Palm Oil Conversion to Bio-Jet and Green Diesel Fuels over Cobalt Phosphide on Porous Carbons Derived from Palm Male Flowers

: Porous carbon was successfully synthesized from palm male ﬂowers (PMFs), using microwave-assisted potassium hydroxide (KOH) activation and was used as a catalyst support for the conversion of palm oil into bio-hydrocarbons, in fractions of green diesel and bio-jet fuel. Palm male ﬂower-derived porous carbon (PC), consolidated with well dispersed cobalt phosphide (CoP) nanoparticles, was synthesized by simple wet-impregnation with subsequent thermal treatment. The physicochemical properties of the synthesized CoP / PC catalysts were evaluated by various techniques including proximate and ultimate elemental analysis, FTIR, XRD, N 2 sorption, SEM, TEM–EDS, and NH 3 -temperature programmed desorption (TPD). The effects of the pyrolysis temperatures (600 − 900 ◦ C), used for the impregnated samples before the reduction process, on catalyst properties and catalytic performance were investigated. Moreover, the effect of a liquid hourly space velocity of 0.5–1.5 h − 1 and reaction temperatures of 340–420 ◦ C was studied in the palm oil conversion. The catalyst pyrolyzed at 600 ◦ C possessed the greatest particle dispersion and surface area, and showed the highest yield of liquid hydrocarbon product (C9–C18). We also found that the high pyrolysis temperature above 800 ◦ C partially transformed the Co 2 P phase into CoP one which significantly exhibited higher cracking activity and bio-jet selectivity, due to the improved acidity of the catalyst.


Introduction
Nowadays, the depletion of petroleum due to the annual acceleration of energy consumption has become a worldwide agenda, and created a necessity for the exploration of renewable and sustainable fuels and chemicals [1]. In recent decades, bioresources such as lignocellulosic materials, organic wastes, and plant oils, have been utilized as feedstocks for the production of renewable biofuel and bio-based chemicals, providing some levels of the global reduction of CO 2 greenhouse gas. Many approaches have been proposed to efficiently convert plant oils into biofuels. Among them, transportation biofuels in the form of liquid hydrocarbons could be produced via catalytic deoxygenation reaction (DO) through the main reaction routes including hydrodeoxygenation (HDO) and decarboxylation/decarbonylation (DeCO x ), with H 2 O and CO 2 /CO as by-products, respectively [2,3]. decarboxylation/decarbonylation (DCOx). Hui et al. [31] prepared activated carbon-supported nickel phosphide catalysts via wet impregnation and tested them on the deoxygenation of palmitic acid for high-grade diesel production. They claimed that NiP supported on activated carbons offered the highest oil production yield of 56 wt %. Moreover, the main products were C 15, and the minor ones were C 11 -C 14 alkanes and alkenes. They indicated that NiP favored deoxygenation through the DCOx pathway, which required lower H 2 consumption.
As described above, cobalt phosphide is one of the promising catalysts for deoxygenation due to its high activity and selectivity of deoxygenation products. However, very few studies investigated the use of cobalt phosphide catalysts in the deoxygenation of vegetable oils for biofuel production. Hence, this study aims at using cobalt phosphide (CoP) catalysts for palm oil conversion to bio-hydrocarbons. In this process, porous carbon derived from palm male flowers (PMFs) using microwave-assisted potassium hydroxide (KOH) activation, was employed as a catalyst support. The PMF was an abundant and low-cost agricultural waste. The approach to use wastes from palm industry as a major component in the catalytic materials for the production of palm-based biofuels offers an alternative concept in biorefinery. Consequently, the performance of the developed catalysts for producing bio-based diesel and jet fuels was presented and discussed. The selectivity to each biofuel product can be successfully controlled by tuning the catalyst properties and reaction conditions.

Synthesis of Cobalt Phosphide@PC Catalysts
The PMF porous carbon (PC) was prepared by a microwave-assisted activation method using KOH as an activating agent. Raw PMFs were pre-carbonized at 500 • C under nitrogen with a flow rate of 100 mL/min [32]. The carbonized PMFs were physically mixed with KOH with a ratio of PMF char: KOH ratios at 2.0 (w/w). The ground mixture was placed in a quartz crucible followed by activation in a custom-made microwave pyrolyzer (Samsung MS23F301EAW) with a frequency of 2.45 GHz. The activation was performed at a microwave power of 700 W using a constant radiation time period of 6 min [33]. Afterwards, the PCs were passivated at room temperature under N 2 atmosphere, and then washed with 0.5 M HCl and deionized water several times until a neutral pH was obtained. The washed PCs were dried at 105 • C overnight before being crushed and sieved to obtain PCs of 0.18−0.5 mm in size. The PC sample prepared at the optimum condition was selected as a support for the preparation of the cobalt phosphide catalysts.
