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plant design

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by

babak panahi

on 14 March 2013

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Transcript of plant design

Production of 45,000 tons/year of 99.8% Pure Cyclohexane through the Hydrogenation of Benzene Catalyst Introduction Uses Uses Market Analysis Benzene & Cyclohexane Price Trend Comparison Supply & Demand US Data Historical:
Fractional Distillation of Crude Oil
Isomerization

Modern:
Hydrogenation of Benzene
Liquid Phase
Vapour Phase Rationale for selection of IFP process
No feed preheating required
Good thermal control leads minimizes side reactions
Only two reactors required, a slurry and a finishing reactor
Convenient catalyst replacement due to continuous circulation of catalytic slurry
Relatively low catalyst & equipment cost
Minimal downtime IFP (Institut Francais du Petrole) Process Catalyst & Reaction Kinetics Raney-Nickel Catalyst (NIPS-2®) Nickel on Alumina (LD-143®) Possible Side Reactions Reaction Kinetics Location Catalyst & Reaction Kinetics Catalyst & Reaction Kinetics Location 532.4110 x10^6
Gallons Liquid Phase: UOP Hydrar Process Equipment Selection: Primary Reactor Packed bubble-flow reactors Slurry Reactors Equipment Selection: Slurry Heat Exchanger Equipment Selection: Other Heat Exchangers Equipment Selection: Separator Equipment Selection: Stabilizer Key: B (Best), G (Good Operation), F (Fair Operation, but better choice is possible), Rd (Risky unless carefully designed, but could be best choice in some cases), R (Risky due to insufficient data), P (Poor Operation), E (Operable but unnecessarily expensive). Equipment Selection: Reboiler Equipment Selection: Reboiler Equipment Selection: Pumps Equipment Selection: Pumps Equipment Selection: Compressors Equipment Selection: Compressors Future Considerations Agenda Introduction
Uses
Market Analysis
Technology Survey
PFD/Mass & Energy Balance
Catalyst & Reaction Kinetics
Equipment Selection
Plant Location
Conclusion Aspen simulation Aspen Plus Simulation Cocurrent TBR Counter Current
TBR Packed Bubble
Column Slurry
Reactor Technology Survey
Full transcript