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Article

High Performance and Sustainable Copper-Modified Hydroxyapatite Catalysts for Catalytic Transfer Hydrogenation of Furfural

by
Balla Putrakumar
1,*,
Prem Kumar Seelam
2,*,
Ginjupalli Srinivasarao
3,
Karthikeyan Rajan
1,
Rajendiran Rajesh
4,
K. Ramachandra Rao
5 and
Tongxiang Liang
1,*
1
College of Rare Earths (CoRE), Jiangxi University of Science and Technology, Ganzhou 341000, China
2
Environmental and Chemical Engineering Research Unit, Faculty of Technology, University of Oulu, P.O. Box 4300, 90014 Oulu, Finland
3
Department of Basic Science and Humanities, Swarnandhra College of Engineering and Technology, Narasapur 534280, India
4
Department of Chemistry, Pondicherry University, Puducherry 605014, India
5
Crystal Growth & Nano Research Centre, Department of Physics, Government College (Autonomous), Rajahmundry, Andhra Pradesh 533105, India
*
Authors to whom correspondence should be addressed.
Catalysts 2020, 10(9), 1045; https://doi.org/10.3390/catal10091045
Submission received: 30 July 2020 / Revised: 19 August 2020 / Accepted: 24 August 2020 / Published: 11 September 2020
(This article belongs to the Special Issue Perspectives in Catalytic Fast Pyrolysis, Catalytic Hydrodeoxygenation, and Catalytic Fast Hydropyrolysis)
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Abstract

:
Designing and developing non-noble metal-based heterogeneous catalysts have a substantial importance in biomass conversion. Meerwein-Ponndorf-Verley (MPV) reaction is a significant pathway for eco-friendly catalytic transfer hydrogenation (CTH) of biomass derived furfural into furfuryl alcohol. In this work, a series of copper-supported hydroxyapatite (HAp) catalysts with different copper loadings (2–20 wt.%) were prepared by a facile impregnation method and tested in the reduction of furfural to furfuryl alcohol using 2-propanol as a hydrogen donor. The structural and chemical properties of the synthesised catalysts were analysed by using various techniques (XRD, N2 sorption, SEM, TEM, UV-DRS, ICP, FTIR, TPR, TPD-CO2 and N2O titration). The effect of copper loading was found to be significant on the total performance of the catalysts. The results demonstrate that 5CuHAp catalyst possess highly dispersed copper particles and high basicity compared to all other catalysts. Overall, 5CuHAp exhibited highest conversion (96%) and selectivity (100%) at 140 °C at 4 h time on stream. The optimised reaction conditions were also determined to gain the high activity.

