Production of Biodiesel from Waste Cooking Oil via Deoxygenation Using Ni-Mo/Ac Catalyst

Waste cooking oil (WCO) from palm oil is one of the most prospective biodiesel feedstock when compared to other oil seeds. Thus, WCO has great potential as a green source of diesel fuel for engines in motor vehicles and machinery. This project aimed to study the potential of three randomly selected types of WCO, namely; sample A (used 1× once to fry an egg), sample B (used 3– 5× to fry salted fish), and sample C (used repeatedly to fry banana fritter) for the production of green diesel fuel over Ni-Mo/AC (nickel and molybdenum oxides incorporated with activated carbon) catalyst through the deoxygenation (DO) process. The prepared catalyst was characterized through X-ray diffraction (XRD), thermogravimetric analysis (TGA), and field emission scanning electron microscopy (FESEM). The DO process was performed at 350 ◦C to remove oxygen from the WCO samples. The liquid products were analysed by gas chromatography-mass spectrometer (GC-MS) and gas chromatography-flame ionization detector (GC-FID), to measure the yields of straight-chain hydrocarbons and fractions in the range C8-C20. Results showed that the highest n-(C8-C20) hydrocarbon fractions were produced in the order of sample B (89.93%) > C (88.84%) > A (82.81%).


Introduction
Current strategies are geared towards a green form of diesel consisting of freeoxygenated hydrocarbon compounds for future use as a clean-burning fuel. Such fuels are characterised by low sulphur and aromatic content, high cetane content, lubricity and regenerability, which can guarantee~70-90% reduction in GHG emissions (Asikin-Mijan et al., 2016a). Since the substance is not only fungible with crude oil-derived fuels, it also has properties similar to alternative biofuels, such as biodiesel or methyl ester fatty acid (FAME). FAME is an extremely oxygenated compound with various drawbacks, such as high viscosity, low cloud and pour point properties, along with low heating value and oxidation stability [1][2][3]. Green diesel is generally synthesized by the deoxygenation (DO) of triglycerides and fatty acid derivatives by decarboxylation or decarbonylation (deCOx), along with the formation of CO 2 and CO + H 2 O as by-products [4][5][6]. Green diesel may also be synthesized by the process of hydrodeoxygenation (HDO), during which oxygenated compounds are extracted in the presence of H 2 gas, resulting in the formation of water (H 2 O) as a by-product [7]. However, the process requires a high amount of expensive H 2 gas and high reaction pressure [8]. In contrast, the DO procedure is considered to be more economical, successful and suitable for industrial practices. The process results in high-quality green diesel, with similar fuel properties as standard crude oil-derived diesel [9].
Recently, the DO process was investigated using various catalysts, such as Pd or Ptbased transition metal oxides consisting of Ni, Co, Zn, Cu, Ga and Ru [2,[10][11][12][13]. The most typical transition metal oxides used for DO are Ni, Co, W [14], and Mo, Cu, Fe, and Zn [15], with Ni showing the highest DO behaviour among the metals. Croker and co-workers observed that 20 wt. per cent Ni/C yielded higher glycerol tristearate compared to 5 wt. percent Pd and 1 wt. percent Pt-promoted catalyst [16]. The results are important since Ni is~1750 and~3450 times cheaper than Pd and Pt, respectively. A few studies have shown that Ni-promoted catalysts exhibited high DO activity through the deCOx pathway during the DO phase of triglyceride oil and model compounds (palmitic acid methyl group stearate) for the production of diesel-range hydrocarbons [17]. The efficacy of the DO reaction mainly includes noble-based catalysts on either Pd or Pt, which result in high deCOx activity and high hydrocarbon fraction yields. However, the high cost of such catalysts restricts industrial applications. Another downside for large-scale applications is the complex method of preparing such catalysts. The acid-based catalysts are also vulnerable to deactivation of the catalytic active sites due to coke formation [18]. The modification of such catalysts is therefore an essential requirement to enhance stability. Recent studies have shown that lower coke formation is accomplished by the use of basic metal-catalyst compared to acid metal-catalysts during DO reactions [1,4]. However, despite the existence of high cracking activity, the fundamental catalyst jointly results in low deCOx activity [4,19]. The acidic-basic properties of disaggregated CaO-La2O3/AC nano-sized carbon-supported catalysts have been effective in the development of biodiesel [19]. The catalytic properties of mixed metal oxides are mostly reliant on the microstructure of the nanosized catalyst. During the nanoparticle stage, the surface-to-volume ratio increases significantly, meaning that the surface atoms absorb an increasing fraction of the entire particulate volume with high defective structures. As a consequence, the atoms show interesting new or enhanced chemical properties. Nanocrystalline NiMoO4, with a particle size of about 20 nm, has been synthesized [20,21], but no catalytic information has been published in the literature. Furthermore, the development and comprehensive examination of catalysts by researchers for industrial biodiesel application are yet to be achieved. The high cost of raw materials is a major obstacle for the commercialization of biodiesel production [22]. Hence, the use of cheap and renewable feedstocks is crucial to the production of biodiesel. Waste cooking oil (WCO) is an abundant by-product of daily food preparation [23]. The use of palm oil-based WCO as feedstock for biodiesel could jointly solve the problems of waste disposal and dwindling environmental standards in Malaysia.
In the current research, the selective catalytic synthesis of stable mesoporous compounds was investigated through DO, using an acidic bimetallic Ni-Mo/AC OXIDE catalyst. The synthesized catalyst was characterized by XRD, TGA, field emission scanning electron microscopy (FESEM) and FTIR. The products obtained were subsequently characterized by GC-MS and GC-FID to investigate the effect of the various palm oil-based WCOs. The selected catalyst for the great performance breakdown of hydrocarbon chains was synthesized at the recommended ratio of 10%:10%:80%, due to higher AC usage compared to the acid and basic metal. The paper provides useful information on the evaluation of WCO from various food types, preparation and frequency of use through DO using a prepared catalyst.

