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Thank you.

for example if i have 50% butane and 50% hexane (by volume) at 50psia and 200F the properties of hexane at these conditions are partial pressure of 25psi with a saturation pressure of 30.1psi and for butane partial press of 25psi and sat press of 193.7psi. now if this gas mixture is flowing...

is it true that if you have a hydrocarbon gas mixture and cool it down enough at constant pressure only certain gas components will start condensing (at their sat temp for their partial pressure) and not the entire gas mixture for a certain specific temperature? i hope this makes sense.

does anyone have any experience on the above situation with an compressure producing a two gas mixtue at a certain pressure and temp then running through an aftercooler where one gas is condensed to a liquid. specifically do you see constant pressure (neglecting inherent pressure drop of heat...

im sorry that was a bad hypothetical. say we have a typical aftercooler for a gas compressor. and that the system is at 100 PSIA and the two gasses enter at 300F and are cooled to 100F, and the first gas condenses to a liquid at 200F. would the second gas stay at 30PSIA and bring the entire...

im sorry, i see now, i did have it backwards thanks. if there are two gasses in a pressurizd container that reads 100 PSIA. and hypothetically we introduce both at once with one gas at a partial pressure of 70 PSIA and the other a partial presssure at 30 PSIA. and still hypothetically the first...

anythoughts on the relation to the pump? ie discharge or suction side?

Is it correct that if the saturation pressure is less than the partial pressure of a gas then that gas exists in a vapor state. and if the saturation pressure is greater than the partial pressure tha that gas exists in a liquid state?

I've seen some references saying the cold side since it has a lower pressur and installing on hot side shortens life of diaphram expansion tank??? vpl? do you know reasonings for the above placement?

Where are expansion tanks typically placed in a closed system? hot side or cold side? any one have good rules of thumb for placement of diaphragm expansion tanks in a system containing a pump, heat source, and heat exchanger? thank you.

thanks everyone, is there any reason in paticular as to why not control pressure with isolation valve?

would anyone suggest using an isolation valve at a pump discharge as a means of controlling operating pressure in a closed system

...or does it consider static pressure? I guesse now i can just pose my question as to how is the 'operating pressure' calculated?

Its a coolant system that the water/glycol is pumped through something to cool it down, and there by heating up the glycol, and then through an air cooled heat exchanger to cool the glycol back down. Its a closed loop system. temperature is a concern, since the ambient air changes, should i be...

thanks ione, one last time tho just so I know whats going on. The term that i hear all the time of the 'operating pressure' of the system at the discharge side of the pump can be calculated by pv^2/2 (which is also called the dynamic head?)

drweig i think you misunderstood my post i am asking what is typically controled by a control panel in this situation. The very generic situation being "closed loop water/glycol systems with a centrifugal pump and a heat exchanger. the water/glycol will be pumped through the system and heated...

ok ione, that makes sence. But what if I have a certain configuration (ie TDH of 100ft) and a certain pump (ie 30gpm at 100ft) and i want my flow to decrease to 20gpm. how would i do that? vfd?

I am just looking for general information on control panels for closed loop water/glycol systems with a centrifugal pump and a heat exchanger. the water/glycol will be pumped through the system and heated up and then cooled back down with heat exchanger, etc. Now i am assuming the control...

ione, So in your example the total dynamic head is calculated and can that be then used in pump diagram that gives tdh versus flow rate. Then for example if this particular diagram says that for a tdh of 100ft, from the example, there is a flow rate of 30gpm. Then the pump will be producing...

I have graph for a pump that shows the flow rate versus a lot of different values. one of those values is the total head (labeled T.D.H.). So if I assume that i have flow rate of 30 gpm this coincides with a TDH of 130ft. Now to figure the operating pressure of my liquid at the pump discharg...