalyst in comparison with their homogeneous analogues. As such, this report first presents the synthesis and characterisation of homogeneous Co 2+ and Ni 2+ N-(1-(pyridin-2-yl)ethylidene)-3-(triethoxysilyl)-1-propanamine pre-catalysts and their γ-Fe 3 O 4 immobilized counterparts, and the application of all four pre-catalysts in the transfer hydrogenation of cinnamaldehyde using formic acid as a hydrogen source.

Syntheses and Characterization of the Ligand and Homogeneous Pre-Catalysts
Complexes C1 and C2 were prepared from the reaction of (N-(1-(pyridin-2-yl)ethylidene)-3-(triethoxysilyl)-1-propanamine (L1) with the appropriate metal salts (Scheme 1). Characterization of L1 and C2, which are known compounds [19], can be found in Figures S1-S3; whilst C1, which is new, was characterized as described below. Complex C1 was isolated as an orange solid that is soluble in dichloromethane and methanol. The IR spectrum showed the following peaks which are assigned to the stretching frequencies in parenthesis; When the IR peaks of L1 ( Figure S4) are compared to those of pre-catalysts C1 and C2, there is a shift in the stretching frequency of the imine bond from 1649 cm −1 to (1646, and 1645) cm −1 . The observed decrease in the stretching energy is associated with the pseudo-single bond that the imino bond assumes as the ligand interacts with the metal centre [20], which requires less stretching energy.

Crystal Structure Determination of C1
The crystal structure of C1 is shown in Figure 1. It is mononuclear with two chelating ligands bound to the metal in a bidentate fashion via the nitrogen atoms. The crystal structure is different from those observed for bidentate cobalt complexes that have bidentate nitrogen chelating bipyridyl and imidazole ligands, which show polymeric crystal structures [17]. Table 1a shows the metal complex to have a monoclinic crystal structure. In the solid-state structure shown in Figure 1, the interaction between the cobalt metal centres with the nitrogen donor atoms is evident. The interaction between the metals and the free imine is weaker (longer bond lengths [Table 1b]) compared to that of the aromatic imine (shorter bond lengths [Table 1b]). C1 crystalizes in a centrosymmetric crystal system (monoclinic [Table 1a]), with a primitive lattice (P) allowing a 2-fold/180 • rotation. Table 1b shows shorter bond lengths between the pyridyl nitrogen and the metal centre compared to the imine nitrogen, suggesting stronger interactions of the cobalt with the pyridyl nitrogen, and the bond angles for an octahedral geometry. Table 1b shows the bite angle of (78.86 and 78.80) • between the cobalt atom and the nitrogen ligand, which shows distortion from the ideal bite angle of 90 • for an octahedral geometry.