Materials
The AC was purchased from Sigma-Aldrich with the appearance of the 100-400 mesh as support. The nickel (II) nitrate hexahydrate (Ni (NO 3 ) 2 ·6H 2 O) with molecular weight 290.79 g/mol and ammonium molybdate ((NH 4 ) 6 Mo 7 ·4H 2 O) with molecular weight 1235.86 g/mol were purchased from HmbG Chemicals. The liquid product used was phosphoric acid (lab-grade standard in 85%) from the Reagent brand. The experimental Processes 2021, 9, 750 3 of 12 palm oil-based WCO feedstock was obtained from a selected café and stall located at Serdang in Selangor, Malaysia. The three treatments were arranged based on the number of uses of the WCO, as shown in Table 1. The oils used for the reactions were applied directly without any treatment or purification.

Catalyst Synthesis
Catalyst preparation for this research was prepared by following the method of Wan Khalit et al. [24] with minor modification. The reflux apparatus shown in Figure 1 was set up in a fume chamber equipped with water flow for the inlet and an outlet for the excess distilled water discharged. The heating and stirrer machines were connected with a retort stand to hold the reflux condenser upward, together with the temperature detector rod placed inside the stainless-steel basin placed on the heater. The 250 mL round bottom flask was immersed in paraffin liquid to avoid rapid evaporation due to the heating effect. Next, precisely 5 g of the AC was weighed using a digital balance, while 75 mL of phosphoric acid was measured using a measuring cylinder. Both materials were transferred to a 250 mL round bottom flask and a magnetic stirrer was placed in the flask before connecting a reflux condenser to the lower part. The hot plate was then set to 150 • C and 500 rpm for 12 h. The purification of the heated substances using warm distilled water was done after adjusting the solution to pH 7. Next, the powder was dried in an oven at 100 • C for 2 h. The AC was then impregnated to synthesize the NiO: MoO: AC catalyst based on the w/w ratio 10%:10%:80%, by constant stirring for six (6) hours. The impregnated metals on the catalyst support were subsequently desiccated at 100 • C for 24 h. Afterwards, AC doped with the metals was calcined under N 2 gas flow at 700 • C for 4 h. selected café and stall located at Serdang in Selangor, Malaysia. The three treatments were arranged based on the number of uses of the WCO, as shown in Table 1. The oils used for the reactions were applied directly without any treatment or purification.