Graphical Abstract

1. Introduction

Energy and chemical intermediates are primarily derived from conventional sources such as natural gas, oil and coal. This causes, exacerbation of environmental problems and depletion of resources [1]. There is an urgent need to analyse the renewability, economy and inexhaustible substitutes that can produce equal or higher energy yields to replace and avoiding usage of fossil fuels. Biomass-derived products often expose superior qualities related to the environment than their fossil fuel-based counterparts [2,3].
Furfural (FA) is widely used platform molecule which is derived from lignocellulosic biomass via acid hydrolysis [4]. FA is a versatile starting material for many intermediate chemicals, monomers and fuels [5]. Catalytic transformation of biomass-based furfural is one of the efficient valorisation processes that can offer in producing useful fuels, polymers and fuel additives such as ethyl levulinate, 2-methyl tetrahydrofuran, δ-valerolactone, 2-methyl furan and ethyl furfuryl ether [6,7]. Direct transformation of furfural into furfuryl alcohol, furans and methyl furan via metal-catalysed hydrogenation, decarbonylation and reduction process is a key and important commercial application in producing wider range of derivatives [8].
Furfuryl alcohol (FAOL) has been used in rocket fuels which combust immediately and energetically when contacted with oxidisers [9]. FAOL is used in improving the moisture-dimensional stability, hardness, decay and insect resistance for the wood and furniture materials [10]. In polymer industry, it is most used in the fabrication of thermostat polymers, production of various synthetic fibres, rubbers-resins and liquid resins in ceramic industry. It is also used as a starting material for various industrial products such as lubricants, lysine, plasticisers, dispersing agents, vitamin C and agro-chemicals [11,12].
Catalytic transformation of FA to FAOL can be achieved either via gas or liquid phase reactions, later one is advantageous than the former in terms of energy consumption and product selectivity [13]. In literature, two main synthesis approaches were reported for liquid phase hydrogenation of FA to FAOL. The first approach describes that dihydrogen gas (H2) as a H-donor, exhibits superior hydrogenation efficiency over the transition metal catalysts, preferably over noble metals (Au, Pd, Pt, Ru, Rh and Re) [14,15,16,17,18]. However, in the first approach, the use of pure hydrogen gas has several drawbacks including the need of costly infrastructure and the difficulty of transportation, safety and efficient storage. Second approach is simpler in terms of required laboratory equipment. The alcohols or formic acid was used as H-donors instead of pure H2 and also acts as a solvent media in liquid phase reaction [19,20].
CTH of FA has been widely investigated over various materials such as metal-based catalysts supported on oxides, carbon, zeolites and other promising support materials [21,22,23,24,25,26,27]. Most commonly used basic oxides in particular MgO, CaO and mixed oxides have been developed for MPV reaction, which are inexpensive, commercially available and environmentally benign [28]. In one study, Solera et al. demonstrated that basicity is a key factor that plays an important role in MPV reaction than acidity [29]. Many promising support materials were optimised and studied in furfural hydrogenation in combination with Cu. A bifunctional activity was presented by the Cu-supported mixed oxides such as zeolites, MgO-Al2O3, CaO and CeO2-ZrO2. Wang et al. reported the effect of support in specific acidity type such as Cu/ZSM-5 and Cu/Al2O3 resulted in the formation of oligomers and over Cu/MgO basic catalyst which had a better mass balance and reaction performance towards FAOL [30]. Recently, Fan et al. suggested that the basic mixed oxide γ-Fe2O3@HAP catalyst had dual functionality, first hydrogen transfer from 2-propanol, and then H2 to FA [31]. Wenjie Shen et al. reported that Cu/La2O3 catalyst exhibited high activity in the transfer dehydrogenation of primary alcohols and also stated that the effective conversion is mainly due to the high basicity of the catalyst [32]. Further, the proton abstraction was favoured by La2O3 under anaerobic conditions and the Cu particles are needed for hydrogen transfer to intermediate species.
Both noble (Pt, Ru, Pd) and non-noble (Ni, Co, Cu) based metal catalysts show good performance in catalytic FA hydrogenation [33,34]. Because of their cost and availability, non-noble transition metal catalysts are feasible for the future industrial applications. Among all the catalysts reported in the literature, Cu-based catalysts presented as the promising choice for selective hydrogenation of furfural due to moderately high activity compared to noble metal catalysts and cost effective [21,35,36]. It is known that the Cu-Cr catalyst was used in the industrial production of FA as it has best features [37]. According to environmental point of view Cr is toxic in nature, hence, non-chromium-based Cu catalysts were developed for both gas and liquid-phase hydrogenation. There are several challenges that still exist in developing sustainable and eco-friendly catalysts for the catalytic hydrogenation of FA. Henceforth, a sustainable and efficient catalyst support is needed in combination with robust Cu for selective catalytic hydrogenation of FA. In this context, we introduced hydroxyapatite support for Cu catalyst with simple preparation methods and precise Cu loading. The calcium-hydroxyapatite (Ca10(PO4)6(OH)2), which is commonly known as hydroxyapatite (HAp), is a naturally occurring inorganic material known for being a basic support catalyst with cationic exchange properties for various applications [38]. Recently, HAp has attracted considerable attention as a catalyst-support material for transition metal-catalysed reactions [39,40].
In the present work, CuHAp catalysts were synthesised by a facile preparation method and tested in catalytic transfer hydrogenation of furfural to furfuryl alcohol using 2-propanol as hydrogen donor and solvent. The physico-chemical and morphological properties of the synthesised catalysts were obtained by various techniques including XRD, N2 sorption, SEM, TEM, UV-DRS, ICP, FTIR, TPR, TPD-CO2 and N2O titration. It was found that basicity and active Cu surface area had a great impact on the catalytic performances. The influences of reaction parameters including catalyst loading, temperature, time and N2 initial pressure were systematically investigated in detail. Finally, the recyclability of the best-performed catalyst was also studied.

