Mathematical Modeling and Simulation for Production of MTBE

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Greek Symbols Symbol Definition Units α Vapor activity coefficient [ _ ] γ Liquid activity coefficient [ _ ] ΔE The error [ o C] ε Reaction volume [m 3 ] ξ Time dimensionless [−] λ Latent heat [J/mole] Λ Parameter in Wilson model [−] υ Stoechiometric coefficient of component [−] ρ Density [kg/m 3 ] Φ Fugacity coefficient [−] List of Abbreviations Symbol Definition EFAO Europe Fuel Associated Organization EQ Equilibrium ETBE Ethyl tertiary butyl ether IB Isobutene MATLAB Matrix Laboratory MESH (Material balance, Equilibrium, Summation of mole, Heat balance) MTBE Methyl tertiary butyl ether NB Normal butane NEQ Non equilibrium RCM Residue curve map RD Reactive distillation TAME Tertiary amyl methyl ether VLE Vapor Liquid Equilibrium X
Chapter One Introduction 1.1 INTRODUCTION: Chapter One Introduction Distillation is the most important separation method in refinery and chemical industry. In terms of installed capacity and energy usage, the commitment of the process industry to this unit operation is enormous. In USA, for example, the energy consumed by distillation is equivelent to about 7.5 % of the U.S. oil consumption (Kimmo, 1998). Reactive distillation (RD) is a combination of separation and reaction in a single vessel, the combination of reaction and distillation is an old idea that has received renewed attention recently. There are two main types of reactive distillation, batch and continuous, the continuous RD is largerly used for production scale, constant product composition, and continuous feed provision. 1.2 SEPARATION PROCESS: The driving force for any distillation process is the difference between the liquid and vapor composition in the mixture. When the liquid and the vapor have the same composition at a certain point, this mixture is called azeotropic mixture and this point is called azeotropic point. Therefore there is no driving force for separation at this point, and the azeotropic mixtures cannot be separated by conventional distillation technique. The conventional distillation can produce azeotropic products, which must be separated by using other methods. There are several enhanced distillation methods which can be used to separate azeotropic mixtures, such as (Perry,1997; Seader, 2006) : 1
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Chapter Four Results and Discussion
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Chapter Five Conclusions and Recomm
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• A References Abrams, D. S. and
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C Carra, S .,E. Santacesaria,M. Mor
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F Fien, G. and Liu, Y.A. “Heurist
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Kooijman H. and Taylor R. The ChemS
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R Renon, H., Prausnitz, J. M., “L
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T Taylor R., Amanda Miller, and Ang
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APPENDIX A: Appendix A (A-1)-Sample
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A-3 Appendix A H = -143.3301 -0.336
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B-2 Appendix B TAB6LE (B-3): LATENT
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UNIFAC Method: Wilson model: C-2 Ap
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Table (C.5)UNIFAC-VLE interaction p
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Condenser Reboiler HEAT DUTY ( W) T
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Reaction rate constant (mol/h/g of
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(7) (8) (9) (10) (11) (12) (13) (14
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Table (E-2) the first assumption of
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0.7 0.9997 0.8 0.9998 0.9 0.9998 1
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Mathematical Modeling and Simulation for Production of MTBE

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