Catalyst Synthesis
Catalyst preparation for this research was prepared by following the method of Wan Khalit et al. [24] with minor modification. The reflux apparatus shown in Figure 1 was set up in a fume chamber equipped with water flow for the inlet and an outlet for the excess distilled water discharged. The heating and stirrer machines were connected with a retort stand to hold the reflux condenser upward, together with the temperature detector rod placed inside the stainless-steel basin placed on the heater. The 250 mL round bottom flask was immersed in paraffin liquid to avoid rapid evaporation due to the heating effect. Next, precisely 5 g of the AC was weighed using a digital balance, while 75 mL of phosphoric acid was measured using a measuring cylinder. Both materials were transferred to a 250 mL round bottom flask and a magnetic stirrer was placed in the flask before connecting a reflux condenser to the lower part. The hot plate was then set to 150 °C and 500 rpm for 12 h. The purification of the heated substances using warm distilled water was done after adjusting the solution to pH 7. Next, the powder was dried in an oven at 100 °C for 2 h. The AC was then impregnated to synthesize the NiO: MoO: AC catalyst based on the w/w ratio 10%:10%:80%, by constant stirring for six (6) hours. The impregnated metals on the catalyst support were subsequently desiccated at 100 °C for 24 h. Afterwards, AC doped with the metals was calcined under N2 gas flow at 700 °C for 4 h.

X-ray Diffraction (XRD)
In this study, XRD was utilized to determine the rate of dispersion and the chemical structure of the reformed AC catalyst, before and after the reaction. The XRD inquiry was carried out on the Shimadzu diffractometer (Model: XRD-6000, Shimadzu Corporation, Kyoto, Japan).  In this study, XRD was utilized to determine the rate of dispersion and the chemical structure of the reformed AC catalyst, before and after the reaction. The XRD inquiry was carried out on the Shimadzu diffractometer (Model: XRD-6000, Shimadzu Corporation, Kyoto, Japan). TGA analysis was used to test the stability of the synthesized catalysts. It was also used to examine the coke deposition on the spent catalysts. Each spent catalyst was heated at 30 • C/min heating rate under the oxygen gas (O 2 ) flow rate of 40 mL/min, from 25 • C to 900 • C.

Field Emission Scanning Electron Microscopy (FESEM)
The morphological characteristics of the catalyst were investigated by field emission scanning electron microscopy (Rayny EDX-720; Shimadzu, Kyoto, Japan). The FESEM images were observed through the LEO 1455 VP electron microscope.

Fourier Transform Infrared (FTIR) Spectroscopy
The FTIR analysis was conducted to analyse the chemical functional groups of the triolein (feedstock) and deoxygenated materials. During the deoxygenation cycle, the absorption bands corresponding to the ester, alcohol, carbonyl, glycerides, and carboxylic groups were recorded. Chemical characterization analysis was done following the method described by Muhamad et al. (2013) with minor modification. The Perkin-Elmer Spectrum One FT-IR Spectrometer was used to examine the chemical composition and chemical bonds present in the prepared films. Before the FTIR analysis, the prepared films were dried overnight at 40 • C in an oven. Each dried film was then ground into a fine powder. Next, 4 mg of the ground films were mixed with potassium bromide (KBr) powder in a ratio of 1:10. The sample pellets were formed under a pressure of 500 kg/cm 2 using a hydraulic press. The prepared samples were then analysed using the Perkin-Elmer Spectrum One FT-IR Spectrometer at a resolution of 4 cm −1 in the range of 4000-400 cm −1 averaged over 16 scans.

Catalytic Deoxygenation of Waste Cooking Oil (WCO)
The DO of WCO was performed in a 250 mL mechanically stirred, semi-batch reactor, as shown in Figure 2. For each run, 10 g of WCO and 5 wt.% of the synthesized catalyst were placed in the reactor, as reported by Wan Khalit et al. [24], who stated that the reactor must be purged with N 2 gas to extract the O 2 from the air created during the heating process, by setting the temperature to 350 • C and run-time of 3 h. The condensed liquid product was subsequently deoxygenated and stored in the collection vessel placed after the chiller. After the reaction was completed, the reactor was cooled to an ambient temperature, while the contents of the vessel collector and round bottom flask were weighed [10]. Lastly, the products were analysed by gas chromatography-flame ionization detection (GC-FID). The liquid-based products were examined by GC-FID. Before each test, the sample was dissolved in the GC standard n-hexane before 1 μL of the sample aliquot was inserted in the GC column. Simultaneously, the temperature of the injection was fixed at 250 °C, whereas nitrogen was  The liquid-based products were examined by GC-FID. Before each test, the sample was dissolved in the GC standard n-hexane before 1 µL of the sample aliquot was inserted in the GC column. Simultaneously, the temperature of the injection was fixed at 250 • C, whereas nitrogen was selected as the transport gas. The oven of the GC-FID was set to 6 min at 40 • C, before ramping to 300 • C at a rate of 7 • C/min for 30 min. The GC-FID analysis was performed to define the hydrocarbon components from the marketed saturated versions from C 8 -C 20 and the commercially unsaturated nonene [5]. The entire area under the chromatographic peak of each hydrocarbon fraction (% relative abundance) also termed the total saturated and unsaturated straight-chain hydrocarbons (C 8 -C 20 ) (n-alkane + n-alkene) fractions, were determined by Equation (1): The term X denotes the saturated and unsaturated straight-chain hydrocarbon fractions (% relative abundance), A o was determined by the area of the alkene (C 8 -C 20 ), A i was determined by the area of the alkane (C 8 -C 20 ), and A z was determined by the area of the total product.

