Core-Shell Zeolite Y@γ-Al2 O3 Nanorod Composites: Optimized Fluid Catalytic Cracking Catalyst Assembly for Processing Heavy Oil

ChemCatChem ◽  
2017 ◽  
Vol 9 (13) ◽  
pp. 2574-2583 ◽  
Author(s):  
Wenqian Jiao ◽  
Xuezhong Wu ◽  
Gang Li ◽  
Teng Xue ◽  
Yimeng Wang ◽  
...  
Keyword(s):  
Heavy Oil ◽  
Catalytic Cracking ◽  
Zeolite Y ◽  
Fluid Catalytic Cracking ◽  
Core Shell

Facile Synthesis of Mesoporous Zeolite Y with Improved Catalytic Performance for Heavy Oil Fluid Catalytic Cracking

2014 ◽  
Vol 53 (8) ◽  
pp. 3406-3411 ◽  
Author(s):  
Junsu Jin ◽  
Chaoyun Peng ◽  
Jiujiang Wang ◽  
Hongtao Liu ◽  
Xionghou Gao ◽  
...  
Keyword(s):  
Heavy Oil ◽  
Catalytic Cracking ◽  
Zeolite Y ◽  
Catalytic Performance ◽  
Fluid Catalytic Cracking ◽  
Mesoporous Zeolite ◽  
Facile Synthesis

Synthesis of zeolite Y from natural aluminosilicate minerals for fluid catalytic cracking application

2012 ◽  
Vol 14 (12) ◽  
pp. 3255 ◽  
Author(s):  
Tiesen Li ◽  
Haiyan Liu ◽  
Yu Fan ◽  
Pei Yuan ◽  
Gang Shi ◽  
...  
Keyword(s):  
Catalytic Cracking ◽  
Zeolite Y ◽  
Fluid Catalytic Cracking ◽  
Natural Aluminosilicate

Numerical Simulation of Chemical Stripping Process in Resid Fluid Catalytic Cracking Stripper

2014 ◽  
Vol 12 (1) ◽  
pp. 525-537
Author(s):  
Yingjie Liu ◽  
Jihe Yang ◽  
Xingying Lan ◽  
Jinsen Gao
Keyword(s):  
Heavy Oil ◽  
Catalytic Cracking ◽  
Fluid Model ◽  
Flow Behavior ◽  
Fluid Catalytic Cracking ◽  
Bed Height ◽  
Catalyst Temperature ◽  
Two Fluid Model ◽  
Stripping Steam ◽  
Two Fluid

Abstract The chemical stripping process in a commercial scale V-baffled resid fluid catalytic cracking stripper was simulated using computational fluid dynamics method. At the outset, it was assumed that the stripping steam initially desorbs hydrocarbons from the catalysts, and the hydrocarbons are then cracked through thermal and catalytic cracking reactions before entering the disengager. The Eulerian–Eulerian two-fluid model coupled with a modified drag model was applied to simulate the gas–solid flow behavior. A desorption model and five-lump kinetic model for thermal and catalytic cracking were utilized to represent the desorption and cracking processes during stripping. The flow modeling results indicated that three different flow regions exist in the stripper: bubbling flow, intermediate flow and turbulent flow. Increasing gas velocity improves the flow conditions of the gas, but adversely affects the particle flow. The degree of mixing of the gas and solid increases along the flowing direction. The results of reaction modeling showed that about 80% of hydrocarbons desorbed from the catalysts. The amount of desorbed oil increases with bed height leading to an increase of heavy oil in the disengager which induces coking problem. By increasing the catalyst temperature, the partial pressure of heavy oil can be lowered down which helps to decrease the disengager coking.

A 12-lump kinetic model for heavy oil fluid catalytic cracking for cleaning gasoline and enhancing light olefins yield

2020 ◽  
Vol 38 (19) ◽  
pp. 912-921
Author(s):  
Yang Chen ◽  
Wei Wang ◽  
Zhifeng Wang ◽  
Kaijun Hou ◽  
Fusheng Ouyang ◽  
...  
Keyword(s):  
Kinetic Model ◽  
Heavy Oil ◽  
Catalytic Cracking ◽  
Fluid Catalytic Cracking ◽  
Light Olefins

scholarly journals The Production of Zeolite Y Catalyst From Palm Kernel Shell for Fluid Catalytic Cracking Unit

2021 ◽  
Vol 2021 ◽  
pp. 1-8
Author(s):  
Angela Mamudu ◽  
Moses Emetere ◽  
Felix Ishola ◽  
Dorcas Lawal
Keyword(s):  
Catalytic Cracking ◽  
Zeolite Y ◽  
Palm Kernel ◽  
Sem Analysis ◽  
Fluid Catalytic Cracking ◽  
Synthesis Process ◽  
Structural Formation ◽  
Palm Kernel Shell ◽  
Alternative Materials ◽  
Increasing Demand

Exorbitant costs of fluid catalytic cracking unit (FCCU) catalysts coupled with their ever-increasing demand have led researchers to develop alternative materials from indigenous sources. In this study, the zeolite Y component of the FCCU catalyst was synthesized from palm kernel shells. Leaching was carried out with the aid of citric acid to remove impurities. The synthesis process was done using alkaline hydrothermal treatment while varying reagent concentration and reaction time. The resultant products were characterized using XRF, XRD, FTIR, BET, and SEM analysis. The XRD and XRF showed a high silicate content level, while an 85% reduction in iron oxide impurities was observed after leaching. The process carried out at a duration of 9 hours, a temperature of 80°C with a NaOH molarity strength of 2 mol/L, had the highest SiO2 and Si/Al ratio value. A spongy, porous zeolite crystal was formed with the presence of hydroxyls in its sodalite cage. All samples had a combination of types II & I adsorption isotherms, Si/Al ratio of 2–5, and specific surface area within 80–260 m2/g, which indicates the presence of intermediate mesostructured Zeolite Y catalyst. Synthesized zeolite Y showed a more significant gap in its structural formation as the addition of NaOH decreased the grain size by 14.3%. FTIR highlighted the significant functional groups present in the novel compound, which, when compared to previous works, proves its suitability.

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