2. Results and Discussion

2.1. Characterisation

Figure 1 shows the X-ray diffraction patterns of pure HAp and Cu-modified HAp catalysts. Well defined diffraction characteristics were observed for pure HAp support and matched with reference patterns of JCPDS Ref. 09-0432 [41]. After Cu loading on HAp support, the XRD patterns were compared with the pure HAp support. However, the absence of Cu peaks for the samples with 2 and 5 wt.% loading was evident because of the fact that small crystallites and a highly dispersed CuO phase was formed over the HAp support. Above 5 wt.% copper loading, the reflections at the 2θ values of 35.57° and 38.67° are broader due to the appearance of copper oxide phase and the corresponding planes are (11-1) and (111), respectively [42]. With further increase in copper loading up to 20 wt.%, the peak intensity of CuO was found to increase to a greater extent. This designates that the increase in copper loading leads to the growth of CuO crystallites. Absence of any other Cu phase was evident in different Cu loading on HAp support which can be seen in the XRD pattern.
The FTIR spectra of pure HAp and the Cu-supported catalysts were analysed in the range of wavelength 400–4000 cm−1, as shown in Figure 2. The strong characteristic functional groups on HAp are phosphate and hydroxyl groups. In theory, four kinds of vibrational modes are present for phosphate ions such as ν1, ν2, ν3 and ν4 [41]. All these modes were observed for all catalysts that are intrinsically infrared active in nature. Two intensive peaks at 500–700 cm−1 and 900–1200 cm−1 ranges were observed. The absorption band (ν1) at ~962 cm−1 is related to P-O symmetric stretching. Similarly, the band (ν2) with weak intensity at ~472 cm−1 is a characteristic peak of O-P-O bending vibrations. The IR band (ν3) observed at ~1040 cm−1 was due to the asymmetric stretching vibrations of P-O phosphate group. The intense band (ν4) was observed in the region of 500–700 cm−1 is due to P-O symmetric and asymmetric bending modes of P=O bond. The low site symmetry bonding of the molecule causes splitting of vibration band (ν4). The OH stretching vibration of water molecules was evident and the corresponding broad peak was appeared at 3440 cm−1 wavelengths. The sharp and low intense band at 3570 cm−1 related to the O-H vibration modes hosted by the hydroxyapatite lattice.
The textural properties of CuHAp catalysts were investigated by nitrogen physisorption measurements and results are reported in Table 1. In case of pure HAp sample, the measured specific surface area found to be 76 m2·g−1 which is the highest BET value compared to rest of the catalysts. From Table 1, it is clearly shown that after Cu incorporation, the surface areas of all Cu-modified are lower than the pure HAp support. The surface area is decreased with Cu loading mainly due to the existence of Cu in bulk and covered on the surface of the HAp matrix.
The N2O titration experiments were performed to find out the average particle size and active Cu surface area of CuHAp catalysts and the results are tabulated in Table 1. Increase in copper surface area was evident with Cu loading from 2 to 5 wt.% and the average particle size was found to be smaller up to 5 wt.% Cu loading. Hence, at low Cu loadings i.e., up to 5 wt.% a uniform dispersion of copper sites over HAp surface was formed. In case of higher Cu loading (above 5 wt.%) metal surface area is found to decrease, while the average particle size is increased due to Cu aggregation. These findings conclude that copper oxide is highly dispersed at lower loadings on HAp support i.e., for the 2 and 5 wt.% Cu catalysts. These results are well matched with XRD patterns.
The UV-visible spectroscopic analysis was carried out for various CuHAp catalysts and the results are shown in Figure 3. The characteristic charge transfer bands depict an idea of environment in the proximity of Cu2+ ions [43]. The spectra exhibited a maximum peak at 255 nm, which is related to charge transfer transition between ligand to metal, i.e., Cu2+ ion and oxygen in a mononuclear species located at the surface. The blue shift was observed from 255 nm to 330 nm with copper loadings (2–20 wt.%) over the HAp surface and this resulted in the aggregation of isolated copper particles and crystal growth of the linear sized copper oxide species. Thus, the axial Cu2+–O2- bonds grow weaker while the in-plane Cu2+–O2- bonds form stronger [44]. In addition to the charge transfer, a shoulder peak at 370 nm was found for 2 and 5 wt.% copper loadings, which indicates that the formation of a highly dispersed and homogeneous Cu clusters was observed. According to the literature, at higher copper loadings a band at 350–450 nm was exhibited in the UV-DRS spectra, which was attribute to three-dimensional Cu+ clusters in the CuO matrix [45]. At 650–750 nm, a low intense peak corresponds to the d-d transitions of Cu2+ ions, which was situated in the octahedral geometry surrounded by OH symmetry.
The TPR experiments were carried out to evaluate the reducibility of copper species in CuHAp catalysts and the profiles are shown in Figure 4. A significant change in the reduction peaks were noticed with different copper loadings along with bulk and surface copper oxides reduction occurred at different temperatures. At relatively low Cu content i.e., below 10 wt.%, low temperature region was found to have two overlapping reduction peaks [46]. Highly dispersed CuO particles were presented in the 2CuHAp and 5CuHAp samples, which are reduced easily at low temperature region [47]. Furthermore, at higher copper loadings, i.e., ≥10 wt.%, more than three peaks were observed related to higher temperature reduction of bulk copper species (above 300 °C). In the case of 10CuHAp catalyst, the reduction profile resulted in four peaks, in which three peaks are between 180 to 400 °C and a small peak found at 450–600 °C. With the increase in Cu loading from 10 wt.% to 20 wt.%, a peak was observed towards higher temperature region at 270 °C. Moreover, combination of small peak at 300–320 °C was also appeared. The peak broadening and the shifting of the Tmax towards the high temperature region was observed for the higher Cu loadings, which could be due to the increased crystallinity of CuO. Herein, the shoulder peak represents the two-step reduction process of bulk CuO species. From literature, the reduction process of bulk CuO to metallic Cu take place via Cu2+ to Cu1+ and Cu1+ to Cu0. The peak position between 350 and 400 °C was corresponding to the reduction of Cu2+ ions (CuO) in Cu2(OH)(PO4) matrix, which is a new solid phase-libethenite [41]. The fourth peak could be the result of surface carbonates reduction between 450 and 600 °C.
The basicity type and strength of various Cu-supported HAp samples were measured by CO2—TPD and the CO2 desorbed profiles are displayed in Figure 5. In general, the basicity of metal oxide is of three types (weak, medium and strong) [44]. In Figure 5, the TPD profiles had three desorption peaks for all the studied catalysts in the region of 50–200 °C, 200–500 °C and 500–650 °C, which are assigned as weak, medium and strong basic sites, respectively. The surface -OH groups are associated with the weak basic sites, the medium basic sites are related to metal-oxygen pairs and the low-coordination oxygen anions are ascribed to the strong basic sites [48]. 2CuHAp and 5CuHAp samples show similar trend but the intensities differ; later one exhibited more intense peaks than the former one. With the increase in Cu loading from 5 wt.% to 20 wt.%, the intensities of the three peaks are gradually decreased due to the surface coverage of bulk CuO phase. Interestingly, the appearance of new peak for 10CuHAp, 15CuHAp and 20CuHAp samples in the region of 500–650 °C might be due to desorption of CO2 from CuCO3 [49]. Moreover, the Tmax of new peak is shifted to lower temperature region. Finally, TPD-CO2 results revealed that the 5CuHAp sample possess maximum number of surface basic sites compared to all investigated samples.
The morphology of the pure HAp- and Cu-modified HAp catalytic materials were analysed using scanning electron microscopy (SEM-EDS) and transmission electron microscopy (TEM). SEM image and corresponding EDX-mapping of 5CuHAp (Figure 6) show the distribution of Ca, Cu, O and P atoms are presented in the Cu-modified HAp support. The EDX analysis attached to electron microscope revealed that the Cu content of 5CuHAP sample is 4.2 wt.%, which was almost similar to the value determined by ICP and Ca/P ratio was found to be 1.54. The TEM image of HAp (Figure 7) indicated that the mixed oxide phase and hybrid structure with nanorods were seen and have lateral sizes ranging from 50 nm to 200 nm.

