The EDPV or BDV is the most crucial part of any high pressure separator used in Oil & Gas industry maybe in EPF or main production facility. Great video showing how to use HYSYS to simulate and obtain results according to old and new API 521. Very helpfull for all the Chemical Engineers both experienced and new.
Your videos are very nice. Your explanation and the way you present is awesome. I love your lectures so much and i never missed anyone. Thanks for sharing such a valuable information.
Hi Sir, first of all thanks for the excellent contribution. Kindly clarify the following doubts without any hesitation pls 1. How do u fix the vapor fraction for inlet stream as 0.5 & Why dont we provide temperature rather than vapor fraction for fire case scenario ? If we can provide temperature what shall be taken as basis ? 2. What is the source of value for orifice co-efficient? 3. How do we determine the volumetric flow rate (For both pipeline & vessel) to run the simulation ? Your positive reply will be highly helpful sir . Thanks once again.
Thanks a lot sir 🙏 It is very informative. I want to know there are three options available in Hysys in blowdown and depressuring section 1) Blowdown 2)Depressuring 3) Staggered blowdown Which one is use for which case? Beacause we can do Adiabatic or fire depressuring in 1 as well as 2 case also.
Hi Ajay, Thanks for the video. I just wanted to ask that for fire case depressuring why do you take the max operating temperature for dynamic depressuring utility and not the fire case temperature. Kindly respond
Perhaps, you need a formal training on process design with simulation software. :) www.converge.net.in You might want to check the above site. Thx. Ajay
Hi, HYSYS provides Orifice upstream and downstream temperatures. Did you solve this example on your own? If yes, then I believe you already know the answer to your question. :) Thx. Ajay
The statement about vapor depressuring rate as per new API rule as on date is not correct in the video. As per API Standard 521 seventh edition(June 2020, Errata 1, Nov. 2022) section 4.6.6 " For pool fire exposure, this generally involves reducing the equipment pressure from initial conditions to a level equivalent to 50 % of the vessel’s design pressure within approximately 15 min. This criterion is based on the vessel wall temperature versus stress to rupture and applies generally to carbon steel vessels with a wall thickness of approximately 25.4 mm (1 in.) or more. ..... Depressuring to a gauge pressure of 690 kPa (100 psi) in 15 min is commonly considered when the depressuring system is designed to reduce the consequences from a vessel leak or failure. This criterion is also commonly applied for both fire and leak scenarios." Please check and confirm.
Hi, Thanks for your message. I have re-checked my ppt w.r.to your comment and found that we both are right. Could you please explain which statement of mine in the video you do not agree with? If you prefer, we can have a WhatsApp call (+91 9867328748). Thx. Ajay
Thank you for this valuable lecture
The EDPV or BDV is the most crucial part of any high pressure separator used in Oil & Gas industry maybe in EPF or main production facility. Great video showing how to use HYSYS to simulate and obtain results according to old and new API 521. Very helpfull for all the Chemical Engineers both experienced and new.
Thank you!
Your videos are very nice. Your explanation and the way you present is awesome. I love your lectures so much and i never missed anyone. Thanks for sharing such a valuable information.
I happened to be a teacher. In case you want to learn about plant design with simulation software, you can check www.converge.net.in.
Thx.
Ajay
Hi Sir, first of all thanks for the excellent contribution. Kindly clarify the following doubts without any hesitation pls
1. How do u fix the vapor fraction for inlet stream as 0.5 & Why dont we provide temperature rather than vapor fraction for fire case scenario ? If we can provide temperature what shall be taken as basis ?
2. What is the source of value for orifice co-efficient?
3. How do we determine the volumetric flow rate (For both pipeline & vessel) to run the simulation ?
Your positive reply will be highly helpful sir .
Thanks once again.
Hey, sorry for the late reply.
Did you Google in these 4 weeks?
@ajaysatputeNerul S of course. But I am unable to get the exact solutions
Thank you for the explanation. This helped me!
Thx.
Ajay
Thanks a lot, sir 🙏 It is very informative. I hope to learn more from you and use them to find solutions in real plant studies.
Thank you!!!
nice one.very helpful
Thx. :)
Very informative
Thank you Sir!!!
Thanks a lot sir 🙏 It is very informative.
I want to know there are three options available in Hysys in blowdown and depressuring section
1) Blowdown
2)Depressuring
3) Staggered blowdown
Which one is use for which case?
Beacause we can do Adiabatic or fire depressuring in 1 as well as 2 case also.
Perhaps, that's for you to explore yourself. :)
Very useful
Thx. :)
Nice lecture delivery
Thx. :)
Hi Ajay, Thanks for the video. I just wanted to ask that for fire case depressuring why do you take the max operating temperature for dynamic depressuring utility and not the fire case temperature. Kindly respond
Well, it is as per ADNOC standard for "Flare System Design Basis" (doc. no. DGS 0180 002 Rev 1).
Hi sir, Good morning. I am newer to use Aspen hysys. I have one doubt sir. U said that about wall thickness and length. How should we consider it sir
Perhaps, you need a formal training on process design with simulation software. :)
www.converge.net.in
You might want to check the above site.
Thx.
Ajay
Dear Sr, why at the minute 13:30, we cannot see the temperature at the Orifice? Is it possible to calculate? Can you explain us, how to do? Thank you!
Hi,
HYSYS provides Orifice upstream and downstream temperatures.
Did you solve this example on your own? If yes, then I believe you already know the answer to your question. :)
Thx.
Ajay
hello sir, for adiabatic case you use PAHH as inlet pressure to vessel. what basis do you use for inlet temperature? can we use TAHH as the basis?
Maximum Operating Temperature can be used. You might want to check the results with TAH & TAHH and decide which case gives more conservative results.
please put up a video on PSV sizing for blocked, overfilling and fire case scenario
If I put everything on CZcams then who will come to attend my process design course? 😁
Sir, for adiabetic case why PAHH pressure is used? Why not operating pressure?
Hi,
It would provide more conservative results.
And also because ADNOC follows this and we do their projects. 😄
Hello sir. How about if we want to do BDV on pipeline? Meaning that the BDV is not attached to the vessel
Same procedure.
I can not find the requirement about how large of Vessel need to be depressurized. Could you help me?
Do you have any specific query related to your project?
Which property package is used for this problem?
PR
The statement about vapor depressuring rate as per new API rule as on date is not correct in the video. As per API Standard 521 seventh edition(June 2020, Errata 1, Nov. 2022) section 4.6.6 " For pool fire exposure, this generally involves reducing the equipment pressure from initial conditions to a level equivalent to 50 % of the vessel’s design pressure within approximately 15 min. This criterion is based on the vessel wall temperature versus stress to rupture and applies generally to carbon steel vessels with a wall thickness of approximately 25.4 mm (1 in.) or more. ..... Depressuring to a gauge pressure of 690 kPa (100 psi) in 15 min is commonly considered when the depressuring system is designed to reduce the consequences from a vessel leak or failure. This criterion is also commonly applied for both fire and leak scenarios." Please check and confirm.
Hi,
Thanks for your message.
I have re-checked my ppt w.r.to your comment and found that we both are right.
Could you please explain which statement of mine in the video you do not agree with?
If you prefer, we can have a WhatsApp call (+91 9867328748).
Thx.
Ajay