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  1. petrochemical87

    Very Very Non Standard Problem in a multistage centrifugal pump

    you could try a couple of things 1)bypass the PSHH trip for a run and observe the pressure increase/decrease trend.By the way are you completely sure the PSHH is not faulty. The line is rated for 150kg/cm2g so bypassing pshh shouldnt be a concern 2)Why dont you open the MOV before before...
  2. petrochemical87

    liquid ring compressor - curve - HELP PLS!

    You have provided very little information, I dont think youll get a meaningful reply...
  3. petrochemical87

    Standard Pump Piping Layout especially Min Flow Lines

    sshep, I concur the first design is superior to the second, but I have seen several configurations in the plants where Ive worked in that have employed the second design. The second design is good enough to handle min flow requirements when atleast one of the pumps in running. Backflow should...
  4. petrochemical87

    Help needed

    I dont see the point of subcooling refrigerant condensate coming out of the condensor. I have seen economizers being used in refrigerant circuits to enhance the efficiency of the system, but using a flooded condensor(with a loop seal setup etc) seems like an awful waste of heat transfer area. I...
  5. petrochemical87

    Help needed

    the compressor discharge pressure depends only on the temperature of cooling media available in the condensor. The refrigerant leaves as saturated liquid in the condensor. check out this thread to learn about slide valve operation in an oil flooded screw...
  6. petrochemical87

    Selecting a Pump Based on Flow Rate and Line Pressure

    I think it is possible to get a centrifugal pump for your duty(500m3/hr,480ft). I dont think you require the 4 PD's in series.
  7. petrochemical87

    Selecting a Pump Based on Flow Rate and Line Pressure

    I must say I do not fully comprehend the problem. You say "I have tanks, centrifugal pumps(to feed the PD pumps), positive displacement pumps". Does this mean you intend to use centrifugal and PD pumps in series to achieve a flow rate of 500 m3/hr @480 feet. I believe this can be done with...
  8. petrochemical87

    Pump curve doesn't cross system curve

    This pump needs to be changed with a pump which is more compatible with your system curve. Installing a flow control valve/orifice to achieve such a huge change in the system curve will cause a lot of energy wastage.
  9. petrochemical87

    Comparision between 2 reciprocating compressor

    your query is not clear 1)Is this six throw recip a single stage compressor? a compression ratio of 126/5 in a single stage is not possible? 2) The LP/MP/HP setup implies a three stage compressor with intercoolers? please clarify
  10. petrochemical87

    Flow meter

    I have seen several arrangements where a coriolis mass flow meter and flow control valve are used for metering/dosing exact amounts of chemicals. A suitable control loop can be easily set up to use this combination for metering.
  11. petrochemical87

    Diaphragm pumps & Flow-monitoring

    yes a flowmeter should be included in the discharge of the pump if the amount of chemical dosed is to be accurately calculated.
  12. petrochemical87

    Friction head

    let h1 be the total suction(static) head h2 be the total discharge(static) head hf1 be the friction head loss in the suction piping hf2 be the friction head loss in the discharge piping total head to be developed by the pump= h2+hf2-h1+hf1
  13. petrochemical87

    Introducing liquid propane in ethane vapor environment

    Tariqi I have no idea what CET means! A small amount of propane will flash till the pressure in your vessel reaches the saturation pressure of propane at 23 deg C, then no more flashing occurs.
  14. petrochemical87

    Introducing liquid propane in ethane vapor environment

    It will depend on the temperature. If you intend to store propane without allowing it to flash then you need to set the pressure taking into account the temperature of liquid propane.
  15. petrochemical87

    Pump station Optimization

    you have 9 pumps in parallel(330KW). They all should produce the same head and flowrate in a parallel configuration. Determine the operating point of these pumps and check whether it is close to BEP .You use the suction and discharge pressures, amps drawn by the pumps to find the operating...
  16. petrochemical87

    LPG Pump for Low NPSH duty

    gasgasman, Dont hijack threads in this forum, start a new one!
  17. petrochemical87

    Significance of Pump Shut Off Head

    As JJPellin points out the shutoff head influences the design pressure of the discharge piping and the pump casing itself. From the operations/maintenence point of view, operating at the extreme left on the pump curve for extended periods of time can cause serious problems with the pump seal and...
  18. petrochemical87

    Vapor Composition in a Closed Tank

    I am not sure I am correct but I will give this a try. Assuming rault's law is valid in this case for both glycol and water, their partial pressures at 110 deg C can be calculated as p(glycol)=vapor pressure of glycol*mole fraction in solution p(water)=vapor pressure of water*mole fraction in...
  19. petrochemical87

    Pump Working pressure

    In a closed loop pumping system the pump does not need to overcome any static head it only needs to overcome the frictional head loss due to pipes and fittings(this assumption is only valid when the system is full of liquid when you start the pump). You need to calculate the frictional head...
  20. petrochemical87

    Pumps connected in Parallel

    I am not quite sure what you want to achieve with your pumping system. Do you wish to increase the header pressure? Is 2 bar the discharge pressure when one pump is running? Do you wish to run both pumps to increase the header pressure? Please provide more details.

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