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...
Typically, this piping stress ratio route to allowing some exceedence on lower design temp is not used, since the actual stresses whilst in operation may well exceed what you compute in the design office. Since this is a marginal exceedence, see if the process engineer can calculate a higher...
Self venting gravity flow lines are typically sized to keep the Froude number N_Fr < 0.31 (in SI units). See equation 6-138 in Perry Chem Engg Handbook (7th edn) for N_Fr expression which accounts for liquids with density other than water - there is no viscosity term here though, so maybe keep...
Avoid high or low point piping pockets in the return lines to the main oil tank - all return lines should be free venting so entrained air or process gas doesnt get trapped at these pockets. Hydraulic flow equations wont help if these lines are pocketed.
We've not configured a backup supply for flare pilot FG for many installations. But the design requirements were to accommodate the short term safe venting of flare gas (max continuous normal operating case only) for all normal range wind speeds and stability classes in the event of accidental...
Speak to the folks at Norton or Koch in the USA who manufacture all sorts of packing for absorber / stripper columns. I dont seem to see Norton USA on Google - its all contaminated with links to China companies.
If this corrosion is internal, then you will have the same problems with above ground lines as with the old underground lines. Got salty water in these fuel grades at the source tanks ?
The quoted "min Cv" in that table of 11 for the 12inch valve implies a rangeability which far exceeds the typical value of 30, since 1875/11 = 170. Hence I would interpret the min Cv of 11 as being that for mechanical integrity and not for controllability - see footnote to those tables.
Hence...
Sizing control valves for the min flow case is an integral part of control valve selection, and often overlooked by process and instrumentation engineers. The end result is not good if ignored - poor controllability at low flow resulting in frequent shutdowns / unsafe operating conditions /...