Series of cobalt phosphide supported on PC were synthesized by a wet impregnation method using cobalt (II) nitrate hexahydrate (Co(NO 3

Catalytic Deoxygenation of the Palm Olein Oil
The deoxygenation of the palm olein oil over the as-synthesized cobalt phosphide supported on PC was carried out in a down-flow trickle-bed reactor having an internal tube dimension of 7 mm in diameter and 700 mm long. Prior to the reaction test, 8 mL (2.5 g) of granular catalyst with sizes of 150-450 µm was loaded into the middle zone of the reactor. The catalyst was subsequently "in situ" reduced under a H 2 atmosphere with a 50 mL/min (99.99% purity, Praxair Co., Ltd., Bangkok, Thailand) at 600 • C for 3 h. Then, the reactor was cooled down to the target reaction temperature (340-420 • C) and was pressurized with H 2 to 50 bar controlled by a back pressure regulator. In deoxygenation, the palm oil was continuously fed by a HPLC pump at a varied liquid hourly space velocity (LHSV) of 0.5-1.5 h −1 under the use of a H 2 /liquid ratio of 1000 N (cm 3 /cm 3 ). The start-up time was at 4 h when the system was in a steady-state condition. Each experiment entry was done on fresh catalysts in order to eliminate the effect of catalyst deactivation that might occur after each experiment. The liquid product was periodically collected at every 2 h intervals for analysis. The gas products (C 3 H 8 , C 2 H 6 , CH 4 , CO, CO 2 ) were analyzed by online-gas chromatography (GC) equipped with a thermal conductivity detector (TCD) and a flame ionization detector (FID) (GC-2010 Plus, Shimadzu) and using Rt-Alumina BOND/KCL, Porapak Q, and MS-13X analytical columns. The liquid product compositions were analyzed by an offline gas chromatography equipped with a mass spectrometer detector (GCMS-QP2020, Shimadzu, Japan) and a capillary column (DB-1HT, 30 m × 0.32 mm × 0.1 µm). The conversion of oil feed was defined as a mass of triglyceride change into others (intermediates and hydrocarbons). The product yields were determined based on the mass balance of liquid hydrocarbon in the products corresponding to the oil feed. The conversion of palm oil, liquid hydrocarbon (LHC) yield, selectivity to green diesel (C 15 -C 18 ) and bio-jet (C 9 -C 14 hydrocarbon) were calculated using the following equations:

Characterization of PC and PC-Supported Cobalt Phosphide Catalysts
Proximate analysis was used to determine the chemical composition, including the moisture, volatile substances, fixed carbon and ash [34]. The moisture content, which was the mass of water in samples, was determined by drying process according to an American Society for Testing Materials, ASTM D2867-99 method (ASTM, 2014) [35]. Volatile substances, which were organic contents in the sample that could be released during the heating process, were measured under an inert atmosphere according to an ASTM D5832-98 (ASTM, 2008) [34,36]. Ash, which was referred to an inorganic component in the carbon structure, was analyzed by direct combustion according to an ASTM D2866-94 (ASTM, 2011) [34,36]. A non-volatile carbon remaining in the sample referred to as fixed carbon was calculated by subtracting techniques [34,36]. Ultimate analysis by CHN elemental analyzer (Leco truespec CHN-628) was used to determine the elemental compositions of raw PMF and as-prepared porous carbon (i.e., carbon, hydrogen, oxygen and nitrogen). The oxygen percentage was directly calculated by subtraction from other elemental compositions in the ultimate analysis. All the analyses are shown in an as-received basis.
The porosity and pore structure of the as-received PCs and CoP/PC catalysts were determined by nitrogen adsorption-desorption isotherm analysis at −196 • C using a gas sorption analyzer (Quantachrome Autosorp iQ-MP-XR). The Brunauer-Emmett-Teller (BET) model was used for the determination of the BET surface area (S BET ). The pore size distribution was analyzed by using the density functional theory (DFT) model, while the micropore volume (V mic ) was determined by the t-plot model. The total pore volume (V T ) was evaluated by a condensation of liquid nitrogen at the relative pressure of 0.99. The mesopore volume (V mes ) was calculated by subtracting the micropore volume from the total pore volume [32].
The surface functional group characteristics of the PMF, PC, and CoP/PC catalysts were studied using the Fourier transform infrared spectroscopy, FTIR (Perkin Elmer UATR Two). The infrared absorption spectra were measured in transmission mode with a wavenumber range from 4000-500 cm −1 [32]. The samples were put into infrared platform and screw-impressed directly before performing the FTIR data collection. X-ray diffractograms of all the catalysts were achieved using Cu-Kα radiation generated at 40 kV and 40 mA, in steps of 0.01 • S −1 with a step time of 0.5 s over the range of 5 • < 2θ < 90 • on an X-ray diffractometer, XRD (SmartLab, Rigaku, Japan). The crystalline size of the catalysts was calculated from the XRD data using the Debye-Scherrer formula.
