Page 318 - Characterization and Properties of Petroleum Fractions - M.R. Riazi

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June 22, 2007
AT029-07
AT029-Manual
298 CHARACTERIZATION AND PROPERTIES OF PETROLEUM FRACTIONS
vap Change in value of a property due to vaporiza-
at 1 atm and 60 F)
tion AT029-Manual-v7.cls T1: IML 17:40 stb Stock tank barrel (unit for volume of liquid oil
◦
S Value of a property at solid phase TVP True vapor pressure
sat Value of a property at saturation pressure VABP Volume average boiling point defined by Eq.
sub Value of a property at sublimation pressure (3.3)
[] (0) A dimensionless term in a generalized correla- %AAD Average absolute deviation percentage defined
tion for a property of simple fluids by Eq. (2.135)
[] (1) A dimensionless term in a generalized correla- %AD Absolute deviation percentage defined by Eq.
tion for a property of acentric fluids (2.134)
◦ Value of a property at low pressure (ideal gas wt% Weight percent
state) condition at a given temperature
THE LAST THREE CHAPTERS of this book deal with application
Subscripts of methods presented in previous chapters to estimate var-
ious thermodynamic, physical, and transport properties of
A Value of a property for component A petroleum fractions. In this chapter, various methods for pre-
B Value of a property for component B diction of physical and thermodynamic properties of pure
b Value of a property at the normal boiling point hydrocarbons and their mixtures, petroleum fractions, crude
c Value of a property at the critical point oils, natural gases, and reservoir fluids are presented. As it was
i, j Value of a property for component i or j in a discussed in Chapters 5 and 6, properties of gases may be esti-
mixture mated more accurately than properties of liquids. Theoretical
L Value of a property for liquid phase methods of Chapters 5 and 6 for estimation of thermophysical
m Molar property (quantity per unit mole) properties generally can be applied to both liquids and gases;
m Mixture property however, more accurate properties can be predicted through
mix Value of a property for a mixture empirical correlations particularly developed for liquids.
nbp Value of a liquid phase property at the normal When these correlations are developed with some theoretical
boiling point of a substance basis, they are more accurate and have wider range of appli-
--`,```,`,``````,`,````,```,,-`-`,,`,,`,`,,`---
pc Pseudocritical property cations. In this chapter some of these semitheoretical corre-
r Reduced property lations are presented. Methods presented in Chapters 5 and 6
ref Value of a property at the reference state can be used to estimate properties such as density, enthalpy,
S Value of a property at the solid phase heat capacity, heat of vaporization, and vapor pressure.
S Value of a property for solvent (LMP) Characterization methods of Chapters 2–4 are used to de-
s Specific property (quantity per unit mass) termine the input parameters needed for various predictive
T Values of property at temperature T methods. One important part of this chapter is prediction of
tp Value of a property at the triple point vapor pressure that is needed for vapor–liquid equilibrium
W Values of a property for water calculations of Chapter 9.
20 Values of property at 20 C
◦
7+ Values of a property for C 7+ fraction of an oil
7.1 GENERAL APPROACH FOR
Acronyms
PREDICTION OF THERMOPHYSICAL
API-TDB American Petroleum Institute—Technical Data PROPERTIES OF PETROLEUM FRACTIONS
Book (see Ref. [9]) AND DEFINED HYDROCARBON MIXTURES
BIP Binary interaction parameter
COSTALD Corresponding State Liquid Density (given by Finding reliable values for inadequate or missing physical
Eq. 5.130) properties is the key to a successful simulation, which de-
DIPPR Design Institute for Physical Property Data (see pends on the selection of correct estimation method [1]. In
Ref. [10]) Chapters 5 and 6 theoretically developed methods for calcu-
EOS Equation of state lation of physical and thermodynamic properties of hydro-
GC Generalized correlation carbon fluids were presented. Parameters involved in these
HHV Higher heating value methods were mainly based on properties of pure com-
LHV Lower heating value pounds. Methods developed based on corresponding states
MB Maxwell and Bonnell (see Eqs. (3.29), (3.30), approaches or complex equations of state usually predict
and (7.20)–(7.22)) the properties more accurately than those based on cubic
RVP Reid vapor pressure EOSs. For the purpose of property calculations, fluids can
PR Peng–Robinson EOS (see Eq. 5.39) be divided into gases and liquids and each group is fur-
PNA Paraffins, naphthenes, aromatics content of a ther divided into two categories of pure components and
petroleum fraction mixtures. Furthermore, fluid mixtures are divided into two
PVT Pressure–volume–temperature categories of defined and undefined mixtures. Examples of
SRK Soave–Redlich–Kwong EOS given by Eq. defined mixtures are hydrocarbon mixtures with a known
(5.38) and parameters in Table 5.1 composition, reservoir fluids with known compositions up to
scf Standard cubic foot (unit for volume of gas at C 6 , and pseudocompounds of the C 7+ fraction. Also petroleum
1 atm and 60 F) fractions expressed in terms of several pseudocomponents
◦

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