Characterization of Magnetite and the Supported Pre-Catalysts
The general reaction schemes that produced the two supported pre-catalysts, Fe 3 O 4 @C1 and Fe 3 O 4 @C2, are shown in Scheme 2. Complexes C1 and C2 were immobilized on superparamagnetic iron oxide (Fe 3 O 4 ) nanoparticles according to previously reported procedures [3,21,22] with some modifications. Figure S5 shows the IR, TEM, SEM-EDS, XRD and particle distribution of Fe 3 O 4 -immino-py. From Figure S5, PXRD patterns show that the inverse spinel phase of magnetite is preserved, as its characteristic peaks are observed, but the phases at hkl values 220 and 422 appear broad, which is an indication of non-uniform macro-straining on the magnetite lattice as the ligand is attached. The IR spectra show the appearance of a new peak at 1700 cm −1 , which is attributed to the presence of the imine moiety in the immobilised ligand [23]. The TEM micrographs show the agglomerated spherical crystalline particles with average particle size of 3.4-4 nm,    Figure 2a shows the powder X-ray diffractions of as-synthesised magnetite. The peaks indexed as the X-ray diffractions from the following planes: (220), (311), (400), (422), (511), and (440), correspond to a face centred cubic inverse spinel phase of magnetite [20,21]. The phases at hkl values 220 and 422 appear broad for the system with supported pre-catalysts. The crystallite size measurements of the supported pre-catalysts were determined from the full width at half maximum (FWHM) of the strongest reflection of the hkl diffraction peak, using the Debye-Scherrer formula, = Ө where D is the crystallite mean size and a shape factor k = 0.9 is used, λ is the wavelength of the radiation, β the full width at half maximum (FWHM) in radians in the 2θ scale, and θ = in radians. The average crystal sizes calculated for the pre-catalysts were 3.40 ± 0.40, 3.0 ± 0.5, and 4.0 ± Scheme 2. Synthesis of Fe 3 O 4 @C1 and Fe 3 O 4 @C2 catalysts. Figure 2a shows the powder X-ray diffractions of as-synthesised magnetite. The peaks indexed as the X-ray diffractions from the following planes: (220), (311), (400), (422), (511), and (440), correspond to a face centred cubic inverse spinel phase of magnetite [20,21]. The phases at hkl values 220 and 422 appear broad for the system with supported pre-catalysts. The crystallite size measurements of the supported pre-catalysts were determined from the full width at half maximum (FWHM) of the strongest reflection of the hkl diffraction peak, using the Debye-Scherrer formula, D = kλ βCosθ where D is the crystallite mean size and a shape factor k = 0.9 is used, λ is the wavelength of the radiation, β the full width at half maximum (FWHM) in radians in the 2θ scale, and θ = 2θ 2 in radians. The average crystal sizes calculated for the pre-catalysts were 3.40 ± 0.40, 3.0 ± 0.5, and 4.0 ± 0.3 nm for magnetite, Fe 3 O 4 @C1, and Fe 3 O 4 @C2, respectively. Figure 2b shows the IR spectra of magnetite, Fe 3 O 4 @C1, and Fe 3 O 4 @C2, with the Fe-O-Fe stretches at 702 cm −1 . The peaks at 1359 cm −1, and 1443 cm −1 correspond to the CH 2 stretch and the adsorbed H 2 O stretch is observed at 1060 cm −1 , while the hydroxy moiety (ν OH ) is observed at 3287 cm −1 . The IR of the supported pre-catalysts is staggered in Figure 2b. The stretching frequencies of Fe-O-Si appear at higher stretching frequencies, 769 and 887 cm −1 , compared to 702 cm −1 for the Fe-O functionality. This shift to higher frequencies shows that a higher energy is required to cause a stretch in the Fe-O bond in the supported pre-catalyst, due to the attached heavy atom (Si), which is also evident from the disappearance of a sharp narrow peak at 1060 cm −1 . The imino functionality of the ligand (C=N) is detected at 1599 cm −1 . The appearance of the stretching frequency at 1018 cm −1 corresponds to the presence of the Si-O bond. 0.3 nm for magnetite, Fe3O4@C1, and Fe3O4@C2, respectively. Figure 2b shows the IR spectra of magnetite, Fe3O4@C1, and Fe3O4@C2, with the Fe-O-Fe stretches at 702 cm −1 . The peaks at 1359 cm −1, and 1443 cm −1 correspond to the CH2 stretch and the adsorbed H2O stretch is observed at 1060 cm −1 , while the hydroxy moiety (νOH) is observed at 3287 cm −1 . The IR of the supported pre-catalysts is staggered in Figure 2b. The stretching frequencies of Fe-O-Si appear at higher stretching frequencies, 769 and 887 cm −1 , compared to 702 cm −1 for the Fe-O functionality. This shift to higher frequencies shows that a higher energy is required to cause a stretch in the Fe-O bond in the supported pre-catalyst, due to the attached heavy atom (Si), which is also evident from the disappearance of a sharp narrow peak at 1060 cm −1 . The imino functionality of the ligand (C=N) is detected at 1599 cm −1 . The appearance of the stretching frequency at 1018 cm −1 corresponds to the presence of the Si-O bond. The Ni and Co metal loadings on the pre-catalysts have been determined by Inductively Coupled Plasma Optical Emission Spectroscopy (ICP-OES) to be 1.22 and 1.37 m/m% for the pre-catalyst Fe3O4@C1 and Fe3O4@C2, respectively, which are comparable to literature reports [3,22]. These observations further support the successful coordination of the active metal to the immobilised ligand. The effect of attaching a ligand/pre-catalyst to magnetite causes strain onto the lattice, which can be identified from the shifts or broadening of the peaks. Peak broadening is a characteristic of non-uniform macro-strain on the lattice, while peak shift is a result of uniform micro-strain. From Figure 2a, the peaks broaden with minor shifts as the pre-catalysts are supported onto the support. The resulting total strain was estimated from the Williamson-Hall (W-H) equation (Equation (1)), where the micro-strain (ε) was obtained from the slope of the straight-line fit, where D is the crystallite mean size, and a shape factor k = 0.9 is used, λ is the wavelength of the radiation, β the full width at half maximum (FWHM) in radians in the 2θ scale, and θ = in radians.
The macro-strains estimated from the W-H plot are shown in Table S1 alongside the metal loading determined from ICP-OES. Attaching the ligand to magnetite exerts a lattice strain (ε) of 9.8 × 10 −3 , giving a highly strained lattice. However, coordinating the metal The Ni and Co metal loadings on the pre-catalysts have been determined by Inductively Coupled Plasma Optical Emission Spectroscopy (ICP-OES) to be 1.22 and 1.37 m/m% for the pre-catalyst Fe 3 O 4 @C1 and Fe 3 O 4 @C2, respectively, which are comparable to literature reports [3,22]. These observations further support the successful coordination of the active metal to the immobilised ligand. The effect of attaching a ligand/pre-catalyst to magnetite causes strain onto the lattice, which can be identified from the shifts or broadening of the peaks. Peak broadening is a characteristic of non-uniform macro-strain on the lattice, while peak shift is a result of uniform micro-strain. From Figure 2a, the peaks broaden with minor shifts as the pre-catalysts are supported onto the support. The resulting total strain was estimated from the Williamson-Hall (W-H) equation (Equation (1)), where the micro-strain (ε) was obtained from the slope of the straight-line fit, where D is the crystallite mean size, and a shape factor k = 0.9 is used, λ is the wavelength of the radiation, β the full width at half maximum (FWHM) in radians in the 2θ scale, and θ = 2θ 2 in radians.