Gas Chromatography-Mass Spectrometer (GC-MS)
GC-MS was employed to evaluate the liquid deoxygenated substances with the saturated and unsaturated hydrocarbon (C 8 -C 20 ) fractions defined under experimental conditions. Asomaning [25] demonstrated that the identification of the unsaturated hydrocarbons can be performed by interpreting the GC-MS based data and comparing it to the National Institute of Standards and Testing Library and Literature data. Asikin-Mijan [26] reported that the chemical composition of the feedstocks and liquid products of DO were characterised qualitatively by the GC-MS (Shimadzu QP50550A model) equipped with a non-polar DB-5HT column (30 m × 0.32 mm × 0.25 µm) through the less split inlet. The completed examination is significant since the resulting liquid product was then assumed to have functions that are not limited to hydrocarbons. The samples were diluted to 100 mg/L with GC grade n-hexane (purity > 98%), while the compounds were identified based on a probable match equal to or above 95%. The selectivity of the deoxygenated products was determined based on Equation (2): The term X denotes the selectivity (%), A x was determined by the peak area of the desired organic compound, and A y was determined by the peak area of the total organic compounds.

WCO Evaluation as Biodiesel Feedstock
Van et al. highlighted the number of carboxylic acid groups such as fatty acids in a mixture of chemical compounds [27]. Typically, a fixed amount of a sample is diluted in an organic solvent (usually isopropanol) and titrated with KOH (potassium hydroxide), using phenolphthalein as an essential colour indicator. Furthermore, the acid number measures the acidity of any substance, such as biodiesel. The volume of KOH (in mg) required to neutralize the acidic constituents is 1 g of the sample. In this study, the three (3) WCO samples, and the acid values of their liquid oil products are shown in Table 2. The acidic and FFA values are expressed in Equations (3) and (4)  However, the WCO feedstock was further subjected to chemical property characterization using GC programs adapted from Wan Khalit et al. [24], due to similarities in the source and locality obtained, as tabulated in Table 3.  Figure 3 shows the XRD pattern of the analysed Ni-Mo/AC catalyst. There is an adjacent graph to the XRD peak distance, which is ascribed to the high crystallinity and clear elements of the mesoporous Ni-Mo/AC structure. Based on the graph, the intense peaks of MoO 2 appeared at 2θ = 26.033 • , 37.121 • , 49.498 • , and 53.888 • (JCPDS card no: 00-002-0422). However, the NiOOH peaks were located at 2θ = 37.281 • ) (JCPDS card no: 00-006-0141). Furthermore, the visible peaks of Ni were found at 2θ = 44.349 • , 51.674 • (JCPDS card no: 00-001-1272), whereas the NiMoO 4 peaks were observed at 2θ = 77.405 • , 44.142 • , 52.488 • (JCPDS card no: 0120348). The results are in agreement with Wu et al. [28], who reported that the successful impregnation of NiO and MoO greatly reduced the amorphous structure of AC. Hence, the overlap of both species in AC ultimately promotes greater dispersal in the AC-based catalyst.

