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EXPLOSION AND STRESS ANALYSIS 8
- Thread starter M.Jamali
- Start date
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LittleInch
Petroleum
M Jamali,
I realise English may not be your first language, but your post doesn't really make sense and is very low on detail.
"Explosion effect"?? External or ??
Piping or pipeline?
"Field" means different things - Animals / crops?, Oil /Gas field?, Operating plant being constructed?
Where are you working? Different codes and standards apply in different places. Legislation and local safety codes differ.
This site is very useful, but it is not an online university or training course.
what is your training, experience, knowledge, position?
Who can you ask in your company?
Provide a LOT more detail and ask a much more specific question.
Otherwise "Could you please Guide me to know how could I do it ?"
Yes, employ a suitably experienced engineering consultant....
Remember - More details = better answers
Also: If you get a response it's polite to respond to it.
I realise English may not be your first language, but your post doesn't really make sense and is very low on detail.
"Explosion effect"?? External or ??
Piping or pipeline?
"Field" means different things - Animals / crops?, Oil /Gas field?, Operating plant being constructed?
Where are you working? Different codes and standards apply in different places. Legislation and local safety codes differ.
This site is very useful, but it is not an online university or training course.
what is your training, experience, knowledge, position?
Who can you ask in your company?
Provide a LOT more detail and ask a much more specific question.
Otherwise "Could you please Guide me to know how could I do it ?"
Yes, employ a suitably experienced engineering consultant....
Remember - More details = better answers
Also: If you get a response it's polite to respond to it.
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HTURKAK
Structural
- Jul 22, 2017
- 3,359
You may consider to look the following doc. and the doc. attached ..
Protection of Piping Systems Subject to Fires and Explosions (FABIG Technical Note 8)
Protection of Piping Systems Subject to Fires and Explosions (FABIG Technical Note 8)
- Thread starter
- #6
Thank you for Reply ,
Dear @LittleInch Your Issues and Details are true and i have to Sent Enough Information .
We Working with ASME/ANSI/API/NFPA Standards Series in our Program
our Group Design Piping Firefighting line and System For LNG Plant .
Our Client Has Request For Check Explosion Effect on Firefighting Pipes (External Explosion )
and at this stage we Can not Fine Some One how has Suitable Knowledge in Blade / Explosion Analyzer
our Line Material CS - A53 B - Sch 40
Dear @HTURKAK
thank For answer
Dear @LittleInch Your Issues and Details are true and i have to Sent Enough Information .
We Working with ASME/ANSI/API/NFPA Standards Series in our Program
our Group Design Piping Firefighting line and System For LNG Plant .
Our Client Has Request For Check Explosion Effect on Firefighting Pipes (External Explosion )
and at this stage we Can not Fine Some One how has Suitable Knowledge in Blade / Explosion Analyzer
our Line Material CS - A53 B - Sch 40
Dear @HTURKAK
thank For answer
EdStainless
Materials
Jamali, What standard did they ask you to check against?
Start with the NFPA, they have comments about the systems tolerance to external damage.
One of the real problems that you face is estimating what an explosion would even look like.
= = = = = = = = = = = = = = = = = = = =
P.E. Metallurgy, consulting work welcomed
Start with the NFPA, they have comments about the systems tolerance to external damage.
One of the real problems that you face is estimating what an explosion would even look like.
= = = = = = = = = = = = = = = = = = = =
P.E. Metallurgy, consulting work welcomed
- Thread starter
- #8
Hi Dear Ed
the plant which we working on it
has 2 vessels , one of them Store Propane and another Butane plus flare line Pipe exist too
i think we have to Simulating by ANSYS or relevant Software but one of Client Engineering team told me Exist some standard formula Which resolve explosion data to dynamic load for input them into Caesar or Bentley autopipe for analysis .
unfortunately i'm not in touch to him for ask more info .
at the present i dont know exist any standard or Code or not .
the plant which we working on it
has 2 vessels , one of them Store Propane and another Butane plus flare line Pipe exist too
i think we have to Simulating by ANSYS or relevant Software but one of Client Engineering team told me Exist some standard formula Which resolve explosion data to dynamic load for input them into Caesar or Bentley autopipe for analysis .
unfortunately i'm not in touch to him for ask more info .
at the present i dont know exist any standard or Code or not .
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M.Jamali
I don't know how much experience you have with explosion design, but my impression is that it is limited.
You mention that you two vessels, one stores Propane and the other Butane, you also mention a flare line.
Under normal operating conditions neither of those things is a problem, you also need to add some type of accident. If something happens that results in a vessel leak and then the leaked gas forms a vapor cloud, that you have the basis for an explosion.
Usually, when I do this type of analysis a risk engineer or process engineer has done a risk analysis and provided the needed scenarios. Once you have the energy, an explosion, or more correct a blast wave can be calculated. When I work with this type of projects I usually get the blast parameters (peak pressure and duration) and go from there.
Typically, for a structure, that is my area of experise, it means a transient dynamic (often non-linear) analysis. You mention Ansys, I work with another general FEM-solver, but Ansys can do this. You mention a few other software's, I recognize some of the names but I don't know if they can do this type of analysis.
You ask about standards and there may be some that are relevant for your specific project. But based on the information you have provided I won't speculate regarding what standards to apply. I also know that some of the "Big guys" in the process industri has their of requirements.
Also, in my experience, that are not that many shortcuts in this type of safety related designs.
Good Luck
Thomas
I don't know how much experience you have with explosion design, but my impression is that it is limited.
You mention that you two vessels, one stores Propane and the other Butane, you also mention a flare line.
Under normal operating conditions neither of those things is a problem, you also need to add some type of accident. If something happens that results in a vessel leak and then the leaked gas forms a vapor cloud, that you have the basis for an explosion.
Usually, when I do this type of analysis a risk engineer or process engineer has done a risk analysis and provided the needed scenarios. Once you have the energy, an explosion, or more correct a blast wave can be calculated. When I work with this type of projects I usually get the blast parameters (peak pressure and duration) and go from there.
Typically, for a structure, that is my area of experise, it means a transient dynamic (often non-linear) analysis. You mention Ansys, I work with another general FEM-solver, but Ansys can do this. You mention a few other software's, I recognize some of the names but I don't know if they can do this type of analysis.
You ask about standards and there may be some that are relevant for your specific project. But based on the information you have provided I won't speculate regarding what standards to apply. I also know that some of the "Big guys" in the process industri has their of requirements.
Also, in my experience, that are not that many shortcuts in this type of safety related designs.
Good Luck
Thomas
You need to define your design case.
For a plant like you describe - a BLEVE, or Boiling Liquid Expanding Vapor Explosion is the extreme design case. Not much survives this case, the design goal is to never let the conditions arise which could lead to a BLEVE.
Some more realistic Propane Emergencies Scenarios can be found at this link. As far as codes go I would start with NFPA, and have someone with prior experience on the design team. If your employer has a relationship with an underwriter, they may be a resource.
For a plant like you describe - a BLEVE, or Boiling Liquid Expanding Vapor Explosion is the extreme design case. Not much survives this case, the design goal is to never let the conditions arise which could lead to a BLEVE.
Some more realistic Propane Emergencies Scenarios can be found at this link. As far as codes go I would start with NFPA, and have someone with prior experience on the design team. If your employer has a relationship with an underwriter, they may be a resource.
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