The macro-strains estimated from the W-H plot are shown in Table S1 alongside the metal loading determined from ICP-OES. Attaching the ligand to magnetite exerts a lattice strain (ε) of 9.8 × 10 −3 , giving a highly strained lattice. However, coordinating the metal centre to the immobilised ligand leads to a decrease in the lattice strain of magnetite from 6.9 × 10 −3 and 9.8 × 10 −3 to 7.0 × 10 −3 for Fe 3 O 4 @C1 and Fe 3 O 4 @C2, respectively, which indicates that the immobilised pre-catalysts are more stable compared to the ligand only, because of lower lattice stain. In this study, the heterogenized catalysts were subjected to thermal analysis in the temperature range of 40-1000 • C. Figure S6 shows the total % weight loss of 10, 40 and 60% for respectively, between 400-1000 • C, which correspond to the loss of the anchored catalyst. These results are similar to the observations made by Sobhani et al. for a palladium-Schiff base complex immobilized covalently on magnetic nanoparticles [1]. Transmission electron microscopy was used to determine the average particle size, morphology and relative shape of magnetite. Figure 3 shows TEM micrographs of magnetite Fe 3 O 4 (a), compared to Fe 3 O 4 @C1 (b and d) and Fe 3 O 4 @C2 (c and e). From the TEM micrographs, the nanocatalysts are agglomerated into spherical shapes. This tendency is not surprising, given the nanoparticles' small size and magnetic properties [24]. The appearance of dark shades in the images (b-e) implies that the electron beam did not penetrate the sample, which could be a result of the homogeneous phase of the catalyst that is attached to the support occluding the electron beam. In contrast, these dark shades are not apparent in Figure 3a showing the pure magnetite. centre to the immobilised ligand leads to a decrease in the lattice strain of magnetite from 6.9 × 10 −3 and 9.8 × 10 −3 to 7.0 × 10 −3 for Fe3O4@C1 and Fe3O4@C2, respectively, which indicates that the immobilised pre-catalysts are more stable compared to the ligand only, because of lower lattice stain. In this study, the heterogenized catalysts were subjected to thermal analysis in the temperature range of 40-1000 °C. Figure S6 shows the total % weight loss of 10, 40 and 60% for Fe3O4, Fe3O4@C1 and Fe3O4@C2, respectively. Between 0 to 400 °C, Fe3O4 shows a mass loss of 8% which corresponds to loss of the adsorbed water molecules, while for Fe3O4@C2, and Fe3O4@C1, mass losses of 40 and 60% are observed, respectively, between 400-1000 °C, which correspond to the loss of the anchored catalyst. These results are similar to the observations made by Sobhani et al. for a palladium-Schiff base complex immobilized covalently on magnetic nanoparticles [1]. Transmission electron microscopy was used to determine the average particle size, morphology and relative shape of magnetite. Figure 3 shows TEM micrographs of magnetite Fe3O4 (a), compared to Fe3O4@C1 (b and d) and Fe3O4@C2 (c and e). From the TEM micrographs, the nano-catalysts are agglomerated into spherical shapes. This tendency is not surprising, given the nanoparticles' small size and magnetic properties [24]. The appearance of dark shades in the images (b-e) implies that the electron beam did not penetrate the sample, which could be a result of the homogeneous phase of the catalyst that is attached to the support occluding the electron beam. In contrast, these dark shades are not apparent in Figure 3a showing the pure magnetite. The SEM images show inhomogeneous surfaces with non-uniform particle shapes ( Figure S7) for magnetite, Fe3O4@C1, and Fe3O4@C2, which is not surprising due to the magnetic nature of the particle, which is often difficult to overcome even by solvent dispersion. The corresponding EDS spectra of Fe3O4@C1 and Fe3O4@C2 are shown in Figure  4, which reveal the presence of the metals (Ni and Co) in the supported pre-catalysts, showing that the active metal centre was successfully coordinated to the supported ligand [25]. The SEM images show inhomogeneous surfaces with non-uniform particle shapes ( Figure S7) for magnetite, Fe 3 O 4 @C1, and Fe 3 O 4 @C2, which is not surprising due to the magnetic nature of the particle, which is often difficult to overcome even by solvent dispersion. The corresponding EDS spectra of Fe 3 O 4 @C1 and Fe 3 O 4 @C2 are shown in Figure 4, which reveal the presence of the metals (Ni and Co) in the supported pre-catalysts, showing that the active metal centre was successfully coordinated to the supported ligand [25].     Figure 5a shows the overview spectra of the composition of the catalyst Fe 2 O 3 @C2 with atomic percentage, whereas the analysis for the elements Fe, Cl, Si are shown in Figure 5c-e. We can fit the N 1s spectrum, Figure 5b, into a typical peak corresponding to a metal-N species (399.1 eV); these species in Ni-N-C support the dispersion of Ni in the form of Ni-N coordination [1,24].  Figure 5a shows the overview spectra of the composition of the catalyst Fe2O3@C2 with atomic percentage, whereas the analysis for the elements Fe, Cl, Si are shown in Figure 5c-e. We can fit the N 1s spectrum, Figure 5b, into a typical peak corresponding to a metal-N species (399.1 eV); these species in Ni-N-C support the dispersion of Ni in the form of Ni-N coordination [1,24].   [26,27]. The N 1s bond with the Co metal may be the possible active site in the reactions [28][29][30]. In both Figure 5c and Figure 6c, the major peak at 710.8 eV (red curve) confirms the characteristic  be divided into three distinct peaks at 399.2 eV, 401.9 eV and 406.3 eV, corresponding to Co-N, graphite-N, and nitrate-N species, respectively [26][27][28]. The nitrogen atoms are mainly in the form of Co-N (79.76%), nitrate-N (12.47%) and graphite-N (7.76%) [26,27]. The N 1s bond with the Co metal may be the possible active site in the reactions [28][29][30]. In both Figures 5c and 6c, the major peak at 710.8 eV (red curve) confirms the characteristic peak from Fe2p3/2 core level electrons that can be attributed to Fe 3+ octahedral and tetrahedral sites, while Fe 2+ species are found at binding energy 714.1 eV (green curve). Furthermore, the peak at 723.9 eV (blue curve) confirms Fe 2+ species in octahedral sites of the Fe 3 O 4 [31,32].