Fourier Transform Infrared (FTIR) Spectroscopy
Based on this study, the chemical functional groups of the triglyceride and deoxygenated products were studied. The spectra for all the samples in Figure 4 showed an absorption band detected at 1743 cm −1 (C=O), that is ascribed to the ester groups in glycerides, whereas the band at 1140 cm −1 (C=O) denotes the alcohol group usually attributed to WCO. The intense peak of the carbonyl (C=O) group and WCO are visible at 1740 cm −1 . Hence, its presence at 1140 cm −1 indicates the progress of the DO reaction. The breakage of triglycerides into the fatty acids of the deoxygenated liquid can be observed through the shift in the C=O (ester) absorption band from 1740 cm −1 to 1700 cm −1 , which is ascribed to Processes 2021, 9, 750 7 of 12 the intermediate carboxylic acid produced. The reaction phase for DO is also evident in the loss of the C=O absorption band near 1150 cm −1 . According to Satyarti and Srinivas [29], the typical C-H stretching peaks at 2921 cm −1 are not affected by hydrocarbon formation.
to the XRD peak distance, which is ascribed to the high crystallinity and clear elements of the mesoporous Ni-Mo/AC structure. Based on the graph, the intense peaks of MoO2 appeared at 2θ = 26.033°, 37.121°, 49.498°, and 53.888° (JCPDS card no: 00-002-0422). However, the NiOOH peaks were located at 2θ = 37.281°) (JCPDS card no: 00-006-0141). Furthermore, the visible peaks of Ni were found at 2θ = 44.349°, 51.674° (JCPDS card no: 00-001-1272), whereas the NiMoO4 peaks were observed at 2θ = 77.405°, 44.142°, 52.488° (JCPDS card no: 0120348). The results are in agreement with Wu et al. [28], who reported that the successful impregnation of NiO and MoO greatly reduced the amorphous structure of AC. Hence, the overlap of both species in AC ultimately promotes greater dispersal in the AC-based catalyst.

Fourier Transform Infrared (FTIR) Spectroscopy
Based on this study, the chemical functional groups of the triglyceride and deoxygenated products were studied. The spectra for all the samples in Figure 4 showed an absorption band detected at 1743 cm −1 (C=O), that is ascribed to the ester groups in glycerides, whereas the band at 1140 cm −1 (C=O) denotes the alcohol group usually attributed to WCO. The intense peak of the carbonyl (C=O) group and WCO are visible at 1740 cm −1 . Hence, its presence at 1140 cm −1 indicates the progress of the DO reaction. The breakage of triglycerides into the fatty acids of the deoxygenated liquid can be observed through the shift in the C=O (ester) absorption band from 1740 cm −1 to 1700 cm −1 , which is ascribed to the intermediate carboxylic acid produced. The reaction phase for DO is also evident in the loss of the C=O absorption band near 1150 cm −1 . According to Satyarti and Srinivas [29], the typical C-H stretching peaks at 2921 cm −1 are not affected by hydrocarbon formation.

Thermogravimetric Analysis (TGA)
The degree of coke formation was investigated by TGA. In this study, the degree of coke formed on the Ni-Mo/AC catalyst is shown in Figure 5. Based on Figure 5a-(TGA N2), the calcined catalyst is defined by a shorter period or phase of coke formation and temperature range compared to the catalyst before calcination. The formation of coke on the external surface of the catalyst during the reaction degraded the DO activity. Hence, the results revealed that the bimetallic Ni-Mo/AC catalyst promotes superior resistance towards coke formation. The findings are in agreement with Wan Khalit et al. [24], who reported that the XRD and TGA confirm that the bimetallic Ni-Mo/AC has potential catalyst stability and prospects for further application at pilot-scale, due to its long-life and reuse. Figure 5b-(TGA O2) shows that the spent catalyst sample A exhibits a decomposition peak in the range 245 °C to 347 °C. For sample B, the decomposition peak was from 252 °C to 319 °C, whereas sample C was from 271 °C to 324 °C, which is linked to the combustion of the AC bulk nanorod. In general, all the spent catalysts showed rapid weight loss due to the decomposition temperature at 700 °C, which indicates the oxidation of coke in air.

