2 replies to this topic

[Ankit_Kumar]

I need to do sizing of RD/PSV on tube rupture case at shell & tube heat exchanger. There is no chance of flashing due to tube rupture and both side contain liquids. The details are as follows:

Shell Side Design Pressure = 19 kg/cm2.g

Shell Side Operating Pressure = 15 kg/cm2.g

Tube Side Design Pressure = 10 kg/cm2.g

Tube Side Operating Pressure = 7 kg/cm2.g

 

As per API-521, “relieving rate is to be the liquid flowing across a rupture equal to twice the cross-sectional area of one tube.” (Correct me if I am wrong).

So Flow Area, A = 2 * Cross sectional Area of tube

A= 2 * ( ∏ /4 * d^2) 

Now

Liquid Flow = 1685 A * SQRT (∆P * Density)

 

d = Inside dia of tube = 14.8 mm

P1 = Rupture’s upstream pressure of fluid = 15 kg/cm2.g

P2 = Rupture’s upstream pressure of fluid = 7 kg/cm2.g I consider max. operating pressure for P 1 & P2.

Density = 913 kg/m3

 

Therefore, So by using above two equations, I got following values; 

Liquid flow = 33.3 tons/hr or 36.5 m3/hr

 

Appreciate if anyone can verify the methodology being adopted & guide about the way forward.

 

Regards

Edited by Ankit_Kumar, 12 January 2016 - 08:58 AM.

[Bobby Strain]

You need to study a bit more.

 

Bobby

[Ankit_Kumar]

Bobby, pardon me i didn't get your point. 

 

The methodolgy adopted is not right?