I have the same feeling, the OP first post said "water, miscible and immiscible monomers (styrene, vinyl acetate, various acrylic polymers), and emulsifying surfactants." but then he proposed to consider components as immiscible...
That assumption can produce large errors and many authors (see...
as suggested by others, if you are not familiar with these calc's, probably a process engineer is the best option,
for these (simple) problems you can adopt many different tools (see previous posts) and procedures as data validation and reconciliation to compare measured values vs. simulated...
Victarion, if you know feed composition, temperature and pressure (the conditions at cooler / condesner outlet) there is only one possible "equilibrium" condition (i.e. gas, liquid or vapor + liquid , not considering non equilibrium) which you can estimate solving the so called isothermal flash...
if you know composition, operating temperature and pressure simply solve a isothermal flash to calculate the amount and compositions of vapor and condensate (at specified conditions, i.e. heat exchanger outlet), many tools allow to do that, for std. HC you may wish to select a EOS such as std...
yes, that is a possibility,
or you can solve n-times the column with different number of trays / parameters in order to identify the best configuration,
also, you may be interested to specify a range of operations for your column as suggested by georgeverghese.
with a simulator you can model an existing column or design a new column,
when modeling an existing column you wish to match the actual performance of column,
for that you can define ideal or real equilibrium stages (see my previous post) and change the number of trays or other parameters to...
I agree with don1980,
many authors as Kister (see for example the chapter Tray Efficiency Fundamentals in Distillation Design etc.) suggest to model stages with 100% efficiency, there are several correlations as Murphree and corrections for non-ideal equilibrium as amines etc. but in practice it...
the answer is generic about pump model available in most simulators (as for expander model)
since this is a chemical process engineering forum with contributes of CHEMCAD, PROII, VMGsim, Prode etc. users, you may expect responses from users of different software,
if you wish to limit responses...
if you have only liquid with similar densities an (equivalent) pump model (considering dH) should give reasonable values,
if you wish to model change of phase, dV etc. a compressor ( expander ) model is more appropriate,
for those cases I have a specific model in PRODE PROPERTIES (compressor &...
you can calculate cp, cv, speed of sound, compressibility etc. for liquids (as for gases),
however take care that results in some cases may show large errors (see previous posts)
see The Properties of gases and Liquids , chapter 6, Heat Capacities of Real gases (previously suggested),
cp = (dH/dT)p
cv = (dU/dT)v
there are different ways to calculate these values, a table of values, a EOS etc.
with a EOS you can calculate cp=(dH/dT)p , V , dV/dP , dV/dT
and finally cv
calculating the flash point (StrFLP method , model PRX, BIPs from Prode datatabase) for 80% C8 20% methanol, I get a value (about 273 K) which is below the flash points of pure fluids (stored in Prode database and in agreement with NFPA), is that normal ?
I have no data for this mixture (to...
if you wish to add a question better to open a different thread,
anyway, to use Prode (or a different simulator) as first step you must define the stream (list of components, fractions, thermo models etc.) then in nozzle.xls you define Tin, Pin, Pout and mass flow,
the program calculates the...
