Page 357 - Characterization and Properties of Petroleum Fractions - M.R. Riazi

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8. APPLICATIONS: ESTIMATION OF TRANSPORT PROPERTIES 337
API No. Compound A June 22, 2007 TABLE 8.2—(Continued) D E T min ,K T max ,K
C
B
375 n-Nonylbenzene −1.0510E+02 6.1272E+03 1.3820E+01 −2.8910E−27 1.0000E+01 360 555
376 n-Decylbenzene −1.0710E+02 6.3311E+03 1.4080E+01 −2.7260E−27 1.0000E+01 253 571
377 n-Undecylbenzene −1.0260E+02 6.2200E+03 1.3380E+01 −2.4450E−27 1.0000E+01 258 587 --`,```,`,``````,`,````,```,,-`-`,,`,,`,`,,`---
378 n-Dodecylbenzene −8.8250E+01 5.6472E+03 1.1230E+01 −1.8200E−27 1.0000E+01 268 601
379 n-Tridecylbenzene −4.5740E+01 3.6870E+03 4.9450E+00 −5.8391E−28 1.0000E+01 328 614
383 Cyclohexylbenzene −4.3530E+00 1.4700E+03 −1.1600E+00 0.0000E+00 0.0000E+00 280 513
386 Styrene −2.2670E+01 1.7580E+03 1.6700E+00 0.0000E+00 0.0000E+00 243 418
342 Cumene −2.4962E+01 1.8079E+03 2.0556E+00 0.0000E+00 0.0000E+00 200 400
Diaromatics and condensed rings
427 Naphthalene −1.9310E+01 1.8230E+03 1.2180E+00 0.0000E+00 0.0000E+00 353 633
472 Acenaphthene 2.0430E+01 1.0380E+02 −4.6070E+00 0.0000E+00 0.0000E+00 367 551
473 Fluorene 4.1850E+00 7.2328E+02 −2.1490E+00 0.0000E+00 0.0000E+00 388 571
474 Anthracene −2.7430E+02 2.1060E+04 3.6180E+01 0.0000E+00 0.0000E+00 489 595
709 Methanol 1.2135E+04 1.7890E+03 2.0690E+04 0.0000E+00 0.0000E+00 176 338
710 Ethanol 7.8750E+00 7.8200E+02 −3.0420E+00 0.0000E+00 0.0000E+00 200 440
to use Eq. (3.105) by calculating blending index of the mix- More recently a corresponding state correlation similar to
ture. The viscosity-blending index can be calculated from the this equation was proposed for estimation of viscosity of hy-
following relation proposed by Chevron Research Company drocarbon fluids at elevated pressures in which the reduced
[19]: molar refraction (parameter r defined by Eq. 5.129) was used
instead of ω [20]. Parameters [μ r ] (0) and [μ r ] (1) have been
log ν
10
BI vis = correlated to T r and P r . Results show that for hydrocarbon
(8.20) 3 + log ν systems, parameter ω can be replaced by r in the correspond-
10

BI mix = x vi BI i ing states correlations. Such correlations have higher power
of extrapolation to heavier hydrocarbons. Moreover, param-
in which ν is the kinematic viscosity in cSt. Once ν is de- eter r can be accurately calculated for heavy petroleum frac-
termined absolute viscosity of a petroleum fraction can be tions and undefined hydrocarbon mixtures as discussed in
estimated from density (μ = ρ × ν). It should be noted that Section 5.9.
Eqs. (2.128)–(2.130) or Eqs. (8.19) and (8.20) are not suitable Equation (8.21) is recommended for low-molecular-weight
for pure hydrocarbons. hydrocarbons [5]. For such systems, Jossi’s correlation
To consider the effect of pressure on liquid viscosity of (Eq. 8.12) can also be used for calculation of viscosity of high-
hydrocarbons, the three-parameter corresponding states pressure liquids. However, this approach is not appropriate
correlations may be used for prediction of viscosity of high- for heavy or high-molecular-weight liquid hydrocarbons and
pressure liquids [5]:
their mixtures. For such liquids the Kouzel correlation is rec-
μ (0) (1) ommended in the API-TDB [5]:
(8.21) μ r = = [μ r] + ω [μ r]
μ c

where [μ r ] (0) and [μ r ] (1) are functions of T r and P r . These func- (8.22) log 10 μ P = P − 1.0133 −1.48 + 5.86μ 0.181
a
tions are given in the API-TDB [5] in the form of polynomials μ a 10000
in terms of T r and P r with more than 70 numerical constants. where P is pressure in bar and μ a is low-pressure (1 atm) vis-
cosity at a given temperature in cp. μ P is the viscosity at pres-
sure P and given temperature in cp. The maximum pressure
10
n-Pentane for use in the above equation is about 1380 bar (∼20000 psi)
and average error is about 10% [5].
n-Decane
When a gas is dissolved in a pure or mixed liquid hydrocar-
n-Eicosane
bons viscosity of solution can be calculated from viscosity of
Cyclohexane gas-free hydrocarbon (μ a ) and gas-to-liquid ratio (GLR) using
Liquid Viscosity, cP Water the following relation [5]: 1/3 + 538.4 3
1
Benzene
1.651(GLR) + 137μ

μ m
a
=
1/3
0.1
(8.23) μ a μ a [137 + 4.891(GLR)] + 538.4
1.209 + log (μ m)

10
log μ T =−1.209 + 132.8
10 T − 178
◦
0.01 where both μ m and μ a are at 37.8 C (100 F) in cp and GLR is in
◦
3
3
200 300 400 500 600 700 m /m . μ T is the viscosity of solution at temperature T, where
T is in kelvin. This equation should not be used for pressures
Temperature, K
above 350 bar. If μ a at 37.8 C (100 F) is not available, it may
◦
◦
FIG. 8.2—Liquid viscosity of several compounds be estimated; however, if μ a at the same temperature at which
versus temperature at atmospheric pressure. μ is to be calculated is available then μ may be estimated from

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