Does anybody know of a site that has the Kern method friction factor plot on it. I cant seem to find it, and the one in the book I have is so worn that I can not read the plot anymore.
The original Documents are messed, and Im looking to calculate this at variable flow rates, so we have a trend on the pressure drop vs flow rate. And unfortunately there is no pressure instrumentation.
I have an exchanger that has 8 baffles, a shell ID of 44" and tubes in the triangular arrangement (15/16" pitch).
I need to know how I can calculate the pressure drop over the shell of this exchanger, if I know the temperatures, flow rate, viscosity and density of the fluid.
This is the...
The tube side outlet will get hotter if its flow is reduced (all other things remaining constant). This is just based on the overal time that the two fluids will be in contact for.
The simple explanation is that the longer the two streams stay in contact with each other, the closer they will...
there are no none condensable gasses in this stream. So that is not a problem. All of the vapour in the stream comes from the crude feed, which is already purged of all non-condensables before it is feed into the unit.
My program has been able to predict the run length for the first series of exchangers in this pre-heat train thus far, using only the U factor ... so just for that it is worth it.
Your right i have no experiance sizing exchangers. And im not trying to size the exchangers, im trying to track the fouling of these exchangers using the U factor. But i have 4 out of the 20 exchangers which end up being condensers on the shell side (although this is not the original design or...
The oil is flowing through these pipes at 900 k#/hr, which makes this flow extremely turbulent (8" - 16" pipes).
And unfortunately, the previous people who have tried this, assumed that the viscosity of crude was constant over the temperature range, and used the old values (from early 70s)...
We pump the oil from a tank that is at ambient conditions. which right now can be anywhere from -10 to 10 deg C. and the process is suppossed to bring the oil up to about 248 deg C, before it goes into the heaters.
This is all done using the products off of the distil. tower, so we dont have...
The feed gets flashed when its about 200 C, so in all of the exchangers that im looking at, this is a completely liquid feed, all the way up to 247 C.
And the pre-flash was a later addition to the plant, and was fit into an area were there is space, that is why it was put so late in the...
This is the preheat section of the an ethylene plant. The system does not go into two phases until after a flash drum, in which the temperature is somewhere around 200 C. We need the high temp to be able to 'distil' the naptha and 2 oil off of the crude.
Im interested in a little bit of a larger temperauter range though. My temps go anywhere from 35 F to 477 F in the area im looking at. So my lab cant exactly give me the whole scale for me. If i use them im going to have to extrapolate the data to fit the curve to my temps.
Ashereng
I am using pressure drops to estimate the flow. But the equations require the use of Reynolds number, which requires the viscosity of the substance. Im starting to think that our lab is going to be getting a little more work soon. I might have them make a correlation on the crude and...
All i need is something that will give me a close estimate to the viscosity. Im trying to determine flows in parrallel lines, but the only flow meter on the lines comes before the split into the lines. An estimate of the viscosity will help me determine the flows.
