Catalytic cracking equilibrium catalyst

This maximum in the entrainment flux observed by Wen and Tanaka is in some agreement with the work of Baeyens et al. [15]. Baeyens et al. worked with equilibrium fluidized catalytic cracking (FCC) catalyst powder with varying additions of fines. They found that below a critical particle size, entrainment rates leveled off and noted that this reflected the point where Van der Waals forces were in balance with gravitational forces. For their systems, this critical particle size was found to be approximated by the expression... 

Comparison of Yield Structure for Fluid Catalytic Cracking of Waxy Gas Oil over Commercial Equilibrium Zeolite and Amorphous Catalysts... 

Olefin isomerization reactions range from some of the most facile using acid catalysts to moderately difficult and, as components of more complex reaction schemes such as catalytic cracking, may be among the most common reactions in hydrocarbon processing. As stand-alone reactions, they are primarily used to shift the equilibrium between terminal and internal olefins or the degree of branching of the olefin. While olefin isomerization was considered for the production of MTBE, today stand-alone olefin isomerization processes are only considered for a few special situations within a petrochemical complex. 

Bayraktar, O., and Kugler, E. Characterization of Coke on Equilibrium Fluid Catalytic Cracking Catalysts by Temperature-Programmed Oxidation. Applied Catalysis A General 233 (2002) 197-213. 

Catalytic Cracking Test. A standard microactivity test (MAT) was used to evaluate the conversion and selectivity of catalyst samples. The tests were done at the University of Pittsburgh s Applied Research Center (former Gulf Research Laboratory), a qualified laboratory for MAT evaluations. A standard method, developed by Gulf, was used without modification. A Cincinnati gas oil was cracked under the following conditions cat/oil=3, 16 h 1 WHSV, and 516°C. Prior to charging the reactor, all samples underwent a standard thermal pretreatment. Solids were first heat shocked for 1 h at 593°C. Next, selected materials were impregnated with 3000 ppm Ni and 6000 ppm V, as naphthenates. Then all samples were calcined for 10 h at 538°C. Finally, each material was steamed at 732°C for 14 h in a fluidized bed to produce a catalyst in a simulated equilibrium state. 

S. C. Cardona and A. Corma, Tertiary recycling of polypropylene by catalytic cracking in a semibatch stirred reactor. Use of spent equilibrium FCC commercial catalyst, Appl. Catal. B Env., 25, 151 (2000). 

A. Marcilla, A. Gomez, J. A. Reyes-Labarta, A. Giner and F. Hernandez, Kinetic study of polypropylene pyrolysis using ZSM-5 and an equilibrium fluid catalytic cracking catalysts. J. Anal. Appl. Pyrolysis, 68-69, 467-480 (2003). 

As an example, the results from catalytic cracking of three types of waxes from thermal cracking of PE are given in Table 8.2 [22], The catalyst used, the equilibrium FCC catalyst. 

The catalytic cracking of cumene to propylene and benzene was studied at 800°F using a fiuidized bed 3 inches in diameter [7]. The silica-alumina catalyst had 13% AI2O3 and a BET surface of 490 m /g. The 100-to 200-mesh fraction of the catalyst was used after fiuidizing for several hours to remove fines. The predicted equilibrium conversion was 0.77, and in many of the fixed bed tests this value was almost reached. With a porous-plate distributor and 8-inch initial bed height, the conversion was 62% at 0.1 ft/sec and 50% at 0.2 ft/sec. Treating the reaction as pseudo-first-order, Nf was estimated to be 8.4 for 0.1 ft/sec and 4.2 for 0.2 ft/sec. 

An easy method to estimate rate constants in complex kinetic models is proposed. This method reduces the number of parameters to be estimated simultaneously. A 5-lump kinetic model for the catalytic cracking process was selected in order to tqiply the proposed methodology. Experimental data obtained in a MAT using three gas oils and a commorcial equilibrium catalyst unit were used to evaluate the rate constants. 

A MAT reactor was used to crack three industrial feedstocks over a commercial equilibrium catalyst in the range of reaction temperature of 480-500°C and WHSV of 6-48 h. The experimental data were utilized to evaluate the kinetic parameters of a 5-lump model for catalytic cracking process, which includes the unconverted gas oil, gasoline, LPG, dry gas and coke. 

Sowerby, B. Becker, S. J., Modeling Catalytic Cracking Kinetics Using Estimated Adsorption Equilibrium Constants, In Dynamics of Surfaces and Reaction Kinetics in Heterogeneous Catalysts, Froment, G. F. Waugh, K. C. (Eds.), Elsevier, 1997. 

I 4 Predictive Modeling of the Fluid Catalytic Cracking (FCQ Process Table 4.23 Equilibrium catalyst properties. 

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