The morphology of the PC and CoP/PC catalysts were examined by a scanning electron microscope, SEM (Zeiss EVO50) operating at 20 kV and a transmission electron microscope, TEM (JEOL JEM-2100plus) equipped with an energy dispersive X-ray spectrometer (EDS). NH 3 -temperature programmed desorption (TPD) was carried out using Quantachrome Chemisorption Analyzer ChemStar TPX Series, equipped with a thermal conductivity detector using 5% NH 3/ He as a probe gas.

Physicochemical Characteristics of PC
The proximate and ultimate analysis (elemental compositions; C, H, N) of the raw PMF, carbonized PMF and PMF-derived porous carbon (PC) are shown in Table 1. A high C percentage is determined from both carbon atoms of the fixed carbon and volatile matters in the porous carbon structure. The observed small amount of N content could be from a native component of plant-based materials such as enzymes or protein, and remains chemisorbed nitrogen in the carbon structure during carbonization [30,34]. The PMF, carbonized PMF and PC have an N content lower than 1.3% (0.9-1.2%). Typically, the H element was chemically bonded with carbon atoms; however, the ratio of H to C may be influenced by moisture. The composition of PMF has the lowest C content about 43.7% since it has a high O content (52.6%) in the form of oxygenated compounds and the moisture of lignocellulosic biomass [37]. Furthermore, the C content increases after the pre-carbonization step, as measured in the carbonized PMF (68.7%) due to the devolatilization. The PC produced in this study contains a high C content of about 79.1%, which is quite similar to the conventional porous carbon consisting of 80-90% C [38]. The proximate analysis, represented in Table 1, provides the gross composition of the biomass in four parameters, namely moisture, fixed carbon, volatile matter, and ash. The fixed carbon represents the non-volatile carbon matters, which are the major component in the porous carbon structure, while ash reflects the persistent component (typically inorganic matters) found in the biomass. For instance, the pores can be blocked when the porous carbon contains a high ash content, leading to the lower BET surface area [39]. The BET surface area of the obtained PC is approximately 964.0 m 2 /g with total pore volume (V T ) of 0.57 cm 3 /g, as demonstrated in Table 2. The pore structure of the PC is commonly identified by using N 2 adsorption-desorption technique [34]. As shown in Figure 1a, the PC sample displays a mixed characteristic of Type I and Type IV isotherms, classified by IUPAC, which exhibit a specific combination of microporous and mesopores structures [40,41]. Table 2. Pore characteristics of PMF porous carbon (PC) and CoP/PC catalysts.

Conditions
Pore Characteristics D XRD (nm)

Characterization of CoP/PC Catalysts
CoP/PC catalysts were synthesized by the wet impregnation technique using an initial P/Co of 1.0 molar ratio using H3PO4 with the controlled 10% metal loading, followed by the pyrolysis of impregnated samples (phosphate species), and the H2 reduction of phosphate species into cobalt phosphide, respectively. The effect of the pyrolysis temperatures of impregnated samples before the reduction process was investigated on the phase formation of cobalt phosphides and their reactivity in palm olein oil deoxygenation. In order to examine the mentioned CoP/PC catalysts regarding the specific properties, a series of CoP/PC catalysts were characterized.
In Figure 2a, the FTIR spectra of all CoP/PC catalysts were observed with a weak peak intensity between 635 and 535 cm −1 , corresponding to the phosphate vibrations in the CoP catalysts [44], whereas this feature is absent in the FTIR spectrum of the bare PC support. These results confirm that The surface chemistry of PC was evaluated by using FTIR. The FTIR spectra of the PMF, carbonized PMF, and the PC were compared to that of the commercial activated carbon. In Figure 1b, the band in the 3680-3000 cm −1 region is related to -OH stretching indicating the characteristic of hydroxyl and carbonyl functional groups of lignin in lignocellulosic biomass, as expected from PMF feedstock. The vibrations at about 2925 and 2850 cm −1 correspond to the aliphatic C-H stretching assigned to the polysaccharide of cellulose and hemicellulose. Moreover, aromatic -C=C-stretching of lignin is mainly observed between 1600 and 1512 cm −1 . Other bands of lignin also situate at 1380-1240 cm −1 and 1460 cm −1 . The C=O vibrations assigned for cellulose and hemicellulose are observed from 1200 to 950 cm −1 . On the contrary, the spectra below 500 cm −1 can be ascribed to the vibration of inorganic components [42]. The absence of vibration bands in the 3680-2850 cm −1 region in the PMF and PC samples are due to the decomposition of lignocellulosic components during carbonization and microwave activation [43]. Additionally, the activation power of 700 W seems to successfully convert PMF into porous carbon, with the surface characteristic as similar as the commercial activated carbon (shown in the inset graph of Figure 1b), confirmed by the resemblance of their FTIR spectra across the measured region. Furthermore, the SEM micrographs of the PC are shown in Figure 1c for the external surface and Figure 1d for the cross-sectional view. The external surface of the PC shows various external small pore cavities. Moreover, various cavities can be observed inside the external pores-like spongy matrix, which is displayed in the cross-section SEM image (Figure 1d). The surface and pore structures of the PC signify its good potential as a catalyst support.

