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06.01 Calculation Error on Property Model Change (p. 337)
06.02 Required Mass Flow Through Safety Valve (p. 338)
06.03 Heat Exchanger Duty Using Different Calculation Routes (p. 340)
06.04 Combustion of Liquid n-Butanol for Steam Generation (p. 343)
06.05 Standard Gibbs Energy of Formation of Hydrogen Chloride (p. 346)
06.06 Deacon Reaction in a Flue Gas (p.347)
P06.01 Enthalpy of a Liquid Stream
A process simulation software reports the enthalpy of a saturated liquid stream of 53 kg/h of cyclohexane at 45°C as -2.301 Gcal/h. Estimate this value using the data given in Appendix A ad B and compare the results.
P06.02 Cooling Duty after Oxyhydrogen Gas Reaction
How much heat per mol of water must be removed to reach a final
temperature of T = 1000 K when the oxyhydrogen gas reaction
H2 + 0.5 O2 in equilibrium with H2O
is performed? Use the ideal gas equation of state and the physical properties from Appendix A. The starting temperature Tstart = 400 K. Assume stoichiometric composition and total conversion.
P06.03 Enthalphy Change of Water Upon Heating Using Two Routes (A, B)
Calculate the enthalpy difference when pure liquid water at P = 1
bar is heated up from J1 = 20°C to J2 = 70°C using both Route A and Route B (see Chapter 6.2). Which is the better option?
Use the Peng-Robinson equation of state for the vapor phase.
P06.04 Enthalpy of Vaporization of Propylene Using Route B
Calculate the enthalpy of vaporization of liquid propylene at J1 = -100°C, J2 = 0°C, J3 = 50°C, J4 = 70°C and J5 = 90°C using Route B (see Chapter 6.2). Use the Peng-Robinson equation of state for the vapor phase. Up to which temperatures can Route B be regarded as a useful option?