Intensification of catalytic cracking on promoted bead catalyst

1993 ◽  
Vol 29 (2) ◽  
pp. 58-62
Author(s):  
V. R. Zinov'ev ◽  
M. I. Levinbuk ◽  
Kh. K. Shapieva
Keyword(s):  
Catalytic Cracking ◽  
Bead Catalyst

Catalytic cracking of low-sulfur vacuum distillate in commercial unit with zeolitic bead catalyst Tseokar-2

1974 ◽  
Vol 10 (4) ◽  
pp. 269-273
Author(s):  
A. Z. Dorogochinskii ◽  
V. R. Zinov'ev ◽  
V. V. Serov ◽  
E. M. Breshchenko ◽  
L. V. Bryzgalina ◽  
...  
Keyword(s):  
Catalytic Cracking ◽  
Vacuum Distillate ◽  
Commercial Unit ◽  
Bead Catalyst ◽  
Low Sulfur ◽  
Zeolitic Bead

Granular filters for cleanup of gases from regeneration of bead catalyst in catalytic cracking units

1979 ◽  
Vol 15 (8) ◽  
pp. 572-573
Author(s):  
N. A. Sidorenko ◽  
V. A. Bagdasarova ◽  
V. Ya. Bashkardin
Keyword(s):  
Catalytic Cracking ◽  
Bead Catalyst ◽  
Granular Filters

Fluidized Catalytic Cracking Catalyst Microstructure as Determined by A Scanning Ion Microprobe

1990 ◽  
Vol 48 (2) ◽  
pp. 302-303
Author(s):  
J.K. Lampert ◽  
G.S. Koermer ◽  
J.M. Macaoy ◽  
J.M. Chabala ◽  
R. Levi-Setti
Keyword(s):  
Catalytic Cracking ◽  
Secondary Ion Mass Spectrometry ◽  
Fuel Oil ◽  
Ion Microprobe ◽  
Fluidized Catalytic Cracking ◽  
Ion Probe ◽  
Silica Alumina ◽  
Resolution Imaging ◽  
The University ◽  
High Spatial Resolution Imaging

We have used high spatial resolution imaging secondary ion mass spectrometry (SIMS) to differentiate mineralogical phases and to investigate chemical segregations in fluidized catalytic cracking (FCC) catalyst particles. The oil industry relies on heterogeneous catalysis using these catalysts to convert heavy hydrocarbon fractions into high quality gasoline and fuel oil components. Catalyst performance is strongly influenced by catalyst microstructure and composition, with different chemical reactions occurring at specific types of sites within the particle. The zeolitic portions of the particle, where the majority of the oil conversion occurs, can be clearly distinguished from the surrounding silica-alumina matrix in analytical SIMS images.The University of Chicago scanning ion microprobe (SIM) employed in this study has been described previously. For these analyses, the instrument was operated with a 40 keV, 10 pA Ga+ primary ion probe focused to a 30 nm FWHM spot. Elemental SIMS maps were obtained from 10×10 μm2 areas in times not exceeding 524s.

An analytical microscopic study of metals in fluidized catalytic cracking catalyst

1986 ◽  
Vol 44 ◽  
pp. 854-855
Author(s):  
Clifford S. Rainey
Keyword(s):  
Electron Microscopy ◽  
Spatial Distribution ◽  
Catalytic Cracking ◽  
Catalyst Deactivation ◽  
Coke Formation ◽  
Acid Sites ◽  
Y Zeolite ◽  
Fcc Catalyst ◽  
Fluidized Catalytic Cracking ◽  
High Regeneration

The spatial distribution of V and Ni deposited within fluidized catalytic cracking (FCC) catalyst is studied because these metals contribute to catalyst deactivation. Y zeolite in FCC microspheres are high SiO2 aluminosilicates with molecular-sized channels that contain a mixture of lanthanoids. They must withstand high regeneration temperatures and retain acid sites needed for cracking of hydrocarbons, a process essential for efficient gasoline production. Zeolite in combination with V to form vanadates, or less diffusion in the channels due to coke formation, may deactivate catalyst. Other factors such as metal "skins", microsphere sintering, and attrition may also be involved. SEM of FCC fracture surfaces, AEM of Y zeolite, and electron microscopy of this work are developed to better understand and minimize catalyst deactivation.

CATALYTIC CRACKING OF PALM OIL: KINETIC STUDY

Clean Air ◽  
2007 ◽  
Vol 8 (1) ◽  
pp. 65-79 ◽  
Author(s):  
Farouq Twaiq ◽  
Abdul Rahman Mohamed ◽  
Subhash Bhatia
Keyword(s):  
Kinetic Study ◽  
Palm Oil ◽  
Catalytic Cracking

Five-Lump Kinetic Model for the Catalytic Cracking Process\

2018 ◽  
Vol 69 (10) ◽  
pp. 2633-2637
Author(s):  
Raluca Dragomir ◽  
Paul Rosca ◽  
Cristina Popa
Keyword(s):  
Kinetic Model ◽  
Programming Language ◽  
Catalytic Cracking ◽  
Computational Method ◽  
Industrial Data ◽  
New Model ◽  
Optimization And Control ◽  
Cracking Process ◽  
And Control ◽  
Matlab Programming

The main objectives of the present paper are to adaptation the five-kinetic model of the catalytic cracking process and simulation the riser to predicts the FCC products yields when one of the major input variable of the process is change. The simulation and adaptation are based on the industrial data from Romanian refinery. The adaptation is realize using a computational method from Optimization Toolbox from Matlab programming language. The new model can be used for optimization and control of FCC riser.

scholarly journals Catalytic cracking of jatropha oil into biofuel over hierarchical zeolite supported NiMo catalyst

2021 ◽  
Author(s):  
Isalmi Aziz ◽  
Tri Retnaningsih ◽  
Dhika Gustama ◽  
Nanda Saridewi ◽  
Lisa Adhani ◽  
...  
Keyword(s):  
Catalytic Cracking ◽  
Jatropha Oil ◽  
Hierarchical Zeolite ◽  
Nimo Catalyst

scholarly journals A diffusion anisotropy descriptor links morphology effects of H-ZSM-5 zeolites to their catalytic cracking performance

2021 ◽  
Vol 4 (1) ◽  
Author(s):  
Xiaoliang Liu ◽  
Jing Shi ◽  
Guang Yang ◽  
Jian Zhou ◽  
Chuanming Wang ◽  
...  
Keyword(s):  
Catalytic Activity ◽  
Catalytic Cracking ◽  
Catalytic Performance ◽  
Zeolite Catalysts ◽  
Time Resolved ◽  
Cracking Performance ◽  
Morphology Effect ◽  
Ft Ir ◽  
The Difference ◽  
Dynamics Simulations

AbstractZeolite morphology is crucial in determining their catalytic activity, selectivity and stability, but quantitative descriptors of such a morphology effect are challenging to define. Here we introduce a descriptor that accounts for the morphology effect in the catalytic performances of H-ZSM-5 zeolite for C4 olefin catalytic cracking. A series of H-ZSM-5 zeolites with similar sheet-like morphology but different c-axis lengths were synthesized. We found that the catalytic activity and stability is improved in samples with longer c-axis. Combining time-resolved in-situ FT-IR spectroscopy with molecular dynamics simulations, we show that the difference in catalytic performance can be attributed to the anisotropy of the intracrystalline diffusive propensity of the olefins in different channels. Our descriptor offers mechanistic insight for the design of highly effective zeolite catalysts for olefin cracking.

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