Catalytic Evaluation
We have investigated the transfer hydrogenation of cinnamaldehyde to different products as shown in Scheme 3. The examples of the 1 NMR and GC spectra used to estimate the conversions are shown in Figures S8-S11.

Catalytic Evaluation
We have investigated the transfer hydrogenation of cinnamaldehyde to different products as shown in Scheme 3. The examples of the 1 NMR and GC spectra used to estimate the conversions are shown in Figures S8-S11. Temperature was established to be an influential factor in the transfer hydrogenation process. For C2, Table 2 entries 1-5 show that a gradual temperature increase from 40 °C to 120 °C (Table 2) resulted in a corresponding gradual increase in the percentage conversion from 0% at 40 °C to 89.9% at 120 °C, while the selectivity towards the hydro-cinnamaldehyde product also gradually increased over the same temperature rise. The same observation is made for C1 (Table 2, entries 6-8), where an increase in the temperature from 80 to 120 °C increased the conversion from 38.5% to 48.8%. C2 showed higher conversions of cinnamaldehyde compared to C1 (Table 2, entries 5 and 8). Both homogeneous pre-catalysts showed high selectivity towards hydro-cinnamaldehyde in the range of 85-92%, while HCOL production is in the range of 7.4-13.1% for both C1 and C2 (Table 2, entries 1-6). These results show that the olefinic moiety (C=C) was selectively reduced compared to the carbonyl moiety (C=O) by the C1 and C2 catalysts.
Magnetite has been reported to have catalytic activity for processes such as the degradation of organic compounds [33], whereas it is reported to be inert towards other catalytic processes [21]. As shown in Table 2, entries 9-13, an increase in the temperature also gave better conversions for both Fe3O4@C1 and Fe3O4@C2. However, the selectivity changed from high yields of HCAL to high yields of COL for the reactions catalysed by both Fe3O4@C1 (89.7%) and Fe3O4@C2 (87.7%). Entry 14, Table 2 shows that no conversion was observed when using pure magnetite as a catalyst. From this study, it is evident that the changes in the selectivity from HCAL to COL as the catalysts are immobilized on magnetite are due to the surface effects of the support. The supported catalysts reduce the substrates through a different mechanism compared to the homogeneous catalysts, which is a possible cause of the varying selectivities observed. Similar selectivity observations have been reported for the hydrogenation of ketones and aldehydes using catalysts supported on magnetite [34]. The selectivity of catalysts for the α,β unsaturated aldehyde is of interest, and cinnamaldehyde with its conjugated phenyl ring has been reported to be reduced to corresponding alcohols over heterogeneous catalysts [35]. Moreover, the use of Fe is also reported to be a known promoter of the hydrogenation of C=O in α,β unsaturated aldehydes, as observed in a study of crotonaldehyde and cinnamaldehyde over supported Pt, Ru, and Rh catalysts, with Fe(II) added as a promoter [35,36]. The homogeneous catalysts convert cinnamaldehyde to hydro-cinnamaldehyde, followed by further conver-Scheme 3. General scheme for the transfer hydrogenation of cinnamaldehyde to hydro cinnamaldehyde and cinnamyl alcohol using the synthesised catalyst.

