﻿ Problems and Solutions Chapter 2

# ## Problems and SolutionsChapter 6 Caloric Properties

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06.01           Calculation Error on Property Model Change

06.02           Required Mass Flow Through Safety Valve

06.03           Heat Exchanger Duty Using Different Calculation Routes

06.04           Combustion of Liquid n-Butanol for Steam Generation

06.05           Standard Gibbs Energy of Formation of Hydrogen Chloride

06.06           Deacon Reaction in a Flue Gas

06.07           Deacon Reaction in a Flue Gas by G-Minimization

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 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?