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cracking results of limited precision and accuracy due to the problems related to the fluid dynamics differences between a fixed bed and a fluidized bed, the large contact time (longer than industrial FCC operations, typically about 2 to 10s), low temperature in the preheating section, or low pressure in the catalyst bed. Most of these shortcomings encountered with the traditional MAT unit can be avoided by using a novel Single Receiver Short-Contact-Time Microactivity Test unit (SR-SCT-MAT, Grace GmbH & Co.KG, Frankfurt, Germany) [15]. Details of the experimental setup of the SR-SCT-MAT unit, the testing conditions, and product analyses used in the present work are described elsewhere [13]. In a typical run, 1.75 g of feedstock (either triolein or WCO) was fed into the reactor which contained a desired amount of catalyst diluted with glass beads to maintain a constant-volume reaction independent of the catalyst-to-oil (CTO) mass ratio used. The CTO mass ratio was varied by keeping the weight of feedstock constant (1.75 g) and changing the catalyst weight. The cracking reaction was carried out at ambient pressure, 550 ◦C, CTO mass ratios of 0–1.2 (g·g−1) and a reaction time of 12 s. After the reaction, stripping of the catalyst was done by using a nitrogen purge. The gaseous and liquid products were collected in the single receiver cooled to 18 ◦C via an external cooling system. All catalytic experiments were repeated at least two times to check the reproducibility and mass balances in all runs were between 95% and 100% of the injected feed. The products comprised mainly hydrocarbons along with oxygenated compounds (water, CO, and CO2) and coke. The gaseous hydrocarbon fraction was divided into dry gas (hydrogen, methane, ethane, and ethene) and liquefied petroleum gas (LPG; propane, propene, butenes, and butanes). The liquid hydrocarbons were lumped in terms of boiling ranges: C5+ gasoline (<221 ◦C), light cycle oil (LCO; 221–360 ◦C), and heavy cycle oil (HCO; >360 ◦C). The gaseous products were analyzed according to the ASTM D1945-3 method using a Refinery Gas Analyzer (Agilent 7890A, Santa Clara, CA, USA). The liquid organic products were classified according to the boiling ranges: C5+ gasoline, LCO, and HCO as mentioned above by means of simulated distillation (ASTM D2887) on a Simulated Distillation gas chromatograph (Agilent 7890A, Santa Clara, CA, USA). For several liquid samples, PIONA (Paraffin, i-Paraffin, Olefin, Naphthene, and Aromatic) analyses were performed to determine the composition of gasoline. Water content was measured by Karl Fischer titration (MKS-520, Kem, Kyoto, Japan) and coke amount on the spent catalyst was determined by an elemental analyzer (CS600, Leco Instrumente GmbH, Mönchengladbach, Germany). The yield toward different products (Yi, wt. %) is defined as gram of product i per gram of the feed. The standard MAT conversion is defined as 100% − (YHCO + YLCO). The selectivity to C2–C4 olefins is defined as the fraction of C2–C4 olefins per total fraction of C2–C4 hydrocarbons. 202PDF Image | Zeolite Catalysis
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