2.2. Catalytic Activity

The liquid phase conversion of FA to FAOL was carried out by using 2-propanol as the H-donor for the prepared catalysts. The solubility of 2-propanol with FA was found to be better for the liquid phase catalytic transformation of FA. He et al. reported that highest FA conversion and FAOL selectivity was achieved by using 2-propanol as the H donor when compared to other solvents such as ethanol, 1-butanol, 2-butanol, tert-butanol and n-propanol [22].

2.2.1. Effect of Cu Loading on CTH of FA

The effect of copper loading on the catalytic transfer hydrogenation of FA to FAOL was investigated and the results are presented in Figure 8. Initially, pure HAp support was tested in the FA hydrogenation at 140 °C and exhibited relatively low FA conversion of 6% and moderately FAOL selectivity of 61% was attained. Copper modified HAp catalysts were tested and found to be complete selective to FAOL and exhibited different conversion values based on the copper loading (2–20 wt.%). Thus, enhanced activity in FA conversion and FAOL selectivity was achieved because of the introduction of copper. However, the FA conversion varies between 56 and 96% with the Cu loadings which had significant role in the final activity of the catalysts. Highest conversion of FA was obtained over 5CuHAp catalyst and thereafter, the conversion declined with copper loading. Fan et al. reported that the basic γ-Fe2O3@HAP catalyst exhibited 96.2% of FA conversion at 180 °C in 10 h reaction time [31]. Chen et al. reported that Cu/MgO-Al2O3 catalyst shows complete conversion of FA and 89.3% of FAOL selectivity at 210 °C in 1 h reaction time [50]. In this work, we found that 5CuHAp catalyst exhibited highest conversion of FA (96%) and selectivity (100%) to FAOL at 140 °C in 4 h reaction time.
The catalytic activity results are well correlated with the physico-chemical properties of the catalysts which are obtained by using different characterisation techniques. From XRD results, increasing the loadings above 5 wt.% Cu leads to aggregation of Cu on the surface of HAp. UVDRS analysis also suggests that the successful impregnation of Cu-ion into HAp structure at the same time was found to be increasing the crystallinity at higher loadings. In addition, over 5 wt.% Cu catalyst, N2O and TPD-CO2 results demonstrated that 5CuHAp owned maximum number of basic sites and copper active surface area compared to all the investigated catalysts. The plot between turn over frequency (TOF) versus Cu loading describes the relation between catalytic activity and the Cu loading (Figure 9), wherein the TOF is proportional to the rate of FA molecules converted per second per site of copper. TOF is much higher for the 2CuHAp catalyst could be due to existence of isolated copper ions in the sample. The similar observation was also reported by Chary et al. in the case of Cu-Al2O3 catalysts [51]. TOF values were gradually declined with copper loading and obtained higher TOF values at lower Cu loading.