Thermogravimetric Analysis (TGA)
The degree of coke formation was investigated by TGA. In this study, the degree of coke formed on the Ni-Mo/AC catalyst is shown in Figure 5. Based on Figure 5a-(TGA N 2 ), the calcined catalyst is defined by a shorter period or phase of coke formation and temperature range compared to the catalyst before calcination. The formation of coke on the external surface of the catalyst during the reaction degraded the DO activity. Hence, the results revealed that the bimetallic Ni-Mo/AC catalyst promotes superior resistance towards coke formation. The findings are in agreement with Wan Khalit et al. [24], who reported that the XRD and TGA confirm that the bimetallic Ni-Mo/AC has potential catalyst stability and prospects for further application at pilot-scale, due to its long-life and reuse. Figure 5b-(TGA O 2 ) shows that the spent catalyst sample A exhibits a decomposition peak in the range 245 • C to 347 • C. For sample B, the decomposition peak was from 252 • C to 319 • C, whereas sample C was from 271 • C to 324 • C, which is linked to the combustion of the AC bulk nanorod. In general, all the spent catalysts showed rapid weight loss due to the decomposition temperature at 700 • C, which indicates the oxidation of coke in air.
on the Ni-Mo/AC catalyst is shown in Figure 5. Based on Figure 5a-(TGA N2), the calcined catalyst is defined by a shorter period or phase of coke formation and temperature range compared to the catalyst before calcination. The formation of coke on the external surface of the catalyst during the reaction degraded the DO activity. Hence, the results revealed that the bimetallic Ni-Mo/AC catalyst promotes superior resistance towards coke formation. The findings are in agreement with Wan Khalit et al. [24], who reported that the XRD and TGA confirm that the bimetallic Ni-Mo/AC has potential catalyst stability and prospects for further application at pilot-scale, due to its long-life and reuse. Figure 5b-(TGA O2) shows that the spent catalyst sample A exhibits a decomposition peak in the range 245 °C to 347 °C. For sample B, the decomposition peak was from 252 °C to 319 °C, whereas sample C was from 271 °C to 324 °C, which is linked to the combustion of the AC bulk nanorod. In general, all the spent catalysts showed rapid weight loss due to the decomposition temperature at 700 °C, which indicates the oxidation of coke in air.   Figure 6a illustrates the FESEM images of the fresh AC and Ni-Mo/AC catalyst at 700 • C activation temperature. The images represent a significant difference between the fresh AC and Ni-Mo/AC catalyst, which are characterized by smooth surfaces and regularshaped spheres. However, the morphology of the catalyst changed when the fresh AC was doped with the bimetal oxide. Hence, Figure 6b shows rough, aggregate, and irregular spherical shapes with particle size > 1 µm. The changes are due to the occurrence of hydrogen bond fractures in the crystalline region triggered by the acid treatment of the activated charcoal surfaces, which assist in the formation of nanocrystalline fibrous-like structures or patterns [8]. The addition of the bimetallic phase of Ni-Mo/AC causes the enlargement of particle size, as expected from the combination of interposed metals (NiO + MoO) throughout the synthesis process. Thus, Table 4 below shows the elemental composition of the synthesized catalyst during the experimental process, as determined by EDX.  Figure 6a illustrates the FESEM images of the fresh AC and Ni-Mo/AC catalyst at 700 °C activation temperature. The images represent a significant difference between the fresh AC and Ni-Mo/AC catalyst, which are characterized by smooth surfaces and regular-shaped spheres. However, the morphology of the catalyst changed when the fresh AC was doped with the bimetal oxide. Hence, Figure 6b shows rough, aggregate, and irregular spherical shapes with particle size > 1 μm. The changes are due to the occurrence of hydrogen bond fractures in the crystalline region triggered by the acid treatment of the activated charcoal surfaces, which assist in the formation of nanocrystalline fibrous-like structures or patterns [8]. The addition of the bimetallic phase of Ni-Mo/AC causes the enlargement of particle size, as expected from the combination of interposed metals (NiO + MoO) throughout the synthesis process. Thus, Table 4 below shows the elemental composition of the synthesized catalyst during the experimental process, as determined by EDX.    3.6. Biodiesel Properties 3.6.1. Gas Chromatography-Flame Ionization Detection

Field Emission Scanning Electron Microscopy (FESEM)
The DO reactivity of WCO over Ni/Mo-AC catalyst is shown in Figure 7a,b. Based on Figure 7a, sample C shows the highest yield of 31%, followed by sample A (17%) and sample B (12%). The significant values imply that the catalytic DO reaction was successful. The dark WCO showed the highest selectivity of DO due to the energetic effect of bimetallic Ni/Mo on the AC nanorod, which enhanced the properties of the acid-base sites. Figure 7b shows the comprehensive overview of the distribution of hydrocarbon portions from n(C 8 -C 20 ) for the liquid DO products. The WCO consisting of~45.68% C 16 and~52.34% C 18 for fatty acids is typically converted to hydrocarbon portions comprising nC 15 and nC 17 by deCox pathways that are consistent with Bezergianni et al. [30].

