Materials and Methods bcrec 6597 v10 n1 p61 69

volves esterification and transesterification re- actions and followed by the process of purifica- tion [9, 10]. However, this process brings a complicated separation process and yields only a biodiesel. In order to have more developed process, cracking and hydrocracking process seems to be more enhancing . Instead of employing the foregoing process, hydrocracking is thus far a more promising em- ployed as the process is comprised from two processes, namely catalytic cracking and hydro- genation. These processes are conducted in high pressure and temperature and using bi- functional catalysts as well. To facilitate that function, the catalysts have two functions, as acids and metal catalysts. The former would function in the process of cracking and isomeri- zation, while the latter is used in the process of dehydrogenation and hydrogenation [11]. Hy- drocracking process yields more than one types of fuels, say for example gasoline, kerosene, and gasoil [12]. In hydrocracking process, metal transition catalysts, cobalt Co and molybdenum Mo, has high selectivity. The catalysts can also be used in the process of hydrodesulfurization HDS and hydrodenitrogenation HDN [13, 14]. Both HDS and HDN processes are methods used to reduce nitrogen and sulfur contents found in the common oil fuels [15, 16]. Other process is the process of hydrotreating using CoMo catalysts with the temperature up to 380 oC and pressure up to 40-60 bar, which may successfully achieved 100 conversion of sun flower oil [17]. Before used, metal catalysts, like cobalt Co and molybdenum Mo or NiMo, are subjected to sulfidation using gas mixtures H 2 SH 2 or SH 2 , for activating the metal sites on the sur- face of catalysts [18, 19]. The use of catalysts in sulfidation process may yield non environmen- tally friendly products as a result of sulfur con- tamination [20]. One of the unfavorable im- pacts for the catalysts deactivation is sulfur where the sources are derived from gases, H 2 S [21]. Therefore, it is necessary to develop a catalyst to obtain products that are environ- mentally friendly. This research is aimed to convert Calophyllum inophyllum kernel oil to environmentally friendly oil fuels through hydrocracking process using CoMoCoMo - Al 2 O 3 , CoMoSiO 2 , and CoMo -Al 2 O 3 -SiO 2 cata- lysts. The 10 wt. CoMo promotors are em- ployed in the impregnation of the support dur- ing catayst preparation without sulfidation process.

2. Materials and Methods

Prior to the research, catalysts preparations, catalysts characterizations and catalysts testing have been carried out in the pressurised reactors. Then, CoMo catalysts was produced with the 10 wt. loading of the support material. The catalysts are made by means of impregnation methods, whereas the raw materials for the catalysts CoNo 3 2 .6H 2 O and NH 4 6 Mo 7 O 2 .4H 2 O. All chemicals were provided with p.a 99 Merck grade. Solution of NH 4 6 Mo 7 O 24 .4H 2 O and CoNO 3 2 .6H 2 O is impregnated in the support of γ-Al 2 O 3 p.a. Merck with 10 wt. loading, and into other supports such as SiO 2 p.a,, Sigma Aldrich and support of γ-Al 2 O 3 -S i O 2 . The mixture of the catalysts would be dried under the temperature 110 C within 8 hours, then calcined under the temperature of 500 C within 5 hours. The characterization of catalysts was con- ducted using X-ray diffraction XRD to identify the compositions of the catalysts and to recog- nize the forms of crystal catalysts. The catalyst samples were placed on the sampling con- tainer, using a Philips PN-1830 with CuK α ra- diation 1.5406 Å at 40 kV and 30 mA. Samples were scanned in the range 2 θ of 5-90o with a step size 0.017 and step time 10.15 s. The following Brunauer Emmett Teller BET analysis method was employed for identifying the surface of the catalysts volume. Sample was added to the sample cell with 3 hours of outgas time and 573 K of outgas tem- perature. Nitrogen has been used in this analy- sis and bath temperature is 77.3 K. Pressure tolerance for adsdes is 0.1000.100 with equil time = 180180sec adsdes, equil timeout = 360360 sec adsdes where time analysis is ap- proximately 67.4 mins. Reactions were carried out with Parr USA pressure reactor, while nitrogen and hydrogen gases were used in the reaction process. This was procceded under the pressure of 30 bar and catalyst weight percent up to 5 from the volume of the oil, while the process is done under the temperature of 350 C. The reaction product would be analyzed by GC-MS Gas Cromotography-Mass Spectromety. It can ana- lyze both qualitatively and quantitatively as well; whereas, the components comprised would be able to be detected by means of the instrument with capillary column model num- ber of Agilent 19091 S-493, HP-5MS 5 Phenyl Methyl Siloxane, nominal length: 30.0 m, nomi- nal diameter: 250 um, nominal film thickness: 0,25 um, and nominal initial pressure of 10,5 psi. Bulletin of Chemical Reaction Engineering Catalysis, 10 1, 2015, 62 Copyright © 2015, BCREC, ISSN 1978-2993 3. Results and Discussion 3.1. Characterization of Catalyst