ChEn 4501 Process Design HDA process Alternative Design Economics Report Section 5 – Group 7 – Yellow Customer Name(Economist) Customer Name(Engineer) Customer Name(Coordinator) Teacher Name

Our Alternative Design PFD

This added millions to our yearly cash flows. What’s New? We installed a heat exchanger using the reactor inlet and outlet as the cold and hot streams. This added millions to our yearly cash flows. For our alternative design, the purge stream was treated in a high pressure flash tank with the goal of benzene recovery. A few auxiliary process units were required to bring the purge stream to the temperature and pressure required for an acceptable separation.

All costs and revenues ($/yr) New Material Flows Stream Flow (lb/hr) Cost ($/100 lb) Materials Cost ($/yr) Fuel Values ($/yr) All costs and revenues ($/yr) Feed Toluene 26,260 -27.27 -58,370,000 # Feed Gas 1,291 -50.33 -5,030,000 Benzene Product 20,870 40.86 69,500,000 Purge Gas 5,229 9,586,000 Purge Diphenyl 1,105 941,100 Total yearly profit from materials bought, sold and purged: $16.62 M/yr

New Energy Flows Energy Streams for: Duty (BTU/hr) Utility Energy Cost ($/yr) Reactor Cooling 527,800 Cooling Water 7,349 Compressor 1 1,185,000 Electricity 169,800 Compressor 2 75,640 Pump 1 28,830 4,132 Pump 2 64,090 9,185 Stabilizer Column Condenser 3,096 3.906 Stabilizer Column Reboiler 4,140,000 Steam at 450 psig 184,800 Benzene Column Condenser 10,920,000 13,780 Benzene Column Reboiler 8,034,000 358,600 Toluene Column Condenser 1,719,000 2,169 Toluene Column Reboiler 1,645,000 235,800 Turbine Generator 979,800 -140,400 Total yearly operating costs from utilities $920,900/yr