Characterization of CoP/PC Catalysts
CoP/PC catalysts were synthesized by the wet impregnation technique using an initial P/Co of 1.0 molar ratio using H 3 PO 4 with the controlled 10% metal loading, followed by the pyrolysis of impregnated samples (phosphate species), and the H 2 reduction of phosphate species into cobalt phosphide, respectively. The effect of the pyrolysis temperatures of impregnated samples before the reduction process was investigated on the phase formation of cobalt phosphides and their reactivity in palm olein oil deoxygenation. In order to examine the mentioned CoP/PC catalysts regarding the specific properties, a series of CoP/PC catalysts were characterized.
In Figure 2a, the FTIR spectra of all CoP/PC catalysts were observed with a weak peak intensity between 635 and 535 cm −1 , corresponding to the phosphate vibrations in the CoP catalysts [44], whereas this feature is absent in the FTIR spectrum of the bare PC support. These results confirm that the cobalt phosphide phase was observed on the PC support at the different pyrolysis temperatures from 600 • C to 900 • C. Varying temperatures in the pyrolysis of the impregnated samples, which are totally amorphous, reveal an influence on transformation of CoP crystalline structure in the corresponding activated catalysts (after the reduction process), as displayed in Figure 2b. The observed XRD broad peak around 40 • -50 • represents the overlapping peaks between the carbon support and the characteristic of an amorphous and well dispersed cobalt phosphide phase on carbon support, in a reduced catalyst obtained by pyrolysis at 600 • C. On the other hand, the sharp and high intensity peaks were found when the pyrolysis temperature further increased before reduction. Typically, the diffraction peaks at 40.  [45]. The strong peaks of the Co 2 P phase were found at 700 • C while the Co 2 P was also transformed into a CoP species when increasing the pyrolysis temperature to 800 • C and higher. This was evidenced by the observed mixture of highly crystalline Co 2 P and CoP phases at 800 and 900 • C of the reduced catalysts. In addition, the CoP species is significantly formed at a high temperature that requires high-phase formation energy. According to these results, it was noted that the pyrolysis temperature before the reduction process was a key factor in the formation of cobalt phosphides in the reduced catalysts and increasing the pyrolysis temperature during catalyst preparation results in the transformation from Co 2 P to CoP crystalline structures. As shown in Table 2, the crystallite size of the cobalt phosphide in the reduced catalysts was calculated by the Debye-Scherrer equation (D xrd ). The cobalt phosphide crystallite sizes are significantly enlarged from 3.4 to 21.7 nm by raising the pyrolysis temperature from 600 to 900 • C.
According to these results, it was noted that the pyrolysis temperature before the reduction process was a key factor in the formation of cobalt phosphides in the reduced catalysts and increasing the pyrolysis temperature during catalyst preparation results in the transformation from Co2P to CoP crystalline structures. As shown in Table 2, the crystallite size of the cobalt phosphide in the reduced catalysts was calculated by the Debye-Scherrer equation (Dxrd). The cobalt phosphide crystallite sizes are significantly enlarged from 3.4 to 21.7 nm by raising the pyrolysis temperature from 600 to 900 °C.  Figure 2c displays the N2 adsorption-desorption isotherms of the reduced CoP/PC catalysts, prepared using different pyrolysis temperatures. All the isotherms show the typical Type I isotherm combined with the type IV isotherm with a narrow hysteresis loop at the high relative pressure. These results suggest that micropores with a mesopores formation exist in the samples, and the isotherm data were derived to calculate porous parameters, as shown in Table 2. An increase in the pyrolysis temperature before the reduction process leads to the shifting of the isotherm toward the lower volume of the adsorbed N2, suggesting a decreasing surface area of catalysts [46]. Furthermore, the decrease in the surface area of catalysts might be affected by the mean particle size of the CoP catalyst due to the aggregation at high-temperature pyrolysis [47]. The pore size distribution (PSD) analysis of the obtained catalysts was evaluated by the DFT model (Figure 2d). The PSD of the samples could be separated into two main distribution ranges within 4 nm. The catalysts have narrow micropores  Figure 2c displays the N 2 adsorption-desorption isotherms of the reduced CoP/PC catalysts, prepared using different pyrolysis temperatures. All the isotherms show the typical Type I isotherm combined with the type IV isotherm with a narrow hysteresis loop at the high relative pressure. These results suggest that micropores with a mesopores formation exist in the samples, and the isotherm data were derived to calculate porous parameters, as shown in Table 2. An increase in the pyrolysis temperature leads to the shifting of the isotherm toward the lower volume of the adsorbed N 2 , suggesting a decreasing surface area of catalysts [46]. Furthermore, the decrease in the surface area of catalysts might be affected by the mean particle size of the CoP catalyst due to the aggregation at high-temperature pyrolysis [47]. The pore size distribution (PSD) analysis of the obtained catalysts was evaluated by the DFT model (Figure 2d). The PSD of the samples could be separated into two main distribution ranges within 4 nm. The catalysts have narrow micropores with the existence of sharp peaks between 0.5 and 1.0 nm, while the PSD around 1.3 nm is also observed with a smaller density. The tiny mesopores of narrow PSD are in the range of around 2.0-2.5 nm. The increasing pyrolysis temperature before the reduction in the catalyst preparation significantly shifts and elevates the mesopore size distribution because of the collapse of micropores.
