Indexing
All Issues
Submission
Author Guidelines
Reviewers
Editorial Members
Publication Fee
Vol.1 , No. 4, Publication Date: Sep. 16, 2014, Page: 194-198
 h period using two adjustable feed rates of 7.7 and 8.3 10-5m3/s. Between 400 ± 50oC the reactor performance and the model result showed an excellent correlation of C2 output suggesting that the catalyst ratio and the temperature favored hexane-heptene fragmentation with a methyl radical as a result of the short space time (0.012s). It was observed that the increase in gas phase(Mgas) was responsible for catalyst regeneration since the catalyst mass (Mcat) was constant in the circulating volume. This condition helped the 3-lump model to operate as a two-stage steady state single reaction with a maximum usage of kerozene at a single pass with a 96% yield of ethylene.&picture=http://www.aascit.org/aascit/decorators/img/journal/902.jpg)
| [1] | Julius Adesoji Adeyinka, Chemical Engineering Department, University of Abuja, Nigeria. |
| [2] | Otaraku Ipeghan Jonathan, Chemical Engineering Department, University of Port Harcourt, PH, Nigeria. |
Catalytic cracking of C13 was carried out on a Z5CaO catalyst using a two stage single reaction to evaluate a 3-lump model of a steady state reaction setting C2 as the objective product. A total volume of 0.0962m3 of kerozene was used over a ten (10) h period using two adjustable feed rates of 7.7 and 8.3 10-5m3/s. Between 400 ± 50oC the reactor performance and the model result showed an excellent correlation of C2 output suggesting that the catalyst ratio and the temperature favored hexane-heptene fragmentation with a methyl radical as a result of the short space time (0.012s). It was observed that the increase in gas phase(Mgas) was responsible for catalyst regeneration since the catalyst mass (Mcat) was constant in the circulating volume. This condition helped the 3-lump model to operate as a two-stage steady state single reaction with a maximum usage of kerozene at a single pass with a 96% yield of ethylene.
Keywords
Kerozene, Cracking, Ethylene, Steady State, Two-Stage, Model, Pilot-Riser, Catalyst Bed
Reference
| [01] | Adeyinka, J.S. and Muganlinskii, F.F. (1994) "Kinetic of Methane Oxidative Pyrolysis Process for Higher Molecular Weight Alcohol (HMMA) Synthesis" A.M.S.E (C) Vol. 47(4): 47-63. |
| [02] | Adeyinka, J. S, Umesi, N. O; Otaraku, I.J and Odobo, O. M. O (2008) ‘Synthesis and property Evaluation of BaX Zeolite’ Jour. of Oilfield Chemistry Vol.1:36 – 41. |
| [03] | Adeyinka, J. S, and Otaraku, I.J (2014a) ' Kinetics of Catalytic Cracking of Kerosene to Ethylene on CaO promoted Z5 nano-Catalyst' Jour of Chemical Processes IISTE USA (in press). |
| [04] | Adeyinka J. S; Oghenejoboh, M. K; Otaraku I. J and Nwambo, Y. P (2014b) ‘Aromatization of Propylene on Pt-Cu/β-Al2O3 Catalyst' Jour of Chemical Processes IISTE USA (in press). |
| [05] | Ali, A. G. A; Ali, L. I; Aboul-Fotouh, S and Aboul-Gheit, A. K. (2001) ' Hydro-isomerization, hydro-cracking and dehydrocyclization of n-pentane and n-hexane using Mono - and Bimetallic catalysts promoted with Flourine' Applied Catalysis A: General. 215:161 - 173. |
| [06] | Bertolacini R. J and Pellet, R. J (1980) stud. Surf. Sci. Catal. In catalyst reactivation, Delmon, B; Fromet, G.F Eds.vol.6:-72 77. |
| [07] | Coppens, M.O and Frovient, G.F. (1995) Diffusion and reaction in fractal catalyst pore II: Diffusion and first order reaction” Chemical Engineering Sci. 50(6)1027 – 1039. |
| [08] | Corrella, J, Fernandez, A and Vidal, J. M (1986) Pilot Plant for the Fluid Catalytic Cracking Process: Determination of the Kinetic Parameters of Deactivation of the Catalyst' Ind Eng. Chem. Process Des. Dev. 25; pp 554 -562. |
| [09] | el Nashaei, S. S. E and el Shishini, S. S (1993) 'Comparison between different Mathematical models for simulation of Industrial Fluidized catalytic Cracking Unit' Math. Comput. Modeling Vol. 18(6)91 - 110 |
| [10] | Forissier, M; Formenti, M and Bernard, J. R (1991) 'Effect of Total Pressure on Catalytic Cracking Reaction' Catal Today 11, pp. 73 – 82. |
| [11] | George, J. A and Abdullahi, M. A (2004) 'Catalytic Naphtha reforming' Second edition. Marcel Dekker, Inc. N.Y Basel pp391 - 432. |
| [12] | Gilbert, F. F and Kenneth B.B (1979) 'Chemical Reactor Analysis and Design' John Wiley and Sons, NY. |
| [13] | Kellog. M .W (1985) Production of Ethylene and Olefin Compounds by Steam Pyrolysis of Hydrocarbons' Hydrocarbon Processing. Nov. 1985, pp134 – 136. |
| [14] | Kraemer, D. W, Sedran U. J and De Lasa H. I (1990) 'Catalytic Cracking Kinetics in a Novel Riser Simulator' Ind. Eng Chem Res. 28: pp 665 – 673. |
| [15] | Samoilova, N. N., Erkin, V. N. and Serikov. P.Y (1991) 'Some Characteristics of the Kinetics of Catalytic Cracking of Heavy Feed' Chem. Tech. Fuel Oil 26. pp521 – 525. |
| [16] | Weekman V. W. (1986) 'A Model of Catalytic Cracking Conversion in Fixed, Moving and Fluid Bed Reactors' Ind. Eng. Chem. Process Des. 7, pp 90 -95. |
| [17] | Weekman, V.M and Nace, D. M (1990) Kinetics of catalytic cracking Selectivity I Fixed, Moving and Fluid Bed Reactor’s AIChE Jour. Vol.16: 397 – 404. |
| [18] | Rajesh, B. B; Nobuko, K and Masaru, I (2005) 'Dehydrogenation of cyclohexane over Ni based catalyst supported on Activated carbon using spray-pulse reactor and Enhanced Activity by addition of small amount of Pt' Catalysis Letters. |
| [19] | Hollewand, M. P and Gladden, L. F (1992) 'Modeling of diffusion and reaction in porous catalysts using a random three- dimensional network model' Chem. Engineering Sci 47(7)1761 - 1770. |
