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Tube Rupture Relief


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#1 felderosfelder101021

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Posted 16 January 2025 - 08:51 AM

Hi all I am curious regarding the following,

If you have a system where the shell side design pressure is 300 psig and tube-side design pressure is 150 psig. Then the tube side fluid is cooling water and the shell side is condensing fluid (hydrocarbon). I'd like to know how would you approach this relief calculation?

Say the high-pressure or MOP of the shell-side can exceed the tube-side pressure. Can the PSV be sized as the liquid flashing of hydrocarbon on the tube-side (would that be conservative)? Or size it based on the overpressure cooling water side? or size it as a mixture of hydrocarbon and water? I just need a background on how to approach these types of problem. I am interested regarding the excerpt on API regarding capacity credit if the cooling tower header can accommodate additional relief not sure how to check that though.



#2 _1angelia23

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Posted 16 January 2025 - 10:24 AM

to understand tube rupture scenario, read API 521,4.4.14.2 Shell-and-tube Heat Exchangers
In addition, read the article attached
https://files.engine...Wing_Wong.pdf..

Edited by _1angelia23, 16 January 2025 - 10:39 AM.


#3 Pilesar

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Posted 16 January 2025 - 08:27 PM

Here is a working link to the tube rupture article:  https://files.engine...-_Wing_Wong.pdf



#4 breizh

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Posted 16 January 2025 - 09:42 PM

Hi,

To add to this thread, there are typos in the doc shared.

Please consider this additional document.

Breizh 

Attached Files



#5 felderosfelder101021

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Posted 19 January 2025 - 03:16 AM

Hi,

To add to this thread, there are typos in the doc shared.

Please consider this additional document.

Breizh 

 

 

Here is a working link to the tube rupture article:  https://files.engine...-_Wing_Wong.pdf

 

 

to understand tube rupture scenario, read API 521,4.4.14.2 Shell-and-tube Heat Exchangers
In addition, read the article attached
https://files.engine...Wing_Wong.pdf..

Everyone, thank you. Just in time from what I just needed gives basically everything I need to consider for tube rupture. May you all be blessed! 



#6 _1angelia23

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Posted 19 January 2025 - 09:41 AM


Hi,
To add to this thread, there are typos in the doc shared.
Please consider this additional document.
Breizh

Here is a working link to the tube rupture article: https://files.engine...-_Wing_Wong.pdf

to understand tube rupture scenario, read API 521,4.4.14.2 Shell-and-tube Heat Exchangers
In addition, read the article attached
https://files.engine...Wing_Wong.pdf..

Everyone, thank you. Just in time from what I just needed gives basically everything I need to consider for tube rupture. May you all be blessed!
You can also read the article by B. Elliot titled using DIERS two phase equations to estimate tube rupture.
I can not upload it because l am writing by mobile.
White paper titled "Equations and Example Benchmark Calculations for Emergency Scenario Required Relief Loads V8.8: Control Valve Failure, Heat Exchanger Tube Rupture, Hydraulic Expansion and Fire" is also so important. It provides you with what you need to know by hysys and handy calculations

Edited by _1angelia23, 19 January 2025 - 09:48 AM.


#7 breizh

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Posted 19 January 2025 - 06:48 PM

Hi,

The document mentioned in the post above (_1angelia23)

Breizh



#8 _1angelia23

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Posted 21 January 2025 - 06:38 AM

Hi,
The document mentioned in the post above (_1angelia23)
Breizh

Breizh
Do you have the article “Correction to ‘PRV sizing for exchanger tube rupture’for W. Y. Wong.
Only the one shared before is availble as far as l know.

Edited by _1angelia23, 21 January 2025 - 06:45 AM.


#9 breizh

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Posted 21 January 2025 - 07:26 AM

Hi,

The correction was issued in Chem Eng sometimes in 1992.
I'm not sure I still have the issue. I will check. 

Edit 1:

 I cannot find it.

Edit 2:

Calculator:

https://www.enground...uberupture.html

 

Breizh 






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