Thanks Mr. Eke for this great video and so much appreciated. Q) suppose we have crude oil with its associated gas inside the tank and the level is at low low liquid level. In this case should ZV be installed upstream the pump to avoid gas blow by scenario and to avoid any process upset in downstream equipment or do you think pump level switch will be enough by tripping the pump? Your answer is highly appreciated.
Thank you Mr Mohammad. I forget to add that the crude is stabilized crude and entrained gas would be vented to the atmosphere. Upstream to the storage tank, separation of gas and liquid would have occurred at HP Separator, LP Separator where the separated gas would have been routed to a Knockout Drum.
Thanks for your video. I have the following problem: when I simulate a dynamic state, the pressure drop through the gas valve becomes lower than zero, and instead of the level to decrease, it increases. Do you know what could happen?
Thanks Mr Eke, for this video, It's a great education job. I have the following doubts: - The dynamic viscosity 3.264 cP isn't equal to 0.0022 lb-s/pie2 like appears in the oil viscosity data, it is? - Could you send me the oil's assay? - Why do you put a Cv of 5000 for the valve? I appreciate your response Regards
Dear Miguel Cruz I appreciate your comment and observation. With reference to API 14e, there is formula for converting Dynamic viscosity from cP to lb. The Cv of the valve was given the stated value in order to satisfy dynamic simulation mode. Atmospheric Storage tank is not the same as Separator at the gas outlet
the pipe roughness in the spreadsheet is 0.0018 meanwhile in the pipe simulation is considered 0.00015, this make change the Total Head calculated at the beginning.
tks for this video sir ........ in pump curve both the head and the flow rate increase simultaniously!!!
Thanks you for your learning
Good work sir.
thanks, its so good
Another question is when I Run dynamic mode tank level start to increase instead of decrease, what action i have to do to make level down
Thanks Mr. Eke for this great video and so much appreciated.
Q) suppose we have crude oil with its associated gas inside the tank and the level is at low low liquid level. In this case should ZV be installed upstream the pump to avoid gas blow by scenario and to avoid any process upset in downstream equipment or do you think pump level switch will be enough by tripping the pump?
Your answer is highly appreciated.
Thank you Mr Mohammad.
I forget to add that the crude is stabilized crude and entrained gas would be vented to the atmosphere.
Upstream to the storage tank, separation of gas and liquid would have occurred at HP Separator, LP Separator where the separated gas would have been routed to a Knockout Drum.
Hello sir, please can you share with me table A-1a typical size and corresponding nominal capacities for tank
at 16.06 min it sates that tak diameter is 15 mt and 14.4mt ht but in simulation it is given as 6mt dia and 5.4 mt dia please can you clarify
Can we calculate dp/dt in pipe line in hysys
Thanks for your video. I have the following problem: when I simulate a dynamic state, the pressure drop through the gas valve becomes lower than zero, and instead of the level to decrease, it increases. Do you know what could happen?
Send me the hysys case so that I can study and response to your challenge
@@kingsleyeke6790 ok I have alreade sent it to your gmail thank you
Feed stream composition??
Geat job, can you provide the excel calculation file please, thanks
Excellent video. Please send an excel calculation file
witch software used to specified the pump
Thanks Mr Eke, for this video, It's a great education job.
I have the following doubts:
- The dynamic viscosity 3.264 cP isn't equal to 0.0022 lb-s/pie2 like appears in the oil viscosity data, it is?
- Could you send me the oil's assay?
- Why do you put a Cv of 5000 for the valve?
I appreciate your response
Regards
Dear Miguel Cruz I appreciate your comment and observation. With reference to API 14e, there is formula for converting Dynamic viscosity from cP to lb.
The Cv of the valve was given the stated value in order to satisfy dynamic simulation mode. Atmospheric Storage tank is not the same as Separator at the gas outlet
@@kingsleyeke6790 I ppreciate your answer. Thanks!
the pipe roughness in the spreadsheet is 0.0018 meanwhile in the pipe simulation is considered 0.00015, this make change the Total Head calculated at the beginning.
@@MiguelCruz-tl2rv 0.0018ft = 0.00015Inches
The centrifugal pump curve should be parabola, the low flowrate should have a higher head.
Why can't I play this video on speed mode? I mean 1.5x speed