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  1. ajs1972

    LOPA alarm response as IPL

    I would say, like you, that is not an IPL, because the valves are common to another IPLs (common cause factor), normally the alarms are for operator´s awareness and the manual actions are required, for example, close manual valves or activate emergency buttons what close another final elements...
  2. ajs1972

    Batch Distillation Optimisation

    Hello you can check "Handbook of Separation Techniques for Chemical Engineers" from Schweitzer. By the other hand, you are right, one of the most important topics, are the pressure control, lowering temperature in condenser, one question, is above atmospheric pressure or in vacuum operation?? I...
  3. ajs1972

    API RP 2350 FOURTH EDITION

    Hello: According the API RP 2350, this recommended practice does not apply for "Tanks (process tanks or similar flow through tanks) that are integral to a process". My question is, the gun barrel tanks (dehydration and desalting oil, 500 000 barrels) must be considered like "process tanks or...
  4. ajs1972

    Blanket Gas Rate Determination

    Hello, please read this. Regardshttp://files.engineering.com/getfile.aspx?folder=ecf5fb2a-cb19-4030-88e3-4d6c3f7b4388&file=rules_of_thumb_(1).pdf
  5. ajs1972

    steam dispersion at atmospheric discharge

    According to EPA regulations you need to calculate the dispersion of released chemicals for some possible scenarios. There are some commercial simulators for this. Please read this EPA document...
  6. ajs1972

    Interlock SIL calculations

    Hello Keyvagirl: In fact, the limit switches improve the reliability of solenoid, and its possible check it by partial testing. Please, check this document (pages 1 and 2)...
  7. ajs1972

    interlock valve

    The fundamentals of the valve is avoid (closing) or allow (opening) the flow through the valve for safety or quality proposes. But, the only valve is only a part of a interlock. The complete interlock consists of tramsmitter (send a signal), controller (compare with a set point value) and final...
  8. ajs1972

    Debutanizer Operation

    Try this, check the pages 14, 66, 86 and 245, regards. http://www.aimsgt.com/technicalpapers/RefiningProcesses_2004.pdf
  9. ajs1972

    Acid gas scrubber with wash solution recycle

    Hello: Do you have aspen plus process simulator? Look the document. Regardshttp://files.engineering.com/getfile.aspx?folder=470798dd-5511-466c-8746-63b248b36345&file=Dynamic_Model_of_a_Scrubber_Using_Aspen_Plus.doc
  10. ajs1972

    PRV sizing for a gas blow-by scenario

    You need to consider that scenario in your PHA and determinate the risk level in case of over pressure. The SIL will be determinate in function of the risk level. You can do a LOPA analysis and to determinate if is necessary the PRV or not according to PFD (probability of failure on demand of...
  11. ajs1972

    Overflow tank control question

    Do you have a drawing in order to clarify your question? Thanks.
  12. ajs1972

    PSV Noise Calclucation

    check this, I think coulde help to you. http://www.valve-world.net/srv/ShowPage.aspx?pageID=585
  13. ajs1972

    Residence Time in Vertical Vessel

    Hello Victor4: The equation was taken from the book: "Unit Operations of Chemical Engineering" from Warren L. Mc. Cabe, Julian Smith and Peter Harriott. In this book, it mentioned that the separation process is influenced by the densities of the sustances involved and the height of the...
  14. ajs1972

    Residence Time in Vertical Vessel

    This problem is related to densities of the fluids. Here, the equation: t= (6.24 * viscosity of continuos phase in cP)/(density of liquid A - density of liquid B in lb/ft3) The time (t) will be in hours. Regards.
  15. ajs1972

    Positive displacement pump

    I think is´possible that scenario; in my experience I have seen plastic containers with 250 gallons of capacity collapsed because of vent closed and bottom valve open.
  16. ajs1972

    Effect of HIPPs with PRV as Overpressure Protection

    The HIPPS and PRV are two independents layers of protection. Must be placed according to a hazard review of the process. The HIPPS not reduces the relief load but the total relief; in case of the HIPPS fails, the PRV must be activated in order to avoid the overpressure of the system. For...
  17. ajs1972

    Stripping time

    Like sshep says, its necessary to know the conditions in your tank (pressure and temperature).
  18. ajs1972

    Stripping time

    What are your initial and desired acetone concentrations? What are the conditions of your steam (temperature or pressure)?
  19. ajs1972

    Siphon Break Question

    Hello Katmar: You are right, in fact this is the base of design in vacuum condenser systems. The height of the leg is designed to 10 meters, in order to achieve the maximum vacuum in the condenser and to avoid the flooding.
  20. ajs1972

    Fire case Relief

    I think the answer is yes, because the wetted area in the vessels are changing, and the heat rates, too.

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