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Have you considered the problem of frothing and seal heights as reasons for design changes?

See a book by Bard-Faulkner on electrochemical methods and look around for cyclicvoltometry and chronocoulometry. These techniques are used to determine what you are talking about.

corrosion rates are very subjective and difficult to determine. One solution is the use of corrosion coupons to determine the actual corrosion rate. A probe that determines this in my mind would be unreliable. What I think your probe is doing is measuring the concentration of a disolve...

The chlorine is coming from someplace, and either through a recycle stream or fresh feed accumulating to 70ppm. Are the side strippers using de chlorinated H2O, or the Desalter wash water, is there a possibility of carry over from the desalters into the CC? There may be other generative...

My error

Check ASME 31.3 Appendix M. If plugging is a concern consider use of a plug valve "if the fluid conditions meets the criteria" otherwise go with 31.3. Also, ask a piping designer if you have no reason to change standards. If your company doesn't have access to these, ask them why they don't...

If your are having second thoughts due to a weld failure wouldn't you look at the type of welding-joints used and what welding process was used (SMAW or whatever) and the type of weld stick (Filler metal) was used? The failure wasn't in the actual 304SS. In the petroleum industry each weld...

jamesbanda (Chemical) You can have almost any velocity so long as there are no problems in that particular application at that velocity. Every tank is a different size, and I believe at surge that there should be about a 5 minute holding time in your tank. There are recommended velocities of...

Boghi1990 (Mechanical) Are you sizing a flash vessel that is already in service? Are you sure on those temperatures... OUCH. Melting point of carbon steel is about 2800 deg F. There really is no good way to answer your question. You might assume that the lines leaving your flash tank were...

JoeChem: Trim is widely considered the auxiliaries surrounding the vessel or column. So, level gauges, standpipes, bridles, staircases. But, depending how the cost of the trim is calculated might include man ways, nozzles, PSVs. It's not a clearly defined term, but usually means low price...

EthanolBlending83 Check to see what if any affect the water vapor would have on this volume of ethanol due to in-breathing. Use a liquid seal material that simply isolates the ethanol from atmosphere. So a layer of inert liquid/solid that floats on the ethanol and to slow the evaporation and...

Do not derate your vessel based upon there always being a supply of demulsfier. Often the supply of demulsfier runs out before the feed into your separator. And once you've sized the vessel, its sized.

Most chemical process engineers learn from a book by Peters and Timmerhaus called "Plant Design and Economics for Chemical Engineers". It's very good and a great reference. This book explains how to find break even points, ROIs on plants and cost estimates for vessels, internals, trim...

During shutdown make sure the vessel is clean and free of sedimentation and physical obstruction. Inspect the Diptube for possible improper mixing issues (air/liquid). You may also need to look at the vessel drawing to see the design on the distributor at the end of the dip tube. The inlet...

Have you tried regressing the data to create an analytical function, and then a taylors series approximation of the function. Or interpolation?

10815L, The information I have is owned by the companies that payed for the work. So, I can't really post that. Sorry can't help.

I believe your design is going to be based on where you want the separation to be. You might want ot be in rating mode also when you do this, but why do you specifically need HYSYS to do this calculation? Why use a hydrocyclone for oil/water separation? Data would be useful to answer your...

HAZOP (Hazard and Operability study), SIL (Safety INtegrity Level), LOPA (Layers of Protection Analysis). First comes HAZOP which determines the possible dangerious deviations of the current design. Inputs are P&ID information, Cause effect diagrams. This step can be difficult but results...

Has anyone had good experience with PRO II and simulating suspended solids in streams? What methods did you use, or add ons? Just curious. Thank you.

Montemayor, Thank you. I usually use a table It is amazing how such a seemingly simple problem can not be simply solved. For example, describing the motion of three objects trajectory bound by their gravitation attraction. Makes me think there might be breathing room for something...