Effect of Temperature on Catalyst Activity and Selectivity of C1, C2, Fe 3 O 4 @C1 and Fe 3 O 4 @C2
Temperature was established to be an influential factor in the transfer hydrogenation process. For C2, Table 2 entries 1-5 show that a gradual temperature increase from 40 • C to 120 • C ( Table 2) resulted in a corresponding gradual increase in the percentage conversion from 0% at 40 • C to 89.9% at 120 • C, while the selectivity towards the hydrocinnamaldehyde product also gradually increased over the same temperature rise. The same observation is made for C1 (Table 2, entries 6-8), where an increase in the temperature from 80 to 120 • C increased the conversion from 38.5% to 48.8%. C2 showed higher conversions of cinnamaldehyde compared to C1 (Table 2, entries 5 and 8). Both homogeneous pre-catalysts showed high selectivity towards hydro-cinnamaldehyde in the range of 85-92%, while HCOL production is in the range of 7.4-13.1% for both C1 and C2 (Table 2, entries 1-6). These results show that the olefinic moiety (C=C) was selectively reduced compared to the carbonyl moiety (C=O) by the C1 and C2 catalysts.
Magnetite has been reported to have catalytic activity for processes such as the degradation of organic compounds [33], whereas it is reported to be inert towards other catalytic processes [21]. As shown in Table 2, entries 9-13, an increase in the temperature also gave better conversions for both Fe 3 O 4 @C1 and Fe 3 O 4 @C2. However, the selectivity changed from high yields of HCAL to high yields of COL for the reactions catalysed by both Fe 3 O 4 @C1 (89.7%) and Fe 3 O 4 @C2 (87.7%). Entry 14, Table 2 shows that no conversion was observed when using pure magnetite as a catalyst. From this study, it is evident that the changes in the selectivity from HCAL to COL as the catalysts are immobilized on magnetite are due to the surface effects of the support. The supported catalysts reduce the substrates through a different mechanism compared to the homogeneous catalysts, which is a possible cause of the varying selectivities observed. Similar selectivity observations have been reported for the hydrogenation of ketones and aldehydes using catalysts supported on magnetite [34]. The selectivity of catalysts for the α,β unsaturated aldehyde is of interest, and cinnamaldehyde with its conjugated phenyl ring has been reported to be reduced to corresponding alcohols over heterogeneous catalysts [35]. Moreover, the use of Fe is also reported to be a known promoter of the hydrogenation of C=O in α,β unsaturated aldehydes, as observed in a study of crotonaldehyde and cinnamaldehyde over supported Pt, Ru, and Rh catalysts, with Fe(II) added as a promoter [35,36]. The homogeneous catalysts convert cinnamaldehyde to hydro-cinnamaldehyde, followed by further conversion to hydrocinnamyl alcohol. With the supported homogeneous catalysts, cinnamaldehyde is converted to both cinnamyl alcohol and hydro-cinnamaldehyde but further conversion of these two products to a fully saturated system (hydrocinnamyl alcohol) is not observed for the heterogeneous catalysts.

Catalyst Reusability Studies Recyclability of Pre-Catalysts C1, C2, Fe 3 O 4 @C1 and Fe 3 O 4 @C2
It is important to establish the number of cycles over which a catalyst can convert a substrate to products before deactivation. In this study, the homogeneous catalysts were recycled as per methods reported in the literature [37]. In the experiment, the reaction was simultaneously repeated with catalyst recovery from the reaction mixture. After the first catalytic cycle, the products were extracted with hexane and diethyl ether. This allowed the pre-catalysts to precipitate, before being dried under reduced pressure and weighed. Dichloromethane was used to wash the catalyst back into the autoclave reactor. The reactor was then charged with the pre-catalyst, substrate, base, and formic acid. For Fe 3 O 4 @C1 and Fe 3 O 4 @C2, after the first cycle the catalyst was separated from the products using a magnet (Figure 7b,c) and washed with dichloromethane and oven dried. The reactor was then charged with the substrate, base, and formic acid. Recyclability studies of homogeneous catalysts are rare in the literature, especially for C1 and C2. From Figure 7, the homogeneous catalysts are recyclable up to 3 cycles, giving conversions ranging between 50-38% and 80-70% from cycle 1 to cycle 3 for catalysts C1 and C2, respectively. The loss of activity in the third cycle could be due to catalyst poisoning/fouling by the organic waste or catalyst loss due to workup. The supported catalysts could be used up to 8 cycles, (Figure 7a) giving conversions of 65% and~99% for Fe 3 O 4 @C1 and Fe 3 O 4 @C2, respectively, maintained over 8 cycles. Loss of activity starting in cycle 9 is observed for both Fe 3 O 4 @C1 and Fe 3 O 4 @C2, which is attributed to the same causes as the homogeneous catalysts.

Characterization of the Used Fe3O4@C1 and Fe3O4@C2
To investigate the stability of the used catalysts, we characterized the TEM, IR, XRD and EDS, and the results were compared to those of the fresh TEM images in Figure S12a,b show no changes in the morphology and size of whereas the functional groups and elements of the supported ligand are sti the IR ( Figure S12c) and EDS ( Figure S13) spectra. From Figure S14, the inv magnetite is still preserved after 9 catalytic cycles. The XPS survey of Fe3O S15) and Fe3O4@C1 ( Figure S17) and the high-resolution analysis of N, C, S in Fe3O4@C2 ( Figure S16) and Fe3O4@C1 ( Figure S18) show no significant c catalysts after use.