2.2.2. Effect of Catalyst Weight on CTH of FA

To evaluate the catalyst effectiveness in the hydrogen transfer during FA conversion to FAOL, the amount of catalyst was varied from 25 to 125 mg. FA conversion is increased with the catalyst mass from 25 to 125 mg (Figure 9). The selectivity remained constant until 100 mg and thereafter, slightly declined at 125 mg of catalyst. As the catalyst amount increased from 25 to 100 mg, the FA conversion increased from 28% to 96% while the selectivity towards FAOL was constant at 100%. Henceforth, 100 mg catalyst loading was selected as the optimal weight for the better performance and chosen for the further catalytic activity tests.

2.2.3. Effect of N2 Pressure on CTH of FA

The effect of reaction pressure on the catalytic activity was evaluated for 5CuHAp catalyst. Figure 5 represents the influence of reaction pressure on the catalytic performances. It was found that the reaction pressure had significant influence on FA conversion and selectivity. From Figure 10, conversion and selectivity increased with the reaction pressure up to 2 MPa and the values are almost similar at 3 MPa as well. Above 3 MPa, the selectivity slightly declined caused by the formation tetrahydro furfuryl alcohol (THFAOL). Finally, 2 MPa was found to be the most optimised pressure where the highest performance can be achieved.

2.2.4. Effect of Reaction Temperature on CTH of FA

The effect of temperature on CTH of FA to FAOL with 5CuHAp catalyst was investigated with temperature between 110 and 150 °C and at reaction time of 4 h, with 100 mg of catalyst (Figure 11). The reaction temperature was one of the key parameters in the catalytic hydrogen transfer of FA to FAOL. As shown in Figure 11, within 4 h of reaction at 110 °C, the conversion of furfural was only 24%. When the reaction temperature increased from 110 to 150 °C, the FA conversion increased from 24% to 98% but the reaction is highly selective towards FAOL. However, the FAOL selectivity was independent of temperature, at 150 °C the reaction was accompanied with the formation of small amount of THFAOL as confirmed from GC-MS spectra, suggesting the high selectivity performance of 5CuHAp catalyst.

2.2.5. Effect of Reaction Time on CTH of FA

The effect of reaction time over 5CuHAp catalyst was investigated on the FA conversion and product selectivity. As shown in Figure 12, the conversion of FA increased upon increasing the reaction time. More specifically, after 3 h, conversion of 85% was achieved, which increased steadily to 96% after 4 h. The selectivity of FAOL was maximum from starting time to 4 h reaction time. However, at extended time to 5 h there is a slight decline in the selectivity of FAOL and very small amount of THFAOL formed.

2.2.6. Recyclibity of 5CuHAp

To examine the stability of the catalysts we carried out recyclability experiments for 5CuHAp catalyst under optimised conditions. In each cycle, the catalyst was removed from the reaction mixture by simple centrifugation, and washed with ethanol before drying at 60 °C under vacuum for 6 h. After drying, the catalyst was tested for the reproducibility of the results in similar conditions (Figure 13). The regeneration and reproducibility of the results were repeated in five successive cycles. From Figure 13, a slight drop in the FA conversion from cycle 1 to cycle 5 was noticed, while the selectivity to furfuryl alcohol remained constant. The decline in conversion is mainly due to the catalyst deactivation occurred through surface oxidation of metallic copper during recycling process. This phenomenon was confirmed by carrying out additional test with spent catalyst recycling. After five cycles, spent catalyst was re-calcined and reduced in 5% H2/Ar flow and tested for CTH of FA. The tested catalyst achieved 91% conversion of FA and 100% selectivity to FAOL and regeneration of the initial catalyst activity was gained. The morphology of the spent 5CuHAp catalyst is shown in Figure 7 and significant HAp rods accumulation can be noticed. The catalytic performance for the CTH reaction of FA to FAOL over CuHAp is compared in Table 2 with different copper catalysts reported in recent literature.

3. Materials and Methods

3.1. Synthesis of Catalysts

The double decomposition method was used to synthesise calcium hydroxyapatite. The synthesis procedure is as follows: a mixture of ammonium hydrogen phosphate solution (Sinopharm Chemical Reagent Co., Ltd., Shanghai, China) (0.4 M) with calcium nitrate solution (Sinopharm Chemical Reagent Co., Ltd., China) (0.5 M) was prepared in the presence of ammonia. The mixture of ammonium hydrogen phosphate (Sinopharm Chemical Reagent Co., Ltd., China) (7.92 gm in 100 mL) and ammonia (Kermel Reagents Co., Ltd., Tianjing, China) (70 mL) is added dropwise to the boiling calcium nitrate solution (23.6 gm in 100 mL). The resulting mixture was further heated under reflux for 3 h at 80 °C and filtered in warm condition. The recovered precipitate solids were washed thoroughly with ultrapure hot water to eliminate the traces of nitrates before drying at 110 °C for 24 h. Finally, the dried solids were calcined at 400 °C for 2 h in ambient air atmosphere.
Copper catalysts with varying copper loadings (from 2.0 to 20.0 wt.%) were prepared on HAp supports by wet chemical impregnation method using aqueous copper nitrate solution. The prepared samples were dried at 110 °C in oven for 12 h and before calcining at 500 °C for 5 h in air atmosphere. All the catalysts are named as xCuHAp, where (x) represents the Cu loadings (%).

