11-Lect-Pressure Drop in Reactors0

Mole balance pbr cstr batch 1 mole balance dw 2 rate

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Unformatted text preview: Engineering - Musgrave € € 1. Mole Balance PBR CSTR Batch 1. Mole Balance dW = 2. Rate Law 2. Rate Law -rA=f(CA) -rA=g(CA) -rA=h(CA) FA 0 dX −rA + 1 2 −rA + = kPA / 3 PB2 / 3 = kRTC1 / 3CB / 3 A 3. Stoichiometry Flow Batch 3. Stoichiometry € € Liquid Gas Liquid Gas Flow CA = FA υ Gas υ = υ 0 (1 + εX ) P0T PT0 4. Combine dV=dV(X) dt=dt(X) (1 − X ) P CA€ CA 0 = (1 + εX ) P0 4. Combine ȹ b ȹ ȹ Θ B − X ȹ ȹ a Ⱥ P €C =C B A0 (1 + εX ) P0 5. Evaluate V=V(X) t=t(X) dW = € dW = • 1st order overall, 1/3 order in A • Not equimolar ε is not 0 • Irreversible • Gas phase • PBR Pressure Drop in Reactors FA 0 dX 2/3 Ⱥ ȹ b ȹ Ⱥ 1/ 3 ȹ Θ B − X ȹ Ⱥ Ⱥ Ⱥ − (1€ X ) P Ⱥ ȺC ȹ a Ⱥ P Ⱥ € kRTȺCA 0 Ⱥ (1 + εX ) P0 Ⱥ Ⱥ A 0 (1 + εX ) P0 Ⱥ Ⱥ Ⱥ Ⱥ Ⱥ Ⱥ 5. Evaluate FA 0 dX −r + €A dW = FA 0 dX 2 kRTC1 / 3CB / 3 A How does P vary along the reactor length? Lecture 11 - Page 16 Chemical Reaction Engineering - Musgrave € 8 5. Evaluate dW = FA 0 dX 2/3 Ⱥ ȹ b ȹ Ⱥ 1/ 3 ȹ Θ B − X ȹ Ⱥ Ⱥ 1 − X ) Ⱥ Ⱥ ( ȹ a Ⱥ Ⱥ kRTȺCA 0 yȺ ȺC y (1 + εX ) Ⱥ Ⱥ A 0 (1 + εX ) Ⱥ Ⱥ Ⱥ Ⱥ Ⱥ Ⱥ εX not Negligible dy α = − (1 + εX ) dW 2y α≡ 2β 0 (1 − φ ) Ac ρc P0 Using the definition of y and simplifying: € € FA 0 dX FA 0 dX dW = = Ⱥ Ⱥ (1 − X ) Ⱥ1 / 3Ⱥ (1 − X ) Ⱥ2 / 3 ȹ 1 ȹ2 / 3€ (1 − X ) Ⱥ Ⱥy kRTCA 0 Ⱥ yȺ Ⱥ Ⱥ y kRTCA 0 ȹ ȹ ȺCA 0 ȹ 2 Ⱥ Ⱥ (1 + εX ) Ⱥ...
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This note was uploaded on 04/25/2010 for the course CHEN 4330 taught by Professor Staff during the Spring '08 term at Colorado.

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