Characterization of the Used Fe 3 O 4 @C1 and Fe 3 O 4 @C2
To investigate the stability of the used catalysts, we characterized the materials by TEM, IR, XRD and EDS, and the results were compared to those of the fresh catalysts. The TEM images in Figure S12a,b show no changes in the morphology and size of the particles, whereas the functional groups and elements of the supported ligand are still observed in the IR ( Figure S12c) and EDS ( Figure S13) spectra. From Figure S14, the inverse spinel of magnetite is still preserved after 9 catalytic cycles. The XPS survey of Fe 3 O 4 @C2 ( Figure S15) and Fe 3 O 4 @C1 ( Figure S17) and the high-resolution analysis of N, C, Si, Cl/Br,  Figure S16) and Fe 3 O 4 @C1 ( Figure S18) show no significant changes in the catalysts after use.

Metal Leaching and Homogeneity Tests Homogeneity Studies for Pre-Catalysts C1 and C2
Mercury interacts with nanoparticles to form amalgam (Hg y M x ), which completely blocks the heterogeneous active sites, leading to inhibited catalytic activity due to heterogeneous species that might have formed in the reaction mixture as a result of catalyst decomposition [38]. Formation of amalgam leads to over 50% decrease in the conversions for heterogeneously catalysed reactions. From Figure S19, it is evident that there was a small decrease in the conversions from 48.7% to 40.7% for pre-catalyst C1 and 89.5% to 83.6% for pre-catalyst C2. These decreases are, however, not enough to account for the possibility of Ni 2+ and Co 2+ decomposition, and the mercury poisoning test has been reported to often lead to inaccurate conclusions with M(II) pre-catalysts, especially in the case of dynamic catalytic systems [38,39].

Leaching Test for Pre-Catalyst Fe 3 O 4 @C1 and Fe 3 O 4 @C2
The leaching of Co and Ni from the Fe 3 O 4 @C1 and Fe 3 O 4 @C2 catalysts was determined using methods reported in the literature [40]. After a 24 h catalytic reaction time, the catalyst was removed from the reaction mixture using a magnet. The reaction mixture was placed in a crucible and heated to 500 • C under a ramping regime of 10 • C/min, before being calcined at 600 • C for 3 h. The residue was weighed and digested in aqua regia and analyzed for Ni and Co using ICP-OES. The results showed that 0.4 and 0.5 mg/kg of Co and Ni, respectively, were detected in the residue, i.e., less than 1% of the initial catalyst loadings, which indicates that only negligible amounts of Ni and Co were leached from the surface of magnetite to the solution. As such, we may infer that the catalysts are stable and tolerate the reaction conditions for the transfer hydrogenation of cinnamaldehyde.

In Silico Studies of the Selectivity of the Catalysts
In supported catalysts, the active metal is dispersed on the surface of the support, which in turn can alter the catalytic activity and selectivity because of the active metalsupport interactions. To gain detailed insight into the selectivity of the homogenous and heterogeneous catalysts towards the C=C and C=O bonds in cinnamaldehyde, we have carried out calculations based on the density functional theory (DFT) to predict the lowest energy adsorption geometries and the adsorption energetics ( Figure 8). The active species formed through oxidative addition of the hydrogen molecule to the metal centre in the pre-catalysts were used to investigate favourable interactions between the Ni metal and the olefinic or carbonyl moieties present in cinnamaldehyde.
The DFT calculations reveal that C=C bond adsorption to the homogenous catalyst is more stable (E ads = −0.79 eV) than that of the C=O bond (−0.58 eV), indicating a higher selectivity to HCAL. In contrast, at the heterogeneous catalyst, the adsorption of CAL via a C=O bond at both the Ni site (−1.29 eV) and on the magnetite support (−1.57 eV) is energetically more favourable than via the C=C bond at the Ni site (−1.11 eV) and on the support (−1.33 eV). These results indicate that the heterogeneous catalysts favour the C=O centred adsorption and hydrogenation, which results in its selectivity towards the formation of COL rather than towards HCOL. These results are consistent with the experimental results, which show that the homogenous catalysts have higher HCAL selectivity, while the heterogeneous catalysts produce higher COL selectivity. The DFT calculations reveal that C=C bond adsorption to the homogenous catalyst is more stable (Eads = −0.79 eV) than that of the C=O bond (−0.58 eV), indicating a higher selectivity to HCAL. In contrast, at the heterogeneous catalyst, the adsorption of CAL via a C=O bond at both the Ni site (−1.29 eV) and on the magnetite support (−1.57 eV) is energetically more favourable than via the C=C bond at the Ni site (−1.11 eV) and on the support (−1.33 eV). These results indicate that the heterogeneous catalysts favour the C=O centred adsorption and hydrogenation, which results in its selectivity towards the formation of COL rather than towards HCOL. These results are consistent with the experimental results, which show that the homogenous catalysts have higher HCAL selectivity, while the heterogeneous catalysts produce higher COL selectivity.