Gas Chromatography-Mass Spectrometry (GC-MS)
The comprehensive distribution of products for all three WCO conditions using the Ni-Mo/AC catalyst at 350 °C is shown in Figure 8. According to the GC-MS results, the arrangement of the highest hydrocarbon fraction produced in the n(C8-C20) range started from sample B (89.93%) > sample C (88.84%) > sample A (82.81%). Lam et al. [31] reported that GC-MS analysis allows for easy detection of isomers based on the mass of the fragmented compound as suggested by the National Institute of Standards. Furthermore, the results of the different range of n(C8-C20) hydrocarbons obtained from both GC-MS and GC-FID confirm that the straight-chained (saturated and unsaturated) hydrocarbons were mostly found in the liquid DO product. This result is in agreement with the finding in Section 3.3. However, a small amount of bulky C21-C24 hydrocarbons and oxygenated intermediates (such as aldehydes, ketones, alcohols, and carboxylic acid) were also detected. As reported by Silva [32], WCOs undergo various procedures to achieve a perfect breakdown of triglycerides into mono-chains (free-fatty acid). Other products include oxygenated DO intermediates, aldol condensation, ketonization and hydrocarbon deoxygenated cyclisation. The comprehensive distribution of products for all three WCO conditions using the Ni-Mo/AC catalyst at 350 • C is shown in Figure 8. According to the GC-MS results, the arrangement of the highest hydrocarbon fraction produced in the n(C 8 -C 20 ) range started from sample B (89.93%) > sample C (88.84%) > sample A (82.81%). Lam et al. [31] reported that GC-MS analysis allows for easy detection of isomers based on the mass of the fragmented compound as suggested by the National Institute of Standards. Furthermore, the results of the different range of n(C 8 -C 20 ) hydrocarbons obtained from both GC-MS and GC-FID confirm that the straight-chained (saturated and unsaturated) hydrocarbons were mostly found in the liquid DO product. This result is in agreement with the finding in Section 3.3. However, a small amount of bulky C 21 -C 24 hydrocarbons and oxygenated intermediates (such as aldehydes, ketones, alcohols, and carboxylic acid) were also detected. As reported by Silva [32], WCOs undergo various procedures to achieve a perfect breakdown of triglycerides into mono-chains (free-fatty acid). Other products include oxygenated DO intermediates, aldol condensation, ketonization and hydrocarbon deoxygenated cyclisation. unsaturated) hydrocarbons were mostly found in the liquid DO product. This result is in agreement with the finding in Section 3.3. However, a small amount of bulky C21-C24 hydrocarbons and oxygenated intermediates (such as aldehydes, ketones, alcohols, and carboxylic acid) were also detected. As reported by Silva [32], WCOs undergo various procedures to achieve a perfect breakdown of triglycerides into mono-chains (free-fatty acid). Other products include oxygenated DO intermediates, aldol condensation, ketonization and hydrocarbon deoxygenated cyclisation.

Conclusions
The remarkable activity of Ni-Mo/AC was due to the energetic effect between the active acidic promoter (Ni-Mo) and the extensive surface area of the AC support. Hence, an increase in the penetration of the large WCO triglycerides for the DO reaction was observed in this study. The yield of biodiesel obtained is influenced by the frequency of usage and type of food fried with the palm oil,

Conclusions
The remarkable activity of Ni-Mo/AC was due to the energetic effect between the active acidic promoter (Ni-Mo) and the extensive surface area of the AC support. Hence, an increase in the penetration of the large WCO triglycerides for the DO reaction was observed in this study. The yield of biodiesel obtained is influenced by the frequency of usage and type of food fried with the palm oil, which is due to chemical compounds released during the high cooking temperatures. Both samples A and B exhibited high hydrocarbon fraction yields of 89.93% and 88.84%, respectively, at optimum conditions within C 14 -C 18 . In future studies, the authors propose to further investigate the current bimetallic acid catalyst, using different processes such as the transesterification of WCO to explore the potential of obtaining higher biodiesel yield and its cost-effectiveness in terms of catalyst stability and reusability. Other studies will synthesise different bimetallic catalysts with AC from different waste sources by altering the percentage ratios. The catalysts will then be examined for reactivity performance using WCO or other fatty acid sources, such as animal fat from poultry or plants that contains extractable triglyceride.