Search results for query: *

Hello, are there any specific issues with modelling of screw compressors? They have to be modelled as the centrifugal ones? thanks, Joisy

Well, I do not presume any problems with storage as the current foam(er) is more corrosive than one it's to be used. I mean operational problems with the foam/water proportioning devices?!

At our plant we used previously Fluorprotein Foam concentrate (CRODA) and we gonna change it over with AFFF. How do you think if it can cause a problem at the foam/water solution makers (the same concentration of foam concentrate & water - 3%) thanks, Joisy

At our plant we used previously Fluorprotein Foam concentrate (CRODA) and we gonnag change it over with AFFF. How do you think if it's a problem for the foam/water solution makers (the same concentration of foam concentrate & water - 3%) thanks, Joisy

Dear All, I've developed a software which calculates the alarm/trip levels (heights in meters) for the 3-phase Separators. They'r calculated on the base of the liquids' hold-up timings. (if the height of a particular level is less than some specific minimum value (meters), then it sets to this...

Phex, Shell practices maybe very good but how can I see them being out of Shell? Maybe someone can send me them at joisy(nospam)@land.ru? thanks everyone I will keep you on track ;), Joisy

Dear All can you please advise me the vendor, which can supply the pump with 1 - 5 cub.m/h flow, 55 barg out and 2 m NPSHA. Assume that we should come up with positive displacement pump. thanks, Joisy

Dear All, can you please advise me where (some practices ?) it's good to read about the cone bottoms' design (maybe with discharge well) for the Petroleum Storage Tanks. thanks, Joisy

Sounds good, but I'd like to get a reply here from such an expert. I was working with the several sales persons from the different pump suppliers and it looks like they do not understand my issues well. cheers, Joisy

Hello Everyone! I need to choose the pump for water/oil sandy service: the blend is to be pumped fro the atmospheric tank - 0.3 m static head to the vessel with 6 barg pressure. The blend contents the significant amount of sand - upto 3%. 80 cub.m/h is the required capacity can you please...

Hello Everyone! I need to choose the pump for water/oil sandy service: the blend is to be pumped fro the atmospheric tank - 0.3 m static head to the vessel with 6 barg pressure. The blend contents the significant amount of sand - upto 3%. 80 cub.m/h is the required capacity can you please...

As far as I concern the cyclones are used for gas/solids separation - not liquid/liquid drops. Why not to use the simple two-phase separator - there are a lot of good manuals, and this will not require the droplet size (at least for the first approach).

Thanks you very much, friends for your replies, but I'm already out of this problem. However this maybe useful either for me or for someone else... cheers, wish you a succesful year............

Once I was with the calc of dP in h-exchanger (I think you calculate tube side as well as I did) and we knew that this can be fouled after a while. We've just doubled the calculated dP for the clean x-changer to predict fouling effect. However the regular maintanance - twice a year is included...

Hello All, can you please explain me the difference in modelling a compressor with & without characteristic curves thanks, Joisy

If you assume no significant dP across the section you can use the same equation as for the liquids... cheers, Joisy

If our respectable moderators will just collect all the tips (with answers) of each topic & make them available for the downloading at once - we can use it as the initial point for a preparation of FAQ. I think the database should let them to do it! E.g. convert it into MsAccess format, so as to...

Hello all, I do have some idea here ). Can someone (maybe from eng-tips) collect all the threads, sort them out by the topic and make them as a FAQ file - set for the downloading. This will help many people not to ask the same questions many times. Howevere this must be experienced engineer as...

Guys, and what tables have you used to define enthalpy? The ones I have have very inconsistent & give the significant mistakes during interpolation?! thanks, Joisy

Assuming that the question is too difficult :) I will answer on it myself! It needs to define Enthalpy "H" of superheated steam at the inlet conditions (P1 & T1), and then find what temperature complies to "H" if the pressure is 389 kPa. hope this is correct & can be useful...