Thanks for the feedback so far..the question I am interested in is the concern with running air through a machine contaminated with lube oil and heating the oil in the casing which could coke out, char or combust --if the oil flash point is higher than the maximum heat of compression.. Would...
I was reviewing a few really top questions related to NACE and valves and well composed/experienced loaded responses by rneill, SJones and Thomas. Would especially appreciate feedback and guidance on this argument over interpretation inside NACE - trying to bottom out.
Reference to ISO 15156...
I appreciate by design dry screw machines in theory should avoid lube oil contamination into the process gas side/casing or importantly contamination of the lube oil from the process gas. However this depends on the seal system and barriers in place, barriers can be breached and propensity for...
I am trying to get feedback from the wider industry on the basis/philosophy considered/used for establishing the leakage rate back through check valves in view of calcualting required relief valve size to protect the upstream section the check valve is leaking into, this is specifically the case...
For ball valve seat material selection can someone advise if there is a selection criteria to allow one to assess the acceptability of coatings for erosion resistance such as RTFE for given concentration of particulates in a fluid that the valve or material may be exposed to.
Specifically to...
For ball valve seat material selection can someone advise where one would be able to verify the definition of "sandy service" in terms of what constitutes sandy service.
Is this
. Quantified sand concentration with particle sizes greater than a certain diameter
. Percentage volume sand with...
Just to clarify my understanding, when ASME updated the code on hydrotest pressure ratio to specify the minimum requirement of 1.3 what was the logic behind selecting 1.3 as the ratio, i recognise this is the minimum requirement and also that no upper limit for hydro is advised but what...
ultrasonic have no chance with boiling fluids like unstabilized crude, or crudes with small gas bubbles mechanically entrained exiting the primary separators--- as most oil facilities operate with at 2 to 3 stages of separation I am curious why more often of not US have been applied and get bad...
JL thanks for your feedback - answers to your questions embedded- I am thinking a strap on ultrasonic or two may work for us. Another constraint is allowable pressure drop for the meter and I will avoid orifices
thanks
compo
a:I assume that the flare line is SSt with lots of straight run...
Appreciate any feedback on flow meter selection types, configuration and suppliers who have the capabilty to accurately measure hydrocarbon gas predomin. methane MW (18-20) over a wide temperature range and specifically at the cold end- gas temperatures range from -80 to upper end 100degC. The...
Appreciate any feedback on flow meter selection types and suppliers who have the capabilty to accurately measure hydrocarbon gas predomin. methane over a wide temperature range and specifically at the cold end- gas temperatures range from -80 to -100degC, upper end 100degC. The application is...
Appreciate the feedback. Chris can you provide more information on your water cut meter application i.e. is it dealing with a heavy crude or emulsions?
We are seeking operational feedback on level instrument and water cut meter manufacturers and specific technology that has been applied successfully in the field for crude oil water emulsion interface detection and outlet oil water cut metering for 3 phase production and test separators. The...
We are seeking operational feedback on level instrument and water cut meter manufacturers and specific technology that has been applied successfully in the field for crude oil water emulsion interface detection and outlet oil water cut metering for 3 phase production and test separators. The...
Offshore crude oil processing. Does anyone have any actual operating experience good or bad of installing a heat exchanger at the front end of the crude stabilisation process, basically heating oil/produced water and associated gas (upstream of the primary separator/slug catcher).