The acidity of the reduced catalysts was also measured using NH 3 -TPD. The total NH 3 uptakes range from 52.5 to 118.1 µmol/g, as reported in Table 2. The catalyst with a high crystalline CoP phase (CoP/PC-900) has much larger NH 3 uptake than those of the other catalysts. The lowest acidity is found in the CoP/PC-600 with the main phase of Co 2 P. However, a recent study [10,34] found that the highly acidic catalyst presents an excellent deoxygenation activity since the cleavage of C-C is favorably catalyzed by the acid sites of catalysts. Moreover, the hydrocracking of heavy hydrocarbons to light molecules is extremely promoted in the similar contribution [42]. TEM images and the particle size distribution curves of the reduced catalysts prepared with various pyrolysis temperatures before the H 2 reduction are shown in Figure 3 on the PC support. The cobalt phosphide particle size become larger with the increasing pyrolysis temperature before the activation into the active phase by H 2 reduction, due to the aggregation of metal salt particles on carbon support. The average particle sizes of cobalt phosphide are enlarged from 15.8 nm (at 600 • C) to 31.2 (at 900 • C). In addition, the particle size distribution of the CoP catalysts was investigated with the accuracy of ±1 nm. All the samples show the similar trends of narrow size distribution within 10-20 nm, suggesting the well-controlled size distribution via the present synthesis method. The TEM image of the reduced CoP/PC-600 catalyst with EDS mapping (Figure 4) confirms the elemental composition of the catalyst. The corresponding EDS mapping of the elemental results reveals a successful cobalt phosphide loading on the carbon support, and the uniform dispersion of CoP crystals surrounded by a carbon framework.
(CoP/PC-900) has much larger NH3 uptake than those of the other catalysts. The lowest acidity is found in the CoP/PC-600 with the main phase of Co2P. However, a recent study [10,34] found that the highly acidic catalyst presents an excellent deoxygenation activity since the cleavage of C-C is favorably catalyzed by the acid sites of catalysts. Moreover, the hydrocracking of heavy hydrocarbons to light molecules is extremely promoted in the similar contribution [42]. TEM images and the particle size distribution curves of the reduced catalysts prepared with various pyrolysis temperatures before the H2 reduction are shown in Figure 3: (a) 600 °C, (b) 700 °C, (c) 800 °C, and (d) 900 °C. All the catalysts exhibit a good dispersion of the cobalt phosphide particles on the PC support. The cobalt phosphide particle size become larger with the increasing pyrolysis temperature before the activation into the active phase by H2 reduction, due to the aggregation of metal salt particles on carbon support. The average particle sizes of cobalt phosphide are enlarged from 15.8 nm (at 600 °C) to 31.2 (at 900 °C). In addition, the particle size distribution of the CoP catalysts was investigated with the accuracy of ±1 nm. All the samples show the similar trends of narrow size distribution within 10-20 nm, suggesting the well-controlled size distribution via the present synthesis method. The TEM image of the reduced CoP/PC-600 catalyst with EDS mapping (Figure 4) confirms the elemental composition of the catalyst. The corresponding EDS mapping of the elemental results reveals a successful cobalt phosphide loading on the carbon support, and the uniform dispersion of CoP crystals surrounded by a carbon framework.