3.2. Activity Tests

CTH of FA was carried out in a stainless-steel autoclave reactor (10 mL) with an inserted glass liner. Reaction temperature was insured with an oil bath on a digital hotplate by a thermocouple. In a typical CTH experiment, the catalyst (100 mg), isopropanol as the solvent (5 mL), reactant FA (480 mg) and decane (50 μL, internal standard for GC) were initially introduced into the reactor. Subsequently, the reaction autoclave was purged with H2 gas. Prior to the activity tests, catalysts were activated ex situ in 5% H2/Ar flow (30 mL/min) at 350 °C for 2 h and then transferred to the reactor, under inert atmosphere (N2). The pressure was adjusted to an initial value of 2 MPa measured at room temperature. Further, the reactor was heated to the desired reaction temperature under a stirring rate of 700 rpm. The reaction products were analysed by a gas chromatograph (GC, Agilent, DB-WAX column) and further liquid by-products were analysed by GC–MS column (Agilent DB-WAX). To study the recyclability of the catalyst, at the end of hydrogenation run, the catalyst was removed from the reaction mixture by centrifugation and washed with ethanol before drying at 60 °C under vacuum for 6 h. The FA conversion is defined as the moles of FA reacted divided by the moles of initial introduced FA; similarly, the selectivity of FAOL is defined as the moles of FAOL produced divided by the moles of FA reacted; and the yield of FAOL is defined as the moles of FAOL produced divided by the moles of initial introduced FA.

3.3. Catalytic Characterisation

The synthesised catalysts were characterised to understand the structural and chemical properties such as basicity, surface area and morphology by using temperature programmed desorption (TPD), N2 sorption, scanning electron microscopy (SEM), X-ray diffraction (XRD) and FTIR techniques. XRD was performed using an Ultima IV diffractometer (Rigaku Corporation, Japan) with a Ni-filtered Cu Kα radiation (λ = 1.5406 Å) operated at 40 kV and 30 mA. The FT-IR spectra were recorded at room temperature on a spectrometer (Bruker TENSOR 27) in the range of 400–3500 cm−1. The specific surface areas were measured by N2 sorption at −196 °C temperature in Autosorb-1C instrument (Quanta chrome instruments, USA). The morphological features of the samples were obtained by SEM (Model: EVO 18, Carl Zeiss) instrument. TEM images were captured on Hitachi HT7700 operated at 100 kV. The copper content was determined by elemental analysis by using ICP-OES (M/s Thermo Scientific, iCAP6500 DU). Temperature-programmed reduction (TPR) studies were carried out on AutoChem 2910 (Micromeritics, Norcross, GA, USA) instrument. In TPR experiment, 100 mg of oven-dried catalyst sample was taken in a U-shaped quartz sample tube. The catalyst was mounted on top of a quartz wool plug. Before the TPR experiments, the catalyst sample was pretreated at 200 °C for 2 h under He flow. After pretreatment the sample was cooled to ambient temperature and TPR analysis was carried out in a flow of 5% H2-Ar from ambient temperature to 600 °C at a ramping rate of 10 °C/min. The surface basicity of catalyst samples was determined by using TPD (M/s Micromeritics, AutoChem 2910 instrument USA) and CO2 as a probe molecule in basicity experiments. In a typical experiment, ~50 mg of sample was loaded in a U-shaped quartz tube and pre-treated at 300 °C for 1 h in the flow of pure He. Thereafter, pre-treated sample was saturated with CO2 at 30 °C for 30 min. The physiosorbed CO2 was removed by treating the sample at 100 °C for 30 min in He flow. Finally, the amount of desorbed CO2 was estimated using TCD detector by heating the sample from 50–700 °C at a ramping rate of 10 °C/min. N2O decomposition experiments were also conducted on micrometric instruments (Auto Chem. 2910). Prior to analysis, the sample was reduced with H2 gas at 350 °C for 2 h followed by He purges for 30 min and then cooled to 80 °C. Thereafter, sample was exposed to 2% N2O-He for 30 min to oxidise Cu to Cu2O. Reduction of surface copper oxide species was performed by the similar procedure as TPR. Moreover, Cu surface area, dispersion and crystal size were evaluated from the total amount of H2 consumed during the TPR analysis and by N2O decomposition method.

