Recent content by dimitris

Dear friend, I do not clearly see what you mean by saying that the total heat balance is on the stripping steam side ? Plus why should there be an increase at the degasifier's pressure ? You do not add a fixed amount of steam but as much steam as it is needed to achieve a certain pressure...

Hi, All chemicals are fed at the exit of the degaser storage tank. Some of them are fed at the suction of the B.F.W pump and some at the discharge, I am sorry for not properly clarifying that at my previous post, Best Regards, Dimitris...

Dear All, In our Hydrogen Production unit we have a UOP Polybed 2 PSA unit. As you all know the purge product contains severe quantities of CO and Hydrogen. (In our case an approximate concentration is 7% CO and 17% Hydrogen). We are currently screening the market for portable CO detectors that...

Hi, Are you refearing to process condensates or just steam condenstates from your steam production ? Each case needs to be treated differently.. Dimitris..

Hi, We are using an all organic BFW treatment. We are producing MP steam at a pressure of 45 Kg/cm2 and superheat it at 440 C. The B.F.W includes: -Addition of a three-amine mixture for the PH adjustment of our condensates -Addition of a mixture of organic polymers for scale inhibition and...

Hi, Normally it is necessary to purge ammonmia piping systems prior to access them. It all depends on the pressure of the system of the overall ammonia hopld up and of the extent of maintenance you will perform. The best way is to isolate the area you want to do work at, properly blind it, and...

Dear jproj You sound a bit tough saying that we forgot our basic chem eng knowledge. Anyway to be absolutely precise you have to add the sensitive heat effect of the superheated steam in the latent one, but usually this is negligble since in most cases the L.P. utility steam is superheated by...

I think that there is a small mistake in your energy balance calculation. T1 should be the temperature of the water leaving the deareator and T2 the water temperature entering the deareator. This amount of steam is the necessary steam for heating the water to its exit temperature (the saturation...

Please discuss the temperature of BFW inlet at a degaser. In our Ammonia plant we are feeding DW at a temperature of 90 C, in the degaser. The degaser operates at 102-103 C. Please discuss if an increase of the inlet temperature at 93-95 C would cause any problems at the degaser's operation...

Does anyone have any experience on inspection methods on refrigerated ammonia piping. We intend to inspect our piping network, but wish to do so without the removal of the insulation and with special care on tee-connections. Anyone has any experience relevant to this issue??? Regards, Dimitris

Thank you very much for your prompt response, Best Regards, Dimitris

Dear All, Does anyone of you have any idea the type of material and the exact composition of SB 111-687 material. I looked in to the appropriate tables but with little luck, thank you in advance, Dimitris

Dear All, I decided to write the following thread in the refining section even though ammonia is not a Hydrocarbon but because the process used to produce it ressembles so much standard ferining processes, I beleive that it is relevant. I am a head process enginner in an Ammonia Plant that is...

Hi everybody, To be able to comment on any potential corrosion problems and methods to monitor them we need to know the working conditions of the unit i.e. feed and product composition, waste gas composition, temp and pressure variations on so on. We operate a UOP PSA H2 purification unit, with...

Dear Whylie, I am afraid that I am not aware of the system your are talking about, but one thing that crosses my mind is that this may be a strat up unit only. As you may already know, when you start a reforming hydrogen production unit, to heat up the reformer you pass nnitrogen through it...