Recent content by sav455

Hi Ajs, I just posted my reply to Jefka's post only to see yours was posted also. I am wondering if you could perhaps elaborte a little more about increase in wetted area and heat rate. I think the wetted area stays the same because it in a way is indicative of hold up volume in the vessel which...

Thanks Jefka. In this case we are not changing any vessel. The only thing which might change is the composition which will change the latent heat of boiling and hence the relief.Same goes with the gas case also. I have a related querry in use of HYSYS depressuring utility for estimating the gas...

Hi All, I am wondering if the relief rate form a PSV sized for fire case is dependent upon plant feed rate. Let's say we want run an existing plant at 130% capacity and do the debottleneck work. Do we need to rerate the fire case relief also?? The equations in API 521 don't indicate the same...

Thanks a lot. Sav

Hi, I am trying to calculate the gas blowby case flowrate from high pressure separator to low pressure separator. I am wondering if I can use the max Cv of the liquid level control valve. The Cv by definition is the related to the flow rate of water at 1 psi pressure drop. In gas blowby case we...

Is it not a choked flow problem? With an supply pressure of 90 psig to 1 atmosphere. I think you will get critical flow through the hose....

Thanks Biginch and JMW. JMW, you did not go off the topic. In fact you talked very much in relation to what I am supposed to do. Thanks. SAV

Hi All, I am required to calculate the reduction in volume of liquid hydrocarbons upon mixing. The detail of the problem is as follows: I have three stream: naphtha, distillate and gas oil.These ssreams can be routed to different tanks.I did a quick simulation in HYSYS and found that there is...

dcasto, the sulfur in Naphtha is 1 ppm and that in Distillate is 130 ppm. This is the total S content. I have the S distribution over the entire boiling range also,so I know what cut range we are looking for. Milutin,Whatever preliminary work I have done shows that It is possible to meet all...

Ammm...I think I should not call it diesel. This is a stream which is back end of naphtha and front end of kero or Distillate. Due to the 15 ppm thing and associated hydroprocessing limitation we have to produce some stream for internal consumption using distillation route. The only deemed feeds...

And this is distillation based scheme. I have to get some cut from these two feeds.Sorry about missing on this information in the first post.

Hi, I am working on developing a scheme for production of 15 ppm diesel from naphtha and kerosene stream. Basically I am trying to get to some scheme which gives me minimum heater duty, minimum no. of stages,min. col diameter, optimum tray location for both the feeds and optimum diesel draw...

Hey, I think these kinds of data are not readily available. From whatever you wrote, it looks like you want to use activated carbon for adsorbing the hydrocarbon from amine stream before sending it to the regenerator. I would probably prefer doing my own experiment and get my own data. Probably...

Thanks Quark.

Thanks Quark and Doug. The cost of one 1 MWh = 45 $ HP steam = 17.76 $/tonne Both are canadian dollars. Regards.