4. Conclusions

In this work, we designed and developed inexpensive and environmentally benign Cu-modified hydroxyapatite (HAp) catalyst for CTH of furfural to furfural alcohol using iso-propanol as an internal H2 source. The Cu loading was found to have profound effect on the reaction performance. The X-ray diffraction patterns confirmed larger crystallites were formed with increasing copper loadings. Copper with 5 wt.% over HAp was the most optimal loading to exhibit desired catalytic properties. Systematic characterisation results revealed that over 5CuHAp catalyst, highly dispersed copper particles and high surface basicity was obtained. Complete selectivity and 96% conversion with high TOF values were achieved over the 5CuHAp catalyst. Moreover, optimised reaction conditions such as temperature, pressure and catalyst weight were determined. The stability of the catalysts was also studied with regeneration and reusability tests and scope to develop further to gain high catalyst durability for the commercial application. Henceforth, 5CuHAp catalyst is promising and shows better performance compared to other Cu-based catalysts published in the literature at relatively lower temperature.

Author Contributions

B.P. (conceptualisation) (writing—original draft) (software), P.K.S. (writing introduction, data analysis and curation) (methodology), G.S. (investigation), K.R. (software) R.R. (validation), K.R.R. (writing—review and editing), T.L. (supervision). All authors have read and agreed to the published version of the manuscript.

Funding

This research was funded by National Natural Science Foundation of China (Project No.51871114).

Acknowledgments

We gratefully acknowledge the financial support from National Natural Science Foundation of China.

Conflicts of Interest

The authors declare no conflict of interest.

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Catalysts 10 01045 g001 550
Figure 1. X-ray diffractograms of CuHAp catalysts with different Cu loadings.
Figure 1. X-ray diffractograms of CuHAp catalysts with different Cu loadings.
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Catalysts 10 01045 g002 550
Figure 2. FTIR spectra of CuHAp catalysts with different Cu loadings.
Figure 2. FTIR spectra of CuHAp catalysts with different Cu loadings.
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Figure 3. UVDRS spectra of CuHAp catalysts with different Cu loadings.
Figure 3. UVDRS spectra of CuHAp catalysts with different Cu loadings.
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Catalysts 10 01045 g004 550
Figure 4. TPR profiles of CuHAp catalysts with various Cu loadings.
Figure 4. TPR profiles of CuHAp catalysts with various Cu loadings.
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Figure 5. CO2-TPD profiles of CuHAp catalysts with different Cu loadings.
Figure 5. CO2-TPD profiles of CuHAp catalysts with different Cu loadings.
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Figure 6. (a) SEM image, (b) EDS results and (c–f) are corresponding EDS elemental mapping images of 5CuHAp catalyst.
Figure 6. (a) SEM image, (b) EDS results and (c–f) are corresponding EDS elemental mapping images of 5CuHAp catalyst.
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Figure 7. TEM images of (a) HAp, (b) 5 CuHAp (c) 20 CuHAp and (d) Spent 5Cu/HAp catalysts.
Figure 7. TEM images of (a) HAp, (b) 5 CuHAp (c) 20 CuHAp and (d) Spent 5Cu/HAp catalysts.
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Catalysts 10 01045 g008 550
Figure 8. The effect of copper loadings (2–20 wt.%) on the CTH of FA to FAOL and corresponding TOF values are presented. Reaction Conditions: The catalyst amount (100 mg), 2-propanol (5 mL), FA (480 mg), reaction temperature—140 °C at 2 MPa N2 pressure and reaction time—4 h.
Figure 8. The effect of copper loadings (2–20 wt.%) on the CTH of FA to FAOL and corresponding TOF values are presented. Reaction Conditions: The catalyst amount (100 mg), 2-propanol (5 mL), FA (480 mg), reaction temperature—140 °C at 2 MPa N2 pressure and reaction time—4 h.
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Catalysts 10 01045 g009 550
Figure 9. The effect of catalyst weight (mg) on the CTH of FA over 5CuHAp catalyst. Reaction conditions: catalyst amount (25–125 mg), 2-propanol (5 mL), FF (480 mg), reaction temperature—140 °C at 2 MPa N2 pressure and reaction time—4 h.
Figure 9. The effect of catalyst weight (mg) on the CTH of FA over 5CuHAp catalyst. Reaction conditions: catalyst amount (25–125 mg), 2-propanol (5 mL), FF (480 mg), reaction temperature—140 °C at 2 MPa N2 pressure and reaction time—4 h.
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Figure 10. The effect of N2 pressure on the CTH of FA over 5CuHAp. Reaction Conditions: The catalyst amount (100 mg), 2-propanol (5 mL), FF (480 mg), reaction temperature—140 °C at (1–4) MPa N2 pressure and reaction time—4 h.
Figure 10. The effect of N2 pressure on the CTH of FA over 5CuHAp. Reaction Conditions: The catalyst amount (100 mg), 2-propanol (5 mL), FF (480 mg), reaction temperature—140 °C at (1–4) MPa N2 pressure and reaction time—4 h.
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Figure 11. The effect of reaction temperature on the CTH of FA over 5CuHAp. Reaction Conditions: The catalyst weight (100 mg), 2-propanol (5 mL), FF (480 mg), reaction temperature—(110–150 °C) at 2 MPa N2 pressure and reaction time—4 h.
Figure 11. The effect of reaction temperature on the CTH of FA over 5CuHAp. Reaction Conditions: The catalyst weight (100 mg), 2-propanol (5 mL), FF (480 mg), reaction temperature—(110–150 °C) at 2 MPa N2 pressure and reaction time—4 h.
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Figure 12. The effect of reaction time on the CTH of FA over 5CuHAp. Reaction Conditions: The catalyst amount (100 mg), 2-propanol (5 mL), FF (480 mg), reaction temperature—140 °C at 2 MPa N2 pressure and reaction time—(1–5 h).
Figure 12. The effect of reaction time on the CTH of FA over 5CuHAp. Reaction Conditions: The catalyst amount (100 mg), 2-propanol (5 mL), FF (480 mg), reaction temperature—140 °C at 2 MPa N2 pressure and reaction time—(1–5 h).
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Figure 13. Recyclability test for 5CuHAp catalyst. Reaction Conditions: The catalyst amount (100 mg), 2-propanol (5 mL), FF (480 mg), reaction temperature—140 °C at 2 MPa N2 pressure and reaction time—(4 h).
Figure 13. Recyclability test for 5CuHAp catalyst. Reaction Conditions: The catalyst amount (100 mg), 2-propanol (5 mL), FF (480 mg), reaction temperature—140 °C at 2 MPa N2 pressure and reaction time—(4 h).
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Table
Table 1. Catalytic properties from ICP, BET, N2O titration and H2-TPR results of CuHAp catalysts with different Cu loadings were summarised.
Table 1. Catalytic properties from ICP, BET, N2O titration and H2-TPR results of CuHAp catalysts with different Cu loadings were summarised.
CatalystCu
(wt.%) a		BET Surface Area (m2/gm) bCu
Surface Area (m2/gm) c		Particle Size (nm) cH2 Uptake
(µmol/g) d
HAp-76---
2CuHAp1.81622043.351
5CuHAp4.57522103.20127
10CuHAp8.9461434.70152
15CuHAp14.143927.30160
20CuHAp18.7376210.8174
a Results from ICP-OES, b results from BET measurements; c results from N2O titration; d results from H2-TPR.
Table
Table 2. Comparison of the catalytic activity of Cu-based catalysts with various copper loadings published in the literature on CTH of FA to FAOL reaction.
Table 2. Comparison of the catalytic activity of Cu-based catalysts with various copper loadings published in the literature on CTH of FA to FAOL reaction.
CatalystH-DonorT (°C)P (MPa)Time (h)XFA (%)SFAOL (%)Ref.
Cu/AC-SO3H2-PrOH15045100100[52]
Cu-AlMeOH20012.510094[35]
Cu-Mg-Al2-PrOH150-6100100[21]
Cu-Mg-Al2O32-PrOH210-110089.3[50]
CuCs-MCMHCOOH170-110099.6[53]
CuHAp2-PrOH1402496100This work
2-PrOH = 2-propanol, MeOH = methanol, X—conversion, S—selectivity.

