Given the viscosity of asphalt, its better to set up a feed spreader to cover the cross section of the tank. This will also improve mixing and reduce the time for homogenisation.
The thermal designer may have picked on a higher tubeside velocity at design flow here so that at turndown, phase stratification in the tubes is still not indicated.
For a pump to "stay at a good operating point", it must be operating at constant differential pressure. This then gives you constant flow. Presume this is what you are aiming for ?
Given that you have a varying level in the source tank, the simplest way to enable constant diff pressure is to...
That foot valve is a necessity in this case, but in the long run, it will turn out to be the weak link in this priming setup. If it is stuck / jammed in some intermediate position, the suction line will not prime. Foot valves fail to work as intended due to corrosion and or bio fouling.
Tube side material should resist corrosion from condensing liquid. With such materials, velocity at 18m/sec should be okay, provided there are no erosive solids suspended in the feedgas. Overall U in this case will be constrained by shellside htc, but watch out for tubeside pressure drop.
For thermal design of and pressure drop on tubeside in partial condensors, pls refer to page 11-12 in Perry Chem Engg Handbook 7th edn. You can do a manual check of the Aspen output with these correlations.
But in this case, the oxidant is already within the pipe, so I dont see what the FA will do to arrest the combustion. Besides, combustion can occur anywhere in the pipe where static could generate a spark.
It is a process design error to set unequal design T for shellside and tubeside in this case. But now that steam is to be permanently disconnected, it probably doesnt matter.
A PSV on shellside set at 24barg is still required to cater for tube rupture failure.
That RO is probably sized to prevent overloading this line with excess flow that could potentially rattle and shake this line off its supports, given line pressure is 700-800psig. So its not meant for operational throttling. Add a choke or needle valve either upstream or downstream of the...
They want DBB upstream of the critical ESDV so that the ESDV can be safely removed without having to depressure the entire upstream pipeline. Otherwise, the Plant Owner may be forced to consider risky alternatives, of which there are many. But I dont see an intermediate bleed.
The DN500 MOV is a...
You may wish to query the rational for these unusually large dia lines. Why is the max operating pressure only 1barg? Can you not allow for a higher operating pressure that will reduce line dia ? Or is there some limitation due to low design pressure of equipment connected to this flare system...
From what I see on Google ( search fake viton gasket), you may be using a generic FKM gasket, and not genuine Viton
"While the term "Viton" is often used interchangeably with FKM (fluoroelastomer), it's actually a trademark of Chemours Company. Therefore, there's no official "fake Viton"...
If your focus is on LPG production from natural gas, then do you need to produce a methane only stream from demethanizer as shown in diagram ? Instead, you can operate a de ethanizer without de methanizer, which will give you a sales gas stream with C1 and C2, while NGL will contain C3 and...
Google tells me atmospheric air cools down by an average of 0.65degC per 100metres rise in altitude, so this is the driving force for the natural convection effect.
There is an error in your warehouse height.
This should help
https://en.wikipedia.org/wiki/Stack_effect
See if this helps :
https://www.linkedin.com/pulse/diesel-fuel-return-line-bleed-back-mike-trumbature
My guess is this check valve requirement on "fuel supply pressure recycle return line to fuel tank" is valid only when BOTH of the following are applicable
a)the return line enters the fuel...
