asifraza0
Chemical
- May 29, 2006
- 62
I'm sizing an centrifugal pump for a water service in a close system. The system starts from the surge tank, pump, few heat exchangers and complex piping network. Eventually the pump discharge comes back and joins the pump suction. The surge tank is 30 ft elevated and is the highest point in the system. The second highest point in the system is the bank of heat exchangers where the pump discharges.
1) I've calculated the discharge pressure by taking a static head of 15 ft. 15 ft is the height from the grade to the highest inlet nozzle of the heat exchangers.
2) Then I've added dynamic losses, control valve losses, filter pressure drop etc to arrive at a total discharge pressure.
A counter argument is: Since the pump discharge comes back and joins the suction in a closed loop system. The static head is irrelevant and should not be included in the sizing calculations. Risk of not adding the static head means the pump will be undersized.
Please commnent and share your thougths.
Thanks in advance
John
Asif Raza
1) I've calculated the discharge pressure by taking a static head of 15 ft. 15 ft is the height from the grade to the highest inlet nozzle of the heat exchangers.
2) Then I've added dynamic losses, control valve losses, filter pressure drop etc to arrive at a total discharge pressure.
A counter argument is: Since the pump discharge comes back and joins the suction in a closed loop system. The static head is irrelevant and should not be included in the sizing calculations. Risk of not adding the static head means the pump will be undersized.
Please commnent and share your thougths.
Thanks in advance
John
Asif Raza