if you solve with Lee Kesler method results will be quite close to those reported in the book,
I agree with Pierreick and gergeverghese, your compressibility factors / densities are wrong,
I attach the solution calculated in Excel with Prode Properties (see prode.com) for your review...
probably it depends from selected thermodynamic package for enthalpy calc's...
for accurate results you should select ASME or IAPWS (95, the most accurate, or 97) these models however work only with pure fluids (not mixtures),
not sure about the models Aspen includes,
with Prode Properties I...
MIANCH,
is that a copy and paste from Aspen documentation ?
Yes, you can estimate Rvp with many different EOS models (at least that is possible with Prode Properties, I would presume with Aspen, too).
Yes, you can correlate ASTM D6377 with ASTM D323 etc. , there are graphs and correlations for...
according API TDB the Reid vapor pressure (Rvp) is the absolute pressure exerted by a mixture (in psi) determided at 100 F and at a feed vapor to liquid volume ratio of 4 (see ASTM D 323 for details about apparatus and procedures, that is important to understand what Rvp means...),
a software...
>>Any books on sour water stripping process chemistry and unit operation are available..please share them
many books available but you may start from original paper : "A New Correlationof NH3, CO2, and H2S Volatility Data from Aqueous Sour Water Systems" which includes a discussion on the...
for a binary you may be able to fit (with a VLE data-regression procedure) experimental VLE data in some (maybe limited) range but standard Peng Robinson may show several limits... a more suitable approach could be, for example, a EOS with complex rules (i.e. Peng Robinson + NRTL with Huron...
probably your manufacturer can propose the right tool (the reason being that there are many specific factors as valve's internals etc. which can affect results in complex models as for example non-homogeneous, non-equilibrium models)
said that, there are many tools available and, since you...
in standard Peng Robinson EOS, BIPs (Binary Interaction Parameters) are included in van der Waals mixing rules as fixed values calculated by data regression of Vapor-Liquid experimental data values (see Dechema),
if you wish to fit VLE data (fugacity calculated by EOS) any data regeression...
for phase equilibria one can solve fg(1)*x(1)=fg(2)*x(2)=... where fg and x are the component's fugacities and fractions in the different phases (vapor, liquid, solid...)
it shouldn't be too difficult for vapor-liquid assuming for example ideal state laws (i.e. vapor pressure for liquids and...
Pulsater555,
for models based on ideal gas laws the generic correlations of H vs. T (from which you can extract (dH/dT)P or cp) are ok,
for real fluids you should include departures (from ideal fluids) calculated with EOS or equivalent systems,
see the previous threads at Eng-tips forums.
the method in API 5.5.10 is based on the (simplified) omega formulation, these formulations dates back to 1980 when not many computer codes were available (see attached paper)
In recent editions API suggests a procedure based on numerical integration for nozzles (see my previous post with the...
as far as I know API formulation adopts an approximate analytical approach based on isenthalpic approximation and omega one parameter equation (see Leung papers for details),
as alternative you can adopt numerical integration (solving many small steps) with the formulations in my previous post...
if I remember correctly they proposed different versions, the oldest being quite simple.
The homogeneous model treats the two-phase mixture as a single fluid at phase equilibrium (no slip).
The (homogeneous) volume is defined as vm = X*vg + (1-X)*vl where X is the weight-flow...
for additional details about the correlation proposed in API 5.5.10 you may refer to the paper "The Discharge of Two-phase Flashing Flow in a Horizontal Duct" by Leung and Grolmes
as alternative you may consider the method based on HEM approach discussed in Emergency Relief System Design Using...
with sub-cooled liquids HEM model could give conservative results (compared for example with HNE-DS which includes a boiling delay), depending from operating point,
anyway you should be able to solve with the help of steam tables.
Another possibility, as said, could be to use a thermodynamic...
which is the purpose of your work ?
If you wish to learn how it works probably the numerical examples included in standards / books / etc. could help,
differently, if you wish to code a procedure a thermodynamic library (see my previous post) or a process simulator could help by solving the...
The Omega method proposed by Leung adopted a single point (pressure vs volume) to determine a compressibility coefficient ω "found to be a unique function of the stagnation pressure for a given fluid", note that first part of process is isentropic, second part is isenthalpic and one can...
in principle many thermodynamic models including cubic EOS (Soave, Peng-Robinson ...), corresponding states (Lee-Kesler...) etc. can predict multiple liquid phases...
but it could also depend from some numerical instability in the solver (Lee-Kesler has multiple roots) and so on...
I am not...
they define x0 as the mass flow quality, i.e. the ratio of the gas mass flow rate to the total mass flow rate of a two-phase mixture, if you know total volume (of vessel, see also the definition of V) and (vapor and liquid) volumes you should be able to get x0 value,
the paper presents a...
there are no examples for E0 = 1-Vl/V where V ?
however they say that x0 is the mass flow quality at sizing conditions, i.e. the gas mass flow rate related to the total mass flow rate of a two-phase mixture, adding that mean value of the specific volume of the homogeneous two-phase mixture at...
