LittleInch,
The requirement for the pressure drop in psv inlet line comes from ASME Section VIII, Div 1, Appendix M and API RP-520 Part II. non-recoverable losses are mainly the line frictional loss. Please note that the static pressure loss is not included. Though 3% of set pressure criteria...
Hi!
I have couple of questions regarding vacuum column overhead design:
1) How to calculate non-condensable gas for vacuum column overheads?
2) What is the criteria for sizing vacuum column overhead line?
I will really appreciate help on the questions above.
Prochem
Petro737,
Thank you very much for validating my understanding about these terms.
Although terms are basic but the concerns were raised due to similar terms used by the different disciplines.
I appreciate your inputs.
Regards,
Prochem
DerekLJ,
Do you have enough details for the pumps e.g. curves and driver detail?Is it a new installation?what is the arrangement for emergency shut-down?what is the service?Provide sufficient detail about your system.
I believe you may have VFD drivers for your pumps.
Regards,
prochem
salar1363,
You can not assume that your 100% liquid relief due to blocked flow will be higher than your vapour / two phase relief due to external fire some other scenario.Hence do not take it for granted.
Your instantaneous vapour / two phase relief may be higher than the sustained liquid...
salar 1363,
pleckner is absolutely right.Check your local regs and find out.If you fall within OSHA, its about time you reconsider your approach. Its not only about violation of the law, we as a designer/engineer have moral responsibility to assure the safety and integrety of the facility too...
pleckner,
Thanks for your comments. I red through those references already.Finally we have decided to use HEM method for two phase relief.
This is a critical relief. Calculating mass flux is not an issue but initial calc shows very high instanteneous relief rate.Which doesnt seem realistic...
CJKruger,
Thanks for your reply.
I also believe that method 1 is more sansible approach as there will be some vapor space above the liquid (saturated).will be generated after initial liquid relief due to volumetric expansion.
However one of my co-enginners believe that the PSV need to be...
Hi all,
I am calculating a relief load of a liquid full Desalter for a fire case. I have a specific concern about flashing liquid at the time of relief.My question is can I size the relief valve based on Vapor relief after considering initial liquid relif due to volumetric expansion of...
Petro0707,
" our desalters are designed for 25.5 API Crude mix.but even with 27 API Crude mix processing (of course crude is the mix of 8-10 crudes belnds depening on Economics,yield pattern etc..) we are not getting desired efficeincy specified by vendors in terms of salts and BS&W.How to face...
Friends,
I am a chemical engineer and have recently joined a pharmaceutical company.Although I know the concepts of cleaning validation, i would appreciate if you can provide me with some good resources ( readings/links) to start with.
Thanks
DownesB,
Check the following thread for the discussion.You can install VFDs on your pumps but not without considering all aspects of your individual case.
thread407-90212
thread237-94051
Friends,
A)UG-125, the wording implies that a pressure relief device does not need to be located directly on the vessel PROVIDED the source of the pressure in the vessel is external to the vessel can be controlled and is below the MAWP of the vessel at operating temperature.
B)For Heat...
