Odds are your flanges are not CSA rated flanges, most times people do a spec break at the first flange above ground to make things simpler, and significantly cheaper, sure one or two planges and fittings built to CSA standards are not too bad, but you dont built much above ground pipeing thats...
I tend to treat tank coils as a cylinder in cross flow for heat transfer calculation, and then make sure i specify the coils so that they are at least 2D spaced center to center, prefferably 3, that is usually enough spacing to allow the simplification of just treating it as a single pipe for...
Hi Remp,
im at home and i dont have any of my notes and stuff to look anything up, so this is all from memory, but it still does not sound like a run away to me.
your talking a flow of 36 m3/h say you use two pumps each doing this service, we are talking maybe 10-20k each pump, with the motor...
Well i think the real question is would the plate exchanger really dot he job at a fraction of the cost?
typically, and i say typically cause i dont knwo all your flow rates and ahve not priced everythign out, but typically a pump is much cheaper capital cost than a plate and frame exchanger...
Hi Flycast,
Im not very familiar with thermoforming (read not at all) so im not quite sure what it is you are trying to do, but im going to give you a few pointers that might help you out without going into the calculations too much.
For reference though you should eb able to look up in a...
Grade 359 Cat II is not the same as A350 LF2.
Grade 359 means the SMYS of the material is 359 MPa, A350 LF2 has an SMYS of ~ 248 MPa, so it is a significantly weaker material and you would need a higher wall thickness to do the substitution.
For myself, i will say that there are arguments for both cases, pipelines are a whole matter entirely, but for process piping in a plant or such, ive seen it too many times where someone has gone no further than looking at the flanges in a system to decide what the max pressure of that system...
Sorry the formulas i gave were for external convection coefficients.
For the internal convection coefficient i use
Nu*k/ID
Nu = Nusselt NUmber
k = Thermal conductivity in W/m°K (Internal Fluid)
ID = Internal Diameter in meters
Sure, there is a simple way to approach this one, set up a thermal circuit, for simplicity i would just assume your steam to be a constant temperature fluid int he pipe, then you can either calculate or assume an internal convection coefficient. work out the conduction throught he pipe, and then...
I believe by MT he means Magnetic Particle Testing.
I know ive come to this late, but yeah id have gottent eh lawyers involved a long time ago, replace all the pipe that came from that supplier.
Ive worked in Offshore and i know the kind of service life that is expected in alot of this stuff...
An ANSI 150# flange is rated to a pressure of 285 PSI @ a temperature of up to 100°F. that means your design pressure can be a maximum of 285 PSI using 150# flanges, you then multiply this by 1.5 to get 472.5 PSI as the test pressure for a 150 ANSI system.
this is typically done at least in oil...
Jimmcmahon,
Im sure it is being done, and im sure you can do a ton of testing to make sure its all up to code, but the fact still remains that jsut because you can do it does not mean you should.
Its basically a colossal waste of money, you can get gaskets (albiet expensive ones) that will...
I agree with David, its pretty rare to have system that sensitive that you need ot purge with N2, but then if the client insists on it, it is at their cost, just make sure you let them know its an extra cost and not somethign thats typically done.
