By Tarek Ahmed
The Vapor-Liquid section Equilibria approach is common for the distillation of petroleum and traditional gasoline ahead of it's transported to the refinery for ultimate owning. whereas simulation courses gives you a few solutions, the standard of the consequences received with those courses depends upon the standard of the version parameters. Parameters that are derived utilizing the calculations tools locate during this book.
- Includes reasons of formulas
- Step through step calculations
- Provides examples and ideas
Read Online or Download Working Guide to Vapor-liquid Phase Equilibria Calculations PDF
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Additional resources for Working Guide to Vapor-liquid Phase Equilibria Calculations
Sample text
APPLICATIONS OF THE EQUILIBRIUM RATIO IN RESERVOIR ENGINEERING Step 3. , xiMi, lb/lb-mol roi ¼ density of component i at standard conditions, lb/ft3 The density of the plus fraction must be measured. Step 4. Using Figure 6-4, enter the rC3þ value into the left ordinate of the chart and move horizontally to the line representing ðmC2 ÞC2þ ; then drop vertically to the line representing ðmC1 ÞC1þ . The density of the oil at standard condition is read on the right side of the chart. Standing (1977) [56] expressed the graphical correlation in the following mathematical form: h i rsc ¼ rC2þ 1 À 0:012ðmc1 ÞC1þ À 0:000158ðmC1 Þ2C1þ þ 0:0133ðmC1 ÞC1þ þ 0:00058ðmc1 Þ2C2þ with h i rC2þ ¼ rC3þ 1 À 0:01386ðmc2 ÞC2þ À 0:000082ðmC2 Þ2C2þ þ 0:379ðmC2 ÞC2þ þ 0:0042ðmc2 Þ2C2þ where rC2þ ¼ density of ethane-plus fraction.
Determine the apparent molecular weight of this mixture: Ma ¼ Sxi Mi Ma ¼ 113:5102 Step 5. Compute the density of the oil system: r0 ¼ r0 ¼ Ma Vm 113:5102 ¼ 44:896 lb=ft3 2:528417 C H A P T E R 7 Equations of State An equation of state (EOS) is an analytical expression relating the pressure p to the temperature T and the volume V. A proper description of this PVT relationship for real hydrocarbon fluids is essential in determining the volumetric and phase behavior of petroleum reservoir fluids and in predicting the performance of surface separation facilities.
For a total of 1 lb-mol of the hydrocarbon mixture, the following conditions are applied at the bubble-point pressure: nL ¼ 1 nv ¼ 0 Obviously, under these conditions, xi ¼ zi. Applying the preceding constraints to Equation 2-15 yields X ðzi Ki Þ ¼ 1 (6-3) i Following the procedure outlined in the dew-point pressure determination, Equation 6-3 is solved for the bubble-point pressure pb by assuming various pressures and determining the pressure that will produce K values that satisfy Equation 6-3.