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Dear all , wonder if anybody out there into simulation who can advice me on correct thermo method to use for a mixutre of components including H2 , N2 , methane , ethylene , butene, isopentane at 30 kg/cm2 g and 95 c fed to S&T exchanger . the exchanger is cool enough to partially condense...

is explosion a scenario in ur case ? i heard of fire case , blocked dicharge , rupture of bottom manway ,line but not explosion ...can u please describe your system ? thnx

more on dilution steam addition purpose ,,, 1- steam has a sufficient oxidising effect on iron and nickel to minimise carbon formation reactions ... 2- used in start up of a furnace in warm up operations .. 3- used for coils decoking operations .. ratio typical ... ethane cracking...

more on dilution steam addition purpose ,,, 1- steam has a sufficient oxidising effect on iron and nickel to minimise carbon dorming reactions ... 2- used in start up of a furnace in warm up operations .. 3- used for coils decoking operations .. ratio typical ... ethane cracking...

why u need a furnace to supply regeneration duty ..most mol sieves are regenerated using steam heaters or electric heaters ...unless u have some waste heat recovery potential .. what type of mol seives u have ...do u need a preload step after regeneration ( safety related step ) ,,,what is...

if its a new design might be feasible to use API 2/3 rule ..and forget about it .. if u really need to size a psv ..i wonder how complicated it will be doing it in a simulation software ,,assuming rubtured tube an orifice....

vessels with knock back exchanger inserted inside vessel is very common too...and can be much cheaper for your application ....

hi all,, wonder if anybody heard of or has experience with on line particle size disribution measurement ....i'm interested in applications for gas/solid fluidised bed .....thx

may be this will help,,, for fixed restriction system ...dp will increase across as flow increases ...talking about typical liquid ..this will follow q=kSQRT(dp),, example of fixed restriction system is pipe , fitting ,equipments like heat exchangers ..filters.....etc. now for any system...

the dry seals are now becoming the default mech seals application ..i know a good number of large centrifugal compressors with dry seals ...running trouble free... as long as the buffer gas source and instrumentation around the seal is well designed ...then the seal should be ok ...buffer gas...

i'm not relif valves expert ..but wonder if : - other cases ( gasoline and diesel ) fillings are emergency steps (like the MTBE )? if yes , can these steps prevented by shutoff valves or other interlock system ..? - i thought API2000 stipulates releif requirements for atmospheric tanks and...

if this discussion is still a live ..for my comment above ..for the outlet secondary seal pot ..consider make up /over flow ..in case oil level is blown ,, regards

this is one good discussion ...few notes first : is this really a vessel ? its not if design pressure is < 15 psig as per ASME code so check API relief protection for atmospheric tanks... is that a psv ? or breather valve ? guess u r talking about a breather and there is no isolation on...

if the container qualifies as vessel that can be isolated as per ASME then a PSV is a MUST. for the gas vessels or vessels which store high boiling liquieds (above deign temp of vessel )a secondary aid like the blow down system (with API 15 minutes criteria ) or a sprinkle system should be...

i dont have this information ...but if you need this to help decide to go for dryseals..these are as reliable as oil film seals ...and are already installed in huge centrifugal machines in many plants....the advantage over oil film seal is quiet clear. hope this helps ..cheers

here is a basic question that has been a source of confusion ,,let me start discusion for those interested ( and know correct answers) by these two qustions ,, i always thought that for a constant speed centrifugal compressor : 1- for any change in suction properties like pressure ,mw ,T...

hi all, here is a basic question that has been a source of confusion ,,let me start discusion for those interested ( and know correct answers) by these two qustions ,, i always thought that for a constant speed compressor : 1- for any change in suction properties like pressure ,mw ,T...

a side note here , in TD2K response says there are variations in pressure basis for standard conditions , i recall variations are in temperature not pressure basis, i,e either 60 F or 32 F (NORMAL Vs STANDARD )while pressure is always 14.7 psi cheers!

known limits for clean liquids are 3 m/s,,,,but practically and away from exact numbers ... go for the higher flow..keep track of couple of elbows thickness frequently ...and if u start loosing thickness (how fast is how much u r lucky )then consider other alternatives...by which time u have...

most common for seawater are ,,,FRP'S or C.S.cement lined FRP'S potential problems are breakage... cement lined c.s problems are when lining is gone... a decision i beleive should be based on how good u will design and engineer any of the two options... 316 L ( known limit for the...