I have a reactor that is insulated with 2" of OC Foam Glass 1. It protected by 304 stainless. Can I take credit for the foam glass when calculating the required relief rate?
I have a reactor consuming hydrogen. The MAWP is 90 psig. The NFPA Pmax ~ 87 psig and Pred ~136 psig. Because the Pmax is lower than the MAWP, does this mean that the vessel will contain a deflagration - i.e. that we do not need to install rupture discs for this scenario?
I have a Client with a distillation column. I am designing for vacuum protection. The column has a reboiler. A portion of the OH vapor is fed downstream to a process and a portion is condensed. Assuming the steam to the reboiler stops and the condenser still operates. The default in the...
For "normal" tube rupture case (tube side is high pressure, shell low pressure) the standard approach is to assume 2 orifice or 1 orifice / 1 pipe - i.e. from both sides. However, for case where tube side is low pressure, protected side, I am not sure how dual source would apply. Anyone had...
I am a bit stumped about handling this system. See attached. At blocked in relief (900 psig), the flow to the system will cease, but before that happens the loop pressure will increase substantially. This will cause the suction pressure to the compressor to increase, ultimately causing the RV...
I have a recycled oil stream, Flash Point 204°F, being fed through indoor ASME filters designed for 150 psig. There is no source of temperature exceeding the flash point. I am questioning whether I need to consider a fire case. Thoughts?
I have come across some distilleries that are applying NFPA as follows to atmospheric tanks (designed to 1 oz/in2:
1. Have automatic sprinkler systems - F factor = .3.
2. There is verbiage in NFPA that states that for ethanol can take another 50% reduction on top of that - i.e. F factor = .15...
I have several insulated tanks that are controlled to 140°F. I am sizing conservation vents a vapor recovery (scrubbing) system. I would seem that I could disregard the thermal outbreathing component since the tank temp will be higher than ambient. The materials have a low volatility.
Any...
I am evaluating installation of a bidirectional RD. To properly calculate the capacity of the RD and related piping I need an estimate of the Kr and MNFA of the candidate RDs. However, this is not an ASME application (MAWP<15 psig and MAEP = -8 psig). I remember running across some...
I have a MeOH stripping column, with reboiler heated by steam. Overhead vapor is condensed in downstream condenser. At shutdown the feeds and steam are shutoff.
Question is how to handle inbreathing if the condenser is left on. At first glance, it would appear that I should treat the...
We are pumping MeOH from a railcar to a storage tank, and venting the vapors from the tank back to the rail car. I have run flow calculations from the tank to the rail car to determine the maximum vapor rate through the OH line - to not overpressure the tank. Then I back calculated the liquid...
I have a 30' tank, feeding 1300 gpm liquid. There is a 8" open vent on top of the tank as well as a 24" emergency vent.
To calculate the the maximum flow rate through the 8" open vent, should I use the design pressure of the tank or the tank elevation?
I am installing an EZHeater, which is a steam injection device, to generated tempered water. This is similar to a Pick heater, with which you may be familar. I will be using 250 psig steam, and the heater will be designed for 300 psig. The upstream steam is limited to under 300 psig. I...
I am attempting to determine the stack height for a vent required to maintain the concentration of contaminant (ammonia) below the LDHL during a release. The stack will be installed above the roof a building. The key is that maintenance will sometimes be required on a platform installed above...
I am trying to find a RV to handle higher viscosity fluids. The highest case is 850 cp. I have run into a problem, as it appears that 160 cp may be the max that will work with conventional Dresser and Crosby valves.
Q1: You know of any reclosing certified RVs that will work at this viscosity...
API 2000 states to use a outbreathing rate due to pump in of 16.04 x gpm for cases where the vapor pressure > .73 psi. Does this mean .73 psia, or .73 psig?
I am estimating the temperature increase while making a coating, which contains a high level of dispersed solids.
To estimate the heat capacity of the mix, I have been using a weight average of each component. Is this a correct approach?
We are looking at a reverse flow case. Normally liquid CO2 flows through a reciprocating pump, then is combined with vaporized CO2, the combination is a vapor. A PHA team found a potential source of overpressure on the suction side of the pump should the pump be shut down. We are modeling...
I am looking at placing an impingement plate on the end of a 5' diameter stack. We are looking at placing it 10' (two pipe diameters) above the stack. I am interested in whether there may be enough back flow off of the plate that might cause a flow disturbance in the stack itself. We are...
