Hydrocracking Model

Figure 1. Calculated hot-spot formation in modeling hydrocracker operation. Reprinted with permission from S. B. Jaife, Ind. Eng. Chem. Process Dev. 15,410 (1976). Copyright 1976 American Chemical Society.

P-15 - Model hydrocracking catalysts combining NiMo sulfide and large-pore zeolite effect of the zeolite nature on the location of NiMo sulfide in relation with catalytic properties... 

Ferreira Da Silva, R.M.C., de Medeiro, J.L., Araujo, O.Q.F. 2007. A network of chemical reactions for modeling hydrocracking reactors. In Pmceedings of European Congress of Chemical Engineering (ECCE-6), Copenhagen, Denmark, September 16-20. 

Based on Laxminarasimhan s work, Korasheh et al. (2001,2005) and Ashuri et al. (2007) have extended the application of the continuous lumping to model hydrocracking, hydrodesulfurization (HDS), and hydrodenitrogenation (HDN) in order to predict the dependence of parameters with temperature. Basak et al. (2004) have modeled the hydrogen consumption and the bed temperature profile in an industrial... 

MODELING HYDROCRACKING OF MAYA CRUDE OIL 11.5.1 Experimental Results... 

C. R. Cutier and R. B. Hawkins, "AppHcation of a Large Model Predictive Controller to a Hydrocracker Second Stage Reactor," Proceedings of... 

It should be noted that many practically important catalytic transformations (such as isomerization of or hydrocracking of paraffins), which are presumed to proceed via consecutive mechanisms, are performed on multifunctional catalysts, with which the coupling of reactions in the sense just discussed may not necessarily occur. The problem of the selectivity of some models of polystep reactions on these catalysts has been discussed in detail by Weisz (56). 

Abramova, A. V., Slivinsky, Ye. V., Goldfarb, Y.Y., Kitaev, L. Ye., Kubasov A. A., Modeling of Nature and Strength of Acid Centres in Ultrastable Zeolites as a Component of Hydrocracker Catalysts, in Hydrotreatment and Hydrocracking of Oil Fractions. 1999, Elsevier Science B. V New York. pp. 377-380. 

All the hydrocracking/hydrogenation experiments were carried out in 500 ml capacity spinning type autoclaves. Two autoclaves of this design were used and the autoclaves were compared in experiments using the model compound phenanthrene, chosen because phenanthrene and its hydro-derivatives represent a large proportion of the solvent which is recycled in coal liquefaction processes. 

An LP model for a petroleum refinery would consist of a number of modules for the different units (e.g., FCC, hydrocracker, fluid delayed coker, etc.). Each of these... 

Elkamel, A., Al-Ajmi, A., and Fahim, M. (1999) Modeling the hydrocracking process using artificial neural networks. Petroleum Science el Technology, 17, 931. 

Hydrogenation and hydrocracking activity of iron catalysts has been extensively investigated using coal and model compounds (93 -95). Iron catalysts can hydrogenerate olefinic unsaturated bonds, while they are known to be less active for the hydrogenation of aromatic rings compared with molybdenum-based catalysts. 

The experimental data obtained in the hydrocracking of coal, coal oil and phenanthrene were tested with equations (iii) and (iv) as shown in Figures 8 and 9 and the data were found compatible with the model. This compatibility confirmed that the rates of hydrocracking were controlled by surface chemical reactions as were also indicated by arrhenius activation energies (Table VIII). 

Well over 50 large-scale EO model-based RTO applications have been deployed for petroleum refining processes. These model applications have been deployed in petroleum refineries Liporace et al., 2009 Camolesi et al., 2008 Mudt et al., 1995, both on separation units (crude atmospheric and vacuum distillation units) and on reactor units (including fluidized catalytic crackers (FCC), gasoline reformers, and hydrocrackers). 

The hydrocracker simulator was also converted to subroutine form for inclusion in the nonlinear programming model of the Toledo process complex. The subroutine was considerably simplified, however, to save computer time and memory. The major differences are (1) the fractionation section is represented by correlations instead of by a multi-stage separation model, (2) high pressure flash calculations use fixed equilibrium K-values instead of re-evaluating them as a function of composition, and (3) the beds in each reactor are treated as one isothermal bed, eliminating the need for heat balance equations. 

J.Coreila,A-Monzon,J.B.ButlrR.PlAt)S4l The modelling of the Kinetics of Deactivation of a Commercial Hydrocracking Catalyst in ihe Reaction of Cumene Disproportionation J.CatalysJs 100(1986)149... 

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