Effects of Cobalt Phosphide Species on Palm Oil Deoxygenation Performance
The palm oil deoxygenation performance was impacted by the cobalt phosphide species, which was obtained from different pyrolysis temperatures during the catalyst preparation before the reduction process. The temperatures in the pyrolysis of impregnated samples determine the stoichiometry of the cobalt phosphide catalysts. This also affects the catalytic behavior of the corresponding catalysts. In this work, the effect of the pyrolysis temperatures during the catalyst preparation on the conversion and the product yield with % selectivity of liquid hydrocarbons were conducted in the wide temperature ranges from 600 to 900 • C under a fixed operating condition as follows: reaction temperature: 400 • C; H 2 pressure: 50 bar; and H 2 /Oil ratio: 1000 N (cm 3 /cm 3 ). Figure 5a shows the impacts of the pyrolysis temperature during the catalyst preparation on the palm olein oil conversion and the liquid hydrocarbon yield. All the catalysts achieved the 100% conversion, however, the catalysts obtained at a higher temperature from 600 to 900 • C slightly decreased the liquid hydrocarbons yield from 75.9 to 71.0%. In Figure 5b, the green diesel selectivity gradually decreased from 45.2 to 35.1%, while the bio-jet selectivity became greater when raising the pyrolysis temperature of the catalysts, perhaps due to the more catalytic hydrocracking presented in the samples with a higher total acidity e.g., the CoP/PC-800 and CoP/PC-900 catalysts ( Table 2). It should be noted that at the higher reaction temperature, the high cracking reactivity typically leads to the decrease in liquid hydrocarbon yield and green diesel selectivity, whereas yields of shorter-carbon chain molecules including biojet and gas products are enhanced. stoichiometry of the cobalt phosphide catalysts. This also affects the catalytic behavior of the corresponding catalysts. In this work, the effect of the pyrolysis temperatures during the catalyst preparation on the conversion and the product yield with % selectivity of liquid hydrocarbons were conducted in the wide temperature ranges from 600 to 900 °C under a fixed operating condition as follows: reaction temperature: 400 °C; H2 pressure: 50 bar; and H2/Oil ratio: 1000 N (cm 3 /cm 3 ). Figure  5a shows the impacts of the pyrolysis temperature during the catalyst preparation on the palm olein oil conversion and the liquid hydrocarbon yield. All the catalysts achieved the 100% conversion, however, the catalysts obtained at a higher temperature from 600 to 900 °C slightly decreased the According to the XRD results, at the low pyrolysis temperature during the catalyst preparation before the H2 reduction to phosphide, Co2P was firstly formed, and then followed by the formation of CoP with an increasing synthesis temperature corresponding to the sufficient energy of phase transformation [44,46]. It is noted that the CoP and Co2P phases would show different activity in deoxygenation. A recent study revealed that the cobalt phosphide catalysts prepared at the high pyrolysis temperature of phosphate salt on carbon supports, presented a high proportion of CoP phases [45,46], which was considered to be an active form of cobalt phosphide and exhibited a higher catalytic performance [24]. The performance of cobalt phosphide catalysts is directly related to the According to the XRD results, at the low pyrolysis temperature during the catalyst preparation before the H 2 reduction to phosphide, Co 2 P was firstly formed, and then followed by the formation of CoP with an increasing synthesis temperature corresponding to the sufficient energy of phase transformation [44,46]. It is noted that the CoP and Co 2 P phases would show different activity in deoxygenation. A recent study revealed that the cobalt phosphide catalysts prepared at the high pyrolysis temperature of phosphate salt on carbon supports, presented a high proportion of CoP phases [45,46], which was considered to be an active form of cobalt phosphide and exhibited a higher catalytic performance [24]. The performance of cobalt phosphide catalysts is directly related to the P/Co ratio in the cobalt phosphide structure leading to a type of cobalt phosphide phase present on the catalyst surface. These results explain the initial activity for these series catalysts [24]. In this sense, the rich P/Co ratio in the CoP phase would exhibit a greater amount of hydrogen spillover effect than the Co 2 P one, resulting in a higher activity.
The CoP/PC-600 catalyst was selected for the further study of the DO parameters including the DO temperatures and the LHSV, since the use of the CoP/PC-600 catalyst can achieve 100% palm oil conversion and the highest liquid hydrocarbon yield while the well dispersed nanosized cobalt phosphide particles are achieved (as shown in Figure 3a). Moreover, a lower preparation temperature could be beneficial in terms of energy consumption and investment cost for the equipment installation and operation.

Effects of DO Temperatures
The effect of deoxygenation temperatures (340-420 • C) over the CoP/PC-600 was investigated. It is found that the palm oil deoxygenation over the CoP/PC catalyst has a complete conversion in the temperature range of 340-420 • C (Figure 5c). The product yield kept quite constant in the reaction temperature range from 340 to 380 • C, but dropped at a temperature above 400 • C, suggesting the promotion of cracking activity. Abdulkareem Alsultan [13] and Asikin-Mijan [16] reported that the lower conversion was typically achieved at a lower deoxygenation temperature, which was not found in our study. As illustrated in Figure 5d, the selectivity of the liquid hydrocarbon products is varied with raising the reaction temperature from 340 to 420 • C. The product in the green diesel range (C 15 -C 18 hydrocarbons) continuously declines, whereas the fraction of the bio-jet (C 9 -C 14 hydrocarbons) tends to increase since the cracking reaction is favorable at a higher temperature to convert longer-chain hydrocarbons into shorter-chain hydrocarbons [48,49].

