Page 385 - Chemical engineering design

DESIGN INFORMATION AND DATA
8.6. For the compounds listed below, estimate the constants in the equation for ideal
gas heat capacity, equation 3.19, using the method given in Section 8.9.2. 359
1. 3-methyl thiophene.
2. Nitrobenzene.
3. 2-methyl-2-butanethiol.
4. Methyl-t-butyl ether.
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8.7. Estimate the heat of vaporisation of methyl-t-butyl ether, at 100 C.
8.8. Estimate the gaseous phase diffusion coefficient for the following systems, at 1
atmosphere and the temperatures given:
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1. Carbon dioxide in air at 20 C,
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2. Ethane in hydrogen at 0 C,
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3. Oxygen in hydrogen at 0 C,
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4. Water vapour in air at 450 C,
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5. Phosgene in air at 0 C.
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8.9. Estimate the liquid phase diffusion coefficient for the following systems at 25 C:
1. Toluene in n-heptane,
2. Nitrobenzene in carbon tetrachloride,
3. Chloroform in benzene,
4. Hydrogen chloride in water,
5. Sulphur dioxide in water.
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8.10. Estimate the surface tension of pure acetone and ethanol at 20 C, and benzene at
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16 C, all at 1 atmosphere pressure.
8.11. Using Lydersen’s method, estimate the critical constants for isobutanol.
Compare your values with those given in Appendix C.
8.12. The composition of the feed to a debutaniser is given below. The column will
operate at 14 bar and below 750 K. The process is to be modelled using a
commercial simulation program. Suggest a suitable phase equilibrium method to
use in the simulation.
Feed composition:
kg/h
propane C 3 910
isobutane i C 4 180
n-butane n C 4 270
isopentane i C 5 70
normal pentane n C 5 90
normal hexane n C 6 20

8.13. In the manufacture of methyl ethyl ketone from butanol, the product is separated
from unreacted butanol by distillation. The feed to the column consists of a mixture
of methyl ethyl ketone, 2-butanol and trichloroethane. What would be a suitable
phase equilibrium correlation to use in modelling this process?