Steam moles
----------------- > 4
Carbon moles
Steam = H20 moler flow
Carbon = any hydrocarbon beside CO2
eg; if you have 3mol/hr of C2H6 = C moles = 3*2=6 mol/hr
and you need to sum all the hydrocarbon to have the Total C mol/hr
Hi Mike,
I bumped into your question during my forum search,
and it sounds familiar :-)
I found a nice paper (student thesis) that summaries Liquid/Liquid cyclone separation (hydrocarbon and Oil in particular)...
Sounds like you create a slug flow - I would move the mixing point before the valve (reduce the amount of flashing) but if you can't do that (pressure issues) I had a good experience with spraying cold fluid in a 2 phase separator vessel (similar to direct condensing)
Tell me if you need a draft.
Spectacle blind AKA figure-8 blank AKA Madka AKA scissor blind - Use the same pipe and valve flanges
-so your "skilled" engineer won’t open the solvent line on the maintenance guys.
-add a line in your check list to check them before starting up.
Check with your electrical/PLC engineer and see if he has a spare AO (analog output).
A control valve will give you more options.
- How many times you need to drain the tank?
120% of the Total flow or one spare
(if you have 5 PSV each will be 24% of the max flow)
One with a lower set-point is a nice trick to overcome small bumps, but you need to make sure that your vent line stay atmospheric (otherwise you will cause back pressure on the others)
On the thermodynamic side
The Plate Heat-exchange (PHE) have lower thermo-mass;
So if your process is fluctuate you won't get the dumping effect you get with a S&T
But since you already have one S&T HE you can use a second PHE (actually it will be better if the first one will be the PHE)...