Effects of Liquid Hourly Space Velocity (LHSV)
The LHSV is one of the most important variables in the continuous flow trickle bed reactor system to evaluate catalyst effectiveness, the expected catalyst life time, and the reaction behavior [10]. Previous studies noted that the formation of white waxy oxygenated intermediates, mainly free fatty acids and long-chain esters, are observed at high operating LHSV leading to rapid blockage inside the reactor. Moreover, the low LHSV (long resident time) plays an important role for the isomerization and cracking reaction in the deoxygenation of triglyceride feedstock [29,30]. In this section, the influences of LHSVs on the conversion and product yield with a % selectivity of products were conducted at various LHSVs of 0.5, 1.0, and 1.5 h −1 under a fixed operating condition as follows: reaction temperature of 400 • C; H 2 Pressure of 50 bar; and H 2 /Oil ratio: 1000 N (cm 3 /cm 3 ) using CoP/PCs-600 catalyst. As displayed in Figure 5e, the LHSVs of 0.5 and 1.0 h −1 obtained 100% conversion at a deoxygenation temperature of 400 • C without waxy compounds. Nonetheless, an increase in LHSV from 1.0 to 1.5 h −1 gradually decreases the conversion of triglycerides to 85.9%, which is influenced by the lowering contact time between the oxygenated compound and the catalyst surface. Patil et al. [50] reported that high space velocity rapidly plugged the reactor with waxy oxygenated compounds, mainly composed of free fatty acids and esters. Moreover, the increase in LHSV might slightly decrease the hydrocarbon yield, indicating the insufficient contact time of reactants and catalysts. The liquid hydrocarbon yield of low LHSV (0.5 h −1 ) was approximately 65.7 wt % and the highest selectivity of bio-jet (92.6%) was obtained because the thermal/catalytic cracking and isomerization reactions simply occurred at the long contact time. The highest liquid hydrocarbon yields (75.9 wt %) were obtained at a moderate LHSV (1.0 h −1 ) with the balance of bio-jet and green diesel fractions of 50.4 and 45.2%, respectively, as shown in Figure 5f. On the other hand, the high LHSV drops the liquid hydrocarbon yield to 66.4 wt % (corresponding to the lower conversion) with the highest green diesel selectivity of 69.3%. However, in terms of the product composition yields, it was revealed that the increase in contact time (at a low LHSV) would generate more gas products obtained by simultaneous cracking reaction [51]. Therefore, a lesser amount of gas products is obtained at a low LHSV and an uncompleted conversion results in the formation of oxygenated compounds in the liquid product.
As shown in Figure 6, the by-products of the deoxygenation of palm oil consisting of water and C 1 -C 3 gas products are significantly influenced by various experimental parameters. These are also suggested by a previous report [48]. In general, free fatty acids, the main oxygenated compounds, could be converted into hydrocarbons via several routes in the deoxygenation process. As displayed in Figure 6a, the elimination of water from palm oil is about 4.0-7.3 wt % of the total liquid products, mainly through hydrodeoxygenation and also a small proportion from decarbonylation. In this study, the effects of DO temperature and LHSV were tested on a CoP/PC-600 catalyst under a H 2 pressure of 50 bar and a H 2 /Oil ratio of 1000 N (cm 3 /cm 3 ). Our results show that increasing the DO reaction temperature and lowering the LHSV reduced the water fraction. The decrease in the water fraction is correlated with the lesser selectivity of the hydrodeoxygenation and decarbonylation pathways under the studied operating conditions, evidenced by the lessened CO amount due to the water-gas-shift reaction [52] which proceeds as a side reaction. In addition, the effects of increasing pyrolysis temperature on catalyst activity were tested on a fixed operating condition: the reaction temperature of 400 • C, an H 2 pressure of 50 bar, and an H 2 /Oil ratio of 1000 N (cm 3 /cm 3 ). Regarding the XRD analysis, increasing the pyrolysis temperature could transform the Co 2 P to CoP. The CoP phase was considered more active than the Co 2 P phase. The CoP/PC catalysts obtained at the higher pyrolysis temperature typically gave lower water content in the liquid products.
