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Recent content by LuNL

  1. LuNL

    Shell and tube HE tube rupture scenario

    Actually I just talked with the HE supplier, they told me freezing is okay for my operating condition since the shell side can handle -50 and 10 barg MAWP, so rupture on the tubes should not be a big problem. This makes me think Suppose we have a heating fluid that never freezes, and LNG keeps...
  2. LuNL

    Shell and tube HE tube rupture scenario

    Hi guys, I did the calculation and suppose the LNG is leaking at a constant speed, it will freeze the shell side, sure. But there is only few LNG trapped in the tube, and the automatic valve will stop coming LNG in 5 sec. Even though, the LNG in the tube remains only in the beginning , which...
  3. LuNL

    Shell and tube HE tube rupture scenario

    Hi georgeverghese Yes, we have the TSLL on the LP side, which can control the automated valve to close the LNG flow to the tube, therefore only small amount of LNG is trapped in the tube, while the Water/Glycol is recirculating, so frozen is protected. But personally concerned, I will put the...
  4. LuNL

    Shell and tube HE tube rupture scenario

    Hi davefitz I understand this. Just curious, can I also apply the API sizing equations for determining the flow through a rupture hole or creep/crack ? I did a simple check between API PSV sizing equation and nozzle injection flow equation Q=uA rqrt (2*deltaP*rho), u = 0.6 for liquid flow. the...
  5. LuNL

    Shell and tube HE tube rupture scenario

    Mine is fifth, time to go shopping for a new one, thanks a lot !
  6. LuNL

    Shell and tube HE tube rupture scenario

    Hi Emmanuel Thanks for this. And which revision of API 521 do you have? The one I have is only a table with text, and in paragraph 5.19 there is nothing related to number or size calculation. I don't have that Crane TP 420, so could you specify a bit detail where this "twice the cross-sectional...
  7. LuNL

    Shell and tube HE tube rupture scenario

    Dear Engineers I have encountered a scenario study for tube rupture inside the shell and tube heat exchanger. tube side : LNG 8 barg, -157 C in, and 25 C gaseous out shell side: water/glycol, 2.5 barg, 55 C in and 35 out. I assume the possible rupture will be on the back side of the tube...
  8. LuNL

    PSV sizing using standard cubic meter per hour but confused by the working fluids

    I thought so , ha ha ! It will be nice if someone can actually calibrate with various gases and make a reference for this.
  9. LuNL

    PSV sizing using standard cubic meter per hour but confused by the working fluids

    Thanks for splendid explanation guys ! So what is the purpose or how to use the table normally provided by manufacturers ? I mean the table that experimented with air, so the rated capacity is Sm3/h air. Is it due to money-wise method, for the manufacturer to only test something ?
  10. LuNL

    PSV sizing using standard cubic meter per hour but confused by the working fluids

    HI TD2K Thanks for pointing out. So is there any easy way to have a very general view about how big the PSV needs to be, before the preliminary sizing calculation? Curious is, I saw most of supplier they give the tested Sm3/h of air when the valve is fully open, can I use that number as a...
  11. LuNL

    PSV flow rate

    there is also a manual book about selection and sizing from LESER PSV, partly secured, but most is open to view. it is also very helpful, just google "LESER engineering handbook"
  12. LuNL

    PSV sizing using standard cubic meter per hour but confused by the working fluids

    Hi dear all Recently I got a interesting question from engineers. While doing the sizing calculation for pressure safety valves, I assumed if I use standard cubic meter per hour, it should be okay no matter the fluid is air, or other industrial gases, like GNG. Since the molar volume at...
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