Characterization Techniques
Nuclear magnetic resonance (NMR) spectra were recorded on a Bruker Ultrashield-400 MHz spectrometer ( 1 H: 400 MHz, 13 C{ 1 H}: 100 MHz) in chloroform using tetramethylsilane (TMS) as a reference. All the chemical shifts were reported in ppm (δ) using TMS as a reference. The functional groups were confirmed using a Thermo Nicolet IR instrument fitted with an ATR probe. Mass spectrometry was carried out on a Water Synapt G2 electrospray ionization mass spectrometer in the negative or positive-ion mode. Elemental analyses were done using a Thermo Scientific Flash 2000 Series CHNO elemental analyzer.
Powder X-ray diffraction (PXRD) data were collected using an XPERT-PRO diffractometer (Cu K α radiation) with a current flow of 40 mA and voltage of 40 kV. Single crystal X-ray data were collected using a Bruker KAPPA APEX II DUO diffractometer with graphite monochromator Mo-K α radiation (l 1 4 0.71073 A). The data collection was carried out at low temperatures (173 K) using a Cryostream cooler. Unit cell refinement and data reduction were performed using the program OLEX. Structure solutions and refinement were achieved by the SHELXS program.
For TEM analysis, the supported catalysts were dispersed in ethanol followed by ultrasonication for 15 min. The samples were placed on a carbon-coated copper grid, dried at room temperature. The transmission electron microscope images were collected using a JEOL Model JEM 2100F electron transmission electron microscopy (TEM) system operating at a voltage of 200 kV. For the scanning electron microscopy (SEM), the heterogeneous catalysts were coated with carbon, and images were collected using the Tescan Vega 3LMH scanning electron microscope coupled with energy-dispersive X-ray spectroscopy (EDS) system. The Co and Ni metal loading on Fe 3 O 4 @C2 and Fe 3 O 4 @C1 were determined using Spectro Arcos ICP-OES.
The XPS analyses were performed with an ESCAlab 250Xi instrument. The X-ray source was chosen as the monochromatic Al K line (1486.7 eV). XPS can detect all elements except hydrogen and helium, it probes the sample surface to a depth of 2-10 nm, and has detection limits of around 0.1 at%. The pass energy was 20 eV, and the energy increment was 100 meV. Narrow scan photoelectron spectra were recorded (between four and eight scans). The spectra were charge-corrected to the main line of the carbon 1s spectrum (adventitious carbon) set at 284.8 eV. Quantifying the detected elements and deconvolution of thespectra was performed with the CasaXPS software (version 2.3.25).

Synthesis of the Supported Catalysts Fe 3 O 4 @C1 and Fe 3 O 4 @C2
The immobilized catalysts were synthesized by a modification of a method reported in the literature. 0.3 g Fe 3 O 4 in 30 mL of toluene was added a solution of 0.3 g of L1 in 5 mL of dichloromethane. The mixture was then reacted together under ultra-sonication for 0.5 h. The metal precursor (2 mmol) was further added to the reaction mixture and allowed to react for 24 h. The reaction mixture was centrifuged, and the solvent discarded. The solid product was washed with dichloromethane and dried in air.

Catalytic Selectivity and Activity Tests Transfer Hydrogenations Studies
A Teflon reactor (50 mL) was used in this study. A mixture of the catalysts, cinnamaldehyde, formic acid, and a base was heated to the desired temperature after purging four times with nitrogen gas at a stirring speed of 960 rpm for a desired reaction time. At the end of the reaction, the reactor vessel was cooled, followed by the release of the excess gas. A sample of the mixture was then analysed by 1 H NMR spectroscopy and/or gas chromatography to determine the conversion and product selectivity. Examples of the typical spectrum are shown in Figures S7 and S8 ( 1 H NMR) and the GC shown in Figures S9 and S10.The conversion of cinnamaldehyde and selectivity of the products were calculated using the following equations:

Computational Details
The spin-polarized density functional theory (DFT) calculations were carried out using the Vienna Ab Initio Simulation Package (VASP) [41][42][43][44] wherein the interactions between the core and valence electrons were treated using the Project Augmented Wave (PAW) method [41]. The exchange-correlation potential was calculated using the Perdew-Burke-Ernzerhof (PBE) generalized gradient approximation (GGA) functional [42] with a Hubbard correction (PBE+U), which accounts for the Coulomb interaction of localized d-electrons [43,44]. In this study, the value for the on-site Coulomb interaction term for Fe was set to U eff = 3.7 eV, which has been demonstrated to provide sufficiently accurate lattice parameters, electronic, and magnetic properties of Fe 3 O 4 [45]. Long-range dispersion interactions were accounted for using the Grimme DFT-D3 scheme [46]. The Kohn-Sham wave functions were expanded in a plane-wave basis set with a kinetic energy cut-off of 500 eV. Structural optimizations were conducted using the conjugate-gradient algorithm until the residual Hellmann-Feynman forces on all relaxed atoms reached 0.01 eV/Å. The bulk Fe 3 O 4 material was modelled in the full conventional cubic unit cell of 56 atoms, where a 5 × 5 × 5 Monkhorst-Pack [47] k-point mesh was used to sample the Brillouin zone. The most stable (001) surface was employed for the construction of the supported pre-catalysts and for the adsorption characterization of CAL. A vacuum region of 20 Å was added to the c-axis to avoid interactions between periodic slabs. Different coordination modes of CAL (C=C and C=O bond adsorption) were explored to find the most stable adsorption configurations [48,49]. No symmetry constraints were imposed in any of the calculations on the structural optimization of the CAL-catalyst systems, and in particular, the CAL was free to move away laterally and vertically from the initial binding site(s) or reorient itself to find the lowest-energy adsorption configuration. The strength of adsorption for CAL was determined by calculating the adsorption energy (E ads ) as follows: where E catalyst+CAL , E catalyst , and E CAL are the relaxed total energies of the catalyst-CAL systems, the isolated catalyst, and the CAL adsorbate molecule, respectively. The adsorption is deemed exothermic and favourable if the calculated adsorption energy is negative.

