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2003 Course Reaction Eng. - II

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Total No. of Questions : 8] [Total No. of Pages : 3 [3664] - 323 P 1353 B.E. (Petrochemical) REACTION ENGINEERING - II Time : 3 Hours] [Max. Marks : 100 Instructions to the candidates: 1) Answer any 3 questions from each section. 2) Answers to the two sections should be written in separate answer books. 3) Neat diagrams should be drawn wherever necessary. 4) Figures to the right indicate full marks. 5) Use of logarithmic tables, slide rule, Mollier charts, electronic pocket calculator and steam tables is allowed. 6) Assume suitable data, if necessary. SECTION - I Q1) a) b) Explain what you mean by Langmuir - Hinshelwood kinetics? [4] Derive rate expression for the following catalytic reaction assuming surface reaction controls the overall rate [6] A + 2B R + S (g) c) (g) (g) (g) State (only) the rate expressions for the reaction in (b), assuming (i) Adsorption of B controls (ii) Desorption of R controls. (Useful form of rate expressions for kinetic data fitting only is expected without proof). [6] Q2) A small experimental packed bed reactor (w = 1 kg) using very large recycle of product stream gives the following kinetic data : A R, C A 0 = 10 mol / m 3 CA, mol/m3 1 2 3 6 9 5 20 65 133 540 0 , lit/hr Find the amount of catalyst needed for 75% conversion for a flow rate of 1000 mol A/hr with CA = 8 mol/m3. Using 0 a) Packed Bed Reactor with no recycle. b) Fluidized Bed Reactor. [16] P.T.O. Q3) a) b) Define effectiveness factor. Discuss its utility in kinetic studies and reactor design. [4] Reaction A R is to take place on a porous catalyst pellet (dp = 6 mm, D = 10-6 m3/m cat.s) How much is the rate slowed by pore diffusional resistance if the concentration of reactant bathing the particle is 100 mol/m3 and the diffusion free kinetics are given by c) [8] r A = 0.1C 2 mol/m3 cat. s. A State how within - particle T and film T can be estimated for a given catalyst pellet using laboratory test. [4] Q4) a) b) c) Discuss factors affecting the activity of a catalyst. [4] Derive concentration - time relationship in case of first order reaction, first order deactivation taking place in batch-solids batch fluid mode.[10] First order reaction carried out in a batch reactor takes place on a catalyst that deactivates by first order kinetics. Reaction is irreversible, having rate constant as 0.2 m3. kgcat-1 s-1. Conversion obtained after waiting for a long time is 60%. Catalyst loading per unit reaction volume is 1.20 kg/m3. Calculate the rate constant for catalyst deactivation. [4] SECTION - II Q5) a) b) c) d) Describe four kinetic regimes usually obtained in gas liquid reactions.[6] Write the design equation used for gas liquid contact in packed bed reactor. [3] State the criterion for a gas-liquid reaction to take place at gas-liquid interface. How is the overall rate expressed in such a case? [4] State various types of gas liquid contactors. [3] Q6) Uniform sized spherical particles UO3 are reduced to UO2 in a uniform environment with the following results. [16] t hr 0.180 0.347 0.453 0.567 0.733 XB 0.43 0.68 0.80 0.95 0.98 Assuming that shrinking core model holds. Find the controlling mechanism and a rate equation for the reduction. [3664] - 323 -2- Q7) a) b) Discuss what you mean by Residence Time Distribution (RTD). How does RTD account for deviations from ideal flow? [6] Response of a reaction vessel to pulse input is given below. Time t, min CPulse, gm/lit 0 0 5 3 10 5 15 5 20 4 25 2 30 1 35 0 Calculate i) Mean residence time of fluid in the vessel. ii) Fraction of the exiting fluid that has spent time between 10 min and 20 min. [12] Q8) Write notes a) Hatta Number and its significance. b) Merits and demerits of fluidized bed reactor. c) Reactors used in crude oil Refining. d) Kinetic Lumping. [3664] - 323 -3- [16]

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