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Putrakumar, B.; Seelam, P.K.; Srinivasarao, G.; Rajan, K.; Rajesh, R.; Rao, K.R.; Liang, T. High Performance and Sustainable Copper-Modified Hydroxyapatite Catalysts for Catalytic Transfer Hydrogenation of Furfural. Catalysts 2020, 10, 1045. https://doi.org/10.3390/catal10091045

AMA Style

Putrakumar B, Seelam PK, Srinivasarao G, Rajan K, Rajesh R, Rao KR, Liang T. High Performance and Sustainable Copper-Modified Hydroxyapatite Catalysts for Catalytic Transfer Hydrogenation of Furfural. Catalysts. 2020; 10(9):1045. https://doi.org/10.3390/catal10091045

Chicago/Turabian Style

Putrakumar, Balla, Prem Kumar Seelam, Ginjupalli Srinivasarao, Karthikeyan Rajan, Rajendiran Rajesh, K. Ramachandra Rao, and Tongxiang Liang. 2020. "High Performance and Sustainable Copper-Modified Hydroxyapatite Catalysts for Catalytic Transfer Hydrogenation of Furfural" Catalysts 10, no. 9: 1045. https://doi.org/10.3390/catal10091045

APA Style

Putrakumar, B., Seelam, P. K., Srinivasarao, G., Rajan, K., Rajesh, R., Rao, K. R., & Liang, T. (2020). High Performance and Sustainable Copper-Modified Hydroxyapatite Catalysts for Catalytic Transfer Hydrogenation of Furfural. Catalysts, 10(9), 1045. https://doi.org/10.3390/catal10091045

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