Catalysts 2020, 10, x FOR PEER REVIEW 14 of 19 was revealed that the increase in contact time (at a low LHSV) would generate more gas products obtained by simultaneous cracking reaction [51]. Therefore, a lesser amount of gas products is obtained at a low LHSV and an uncompleted conversion results in the formation of oxygenated compounds in the liquid product. As shown in Figure 6, the by-products of the deoxygenation of palm oil consisting of water and C1-C3 gas products are significantly influenced by various experimental parameters. These are also suggested by a previous report [48]. In general, free fatty acids, the main oxygenated compounds, could be converted into hydrocarbons via several routes in the deoxygenation process. As displayed in Figure 6a, the elimination of water from palm oil is about 4.0-7.3 wt % of the total liquid products, mainly through hydrodeoxygenation and also a small proportion from decarbonylation. In this study, the effects of DO temperature and LHSV were tested on a CoP/PC-600 catalyst under a H2 pressure of 50 bar and a H2/Oil ratio of 1000 N (cm 3 /cm 3 ). Our results show that increasing the DO reaction temperature and lowering the LHSV reduced the water fraction. The decrease in the water fraction is correlated with the lesser selectivity of the hydrodeoxygenation and decarbonylation pathways under the studied operating conditions, evidenced by the lessened CO amount due to the water-gas-shift reaction [52] which proceeds as a side reaction. In addition, the effects of increasing pyrolysis temperature on catalyst activity were tested on a fixed operating condition: the reaction temperature of 400 °C, an H2 pressure of 50 bar, and an H2/Oil ratio of 1000 N (cm 3 /cm 3 ). Regarding the XRD analysis, increasing the pyrolysis temperature could transform the Co2P to CoP. The CoP phase was considered more active than the Co2P phase. The CoP/PC catalysts obtained at the higher pyrolysis temperature typically gave lower water content in the liquid products. A major gas fraction was released from the decarbonylation/decarboxylation reactions in the form of CO/CO2, as shown in Figure 6b. Furthermore, the C3H8 gas was produced from the hydrogenolysis of saturated triglycerides. However, gas products could be generated from the A major gas fraction was released from the decarbonylation/decarboxylation reactions in the form of CO/CO 2 , as shown in Figure 6b. Furthermore, the C 3 H 8 gas was produced from the hydrogenolysis of saturated triglycerides. However, gas products could be generated from the cracking reaction under the harsh DO condition resulting in light hydrocarbon formation such as CH 4 , C 2 H 6 , C 3 H 8 , as suggested by Pinto et al. [53]. The slight decrease in C 3 H 8 would be describable to its cracking to CH 4 and C 2 H 6 . Perhaps, the increase in the amount of CH 4 also relates to the decrease in CO and CO 2 via methanation with H 2 [10,53]. It is worth noting that the gas products also contained small amounts of light hydrocarbons, C 4 -C 7 (<2.6%) which were likely formed via the cracking reaction of bio-jet products [48,49]. According to Figure 6b, the findings suggest that the DO temperature, the LHSV and the pyrolysis temperature during the catalyst preparation significantly influenced the composition of the by-products of palm oil deoxygenation. Moreover, the CoP phase, which shows a higher acidity than Co 2 P, can favorably promote catalytic hydrocracking under the high DO temperature condition i.e., 400 • C or higher. In addition, the comparison of the catalytic hydrotreatment with the different catalysts and the different conditions for biofuel production from various fatty acid feedstocks is shown in Table 3. Some non-precious metal catalysts, such as MoO 2 /CNTs, Ni/H-ZSM-22, and Ni-Co/MWCNTs, were successfully used for the production of green diesel biofuels in a batch-type reactor. In addition, the use of NiP catalysts such as NiP/SiO 2 and NiP/AC was demonstrated for the conversion of soybean oil and palmitic acid into green diesel, respectively. The present work shows for the first time the use of a CoP catalyst with the carbon support derived from the biomass waste which is highly cost effective. Moreover, we show that the carbon-supported cobalt phosphide catalyst was effective in producing both the diesel-range and jet-range biofuels. The CoP/AC developed in this work can be considered a promising catalyst for advanced biofuel production.

Conclusions
In this study, microwave-assisted activation is an effective process for porous carbon production due to the reduction in the operating time. Moreover, palm male flower-derived porous carbon (PC) exhibits a great potential as a carbon-based catalyst support. The results show that the cobalt phosphide supported on PC catalysts becomes an effective catalyst in the deoxygenation of vegetable oil or non-edible oil for the production of alternative transportation fuels. The characteristics of CoP/PC catalysts strongly influence catalytic behaviors and the selectivity of hydrocarbon products. Pyrolysis temperature during catalyst preparation significantly controls the formation of the cobalt phosphide phase after the reduction process. At 800-900 • C pyrolysis temperature, mixed phases of cobalt phosphide compounds are generated. The Co 2 P formation firstly occurs and is later converted into CoP while the pyrolysis at 600-700 • C results in a lower yield of the single phase Co 2 P. It is noted that CoP exhibits a higher hydrocracking activity than Co 2 P, as suggested by the obtained product distribution in the deoxygenation of palm oil at 400 • C. The important keys on the deoxygenation activity of cobalt phosphide catalysts are operating conditions such as temperature and LHSV. The CoP/PC catalyst pyrolyzed at 600 • C exhibits a 100% triglyceride conversion at 360 • C and the highest liquid hydrocarbons yield of 77.0% with a selectivity to bio-jet of 26.9% and a selectivity to green diesel of 58.0%. The hydrocarbon yield decreases when the reaction temperature rises to 420 • C with a high fraction of bio-jet fuel. Furthermore, reducing the LHSV exhibits a lower liquid hydrocarbon yield with a high fraction of bio-jet fuel. The highest selectivity to bio-jet was achieved at 92.6% at an LHSV of 0.5 h −1 . According to the findings, the improvements in the yield and selectivity of the desired liquid hydrocarbon products could be achieved by optimizing the operating parameters in deoxygenation and fine-tuning the acidity of cobalt phosphide/PC during the catalyst preparation.