Conclusions
We have reported the synthesis and characterisation of the homogeneous cobalt(II) and nickel(II) pre-catalysts (C1 and C2) of the E-1pyridyl-N-3-triethoxysilylpropyl methanimine ligand and their magnetite-immobilised counterparts Fe 3 O 4 @C1 and Fe 3 O 4 @C2, as efficient catalysts in the transfer hydrogenation of cinnamaldehyde. Catalyst Fe 3 O 4 @C1 and Fe 3 O 4 @C2 are efficient, recyclable, and easily recoverable from the reaction mixture, yielding over 80% of cinnamyl alcohol with a metal loading of 1.37%m/m and 1.22%m/m, respectively, while the homogeneous catalysts yielded over 89% of hydro-cinnamaldehyde. Supporting the homogeneous catalysts on magnetite was found to alter the selectivity from the reduction of C=C to the reduction of C=O, which change in selectivity was established to be associated with the interaction of the favoured C=O moiety at the support surface, as compared to the C=C. The catalysts Fe 3 O 4 @C1 and Fe 3 O 4 @C2 show negligible metal leaching at less than 1% after 9 cycles, which creates less pollution and more stable catalysts. Thus, anchoring the homogeneous catalysts to a support is an effective way to improve catalyst recyclability, but as observed in this work, product selectivity can be influenced by the magnetite support, even though the support itself is catalytically inactive in the transfer hydrogenation process.
Supplementary Materials: The following supporting information can be downloaded at: https:// www.mdpi.com/article/10.3390/molecules28020659/s1, FigureS1: 1 H NMR spectra of (E)-1-(pyridin-2-yl)-N-(3-(triethoxysilyl)propyl)methanimine, Figure S2: The 13 C NMR spectra of 2:(E)-1-(pyridin-2-yl)-N-(3-(triethoxysilyl)propyl)methanimine, Figure S3: Time of Flight Electrospray Ionisation spectrum of C2 in negative mode, Figure S4: The IR spectra of the ligand and the corresponding homogeneous catalysts, Figure S5: P-XRD, FTIR, SEM, EDS, particle size distribution and TEM characterization of Fe 3 O 4 -immino-py, Figure S6: Thermal gravimetric analysis of the supported pre-catalysts, Figure S7: The SEM images of the fresh heterogeneous catalysts, Figure S8: Example of the 1 H NMR spectrum of the isolated products of CAL hydrogenation using homogeneous catalyst C2 after 16 h of reaction time, Figure S9: Example of the 1 H NMR spectrum of the crude mixture after CAL hydrogenation using Fe 3 O 4 @C2 after catalyst 8 h of reaction time, Figure S10: Example of the GC spectrum of CAL hydrogenation using homogeneous catalyst C2, Figure S11: Example of the GC spectrum of CAL hydrogenation using homogeneous Fe 3 O 4 @C2 catalyst, Figure S12: The TEM images of catalyst Fe 3 O 4 @C2 (a) and Fe 3 O 4 @C1 (b) and the IR analysis(c) of after the 9th cycle, Figure S13: The EDS spectra of the spent catalysts, Figure S14: The XRD of the spent catalysts, Figure S15: The XPS survey of spent Fe 3 O 4 @C2, Figure S16: The high-resolution analysis of the elements detected in Fe 3 O 4 @C2, Figure S17: The XPS survey of spent Fe 3 O 4 @C1, Figure S18: The high-resolution analysis of the elements detected in Fe 3 O 4 @C1, Figure S19: Homogeneity tests for the transfer hydrogenation of CAL using catalysts C1 and C2 in the presence of liquid mercury. Reaction conditions: CAL (20 mmol), catalyst (0.02 mmol) formic acid (40 mmol), base (20 mmol), 120 • C, 2 mg Hg (0), 24 h. Conversions are estimated by gas chromatography. Table S1: Calculated strain on the lattice of magnetite for the supported pre-catalysts, ligand, and the support. Data Availability Statement: The data supporting this investigation are available from the corresponding authors upon request.