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I am wondering what will be the best suitable elastomer (Buna-N, EPDM, PVC or something else) for rubber seat/ lining. The fluid being either Acid (0.2% wt HCL) or 1% wt. NaOH. Temperature may vary between 5 -40 C. A quick reply is highly appericiated. Thanx

I tried simulating it based on tbp only. but when it comes back to the simulation enviorment it asks for composition again. therefore could not fig out what is happening. thanx.

TBP cut points are available. I need very simple composition that I can plug in hysys or pro-II. Therefore I need to pick the right components and in wt frac. As far as psedo components are concerned, I have modeled them. Therfore it will be highly appericiated if you can provide some thing on...

Can some one provide general naphtha composition in terms of c3, c4, c5 ...... etc in wt %. Actual names will be more useful. such as i C4 or ch, i c5 etc.

Yes, I will very much like those papers and as soon as possible. Can you email those on this weekend i.e. Sept. 6th to Sept. 8th. I will very much appericiate. You can e mail at Sandeep1970@hotmail.com. Thanx. Thanx.

Thanx, Any info. on the web or someone's own condensed info. is highly welcome.

Can any one suggest latest industry developments on energy saving/ managment techniques for refineries. Any useful literature, web site etc.. Thanx.

Guys, I am looking to start a consulting company. I saw lot of you guys representing small companies and very experienced professionals. I am wondering if you guys can provide any useful ideas how to start and get initial assignments. I will appreciate any useful leads or references, articles...

Re cost of bulk Oxygen, guess your best bet would be to contact Air Liquid Inc. or Paraxair as they sell the Oxygen directly. This will be able to give you a rough estimate i.e. approximately how much will it cost you to manufacture your own Oygen.

Various govt. agencies have stipulated the lethal (limits) for various materials at different conditions. You can find that info on the ineternet.

The answer given by TD2K is correct. In your scenario if there is the probability of overpressuring the column do exist then you can look in to the option of switching the fluid sides i.e. fro shell side to tube side. Sometimes this can solve your problem easily. in the worst scenario this...

API- 520/521 is the first step. As this is very generic, if you have specific problem/ confusion then you can discuss that seperatly.

Can you elaborate on the intented use of the wet steam. otherwise if it is only heating the fuel oil then it may be better to do it directly but if you want to heat the water as well then it is different. Re the valve Yarway could have the valves you are looking for. Thanx.

Courtney Dehn: Thanks for your response, I am interseted in your code. If it is possible can you post it? Thanks. Thanks to others as well for your thoughts and useful software sites. I have used "http://www.jehar.com/online.stm" quite often. Thanx.

Same as said by TD2K, the KBR ROSE unit is with C2/ C3. Havent heard of Rose unit with Hexane (C6). I will be intersted in theis topic if you find anything on the C6 Solvent let me know. Thanks. Thanx

There is no standard API or anything on the spare pump philosphy. But normal practice differs based on the importance of the pump. Such as if the pump is very critical, then you will test start the spare pump every morning shift i.e once a day. if it is not that critical then you do it at least...

Good points. Steven's example is good, In the moderen refineries to addresss that issue quite often people install at least one utility boiler with multiple fuel option ( as this does not cost that much as far as fixed capital is concerned) because this gives a very good operational...

As you have seen most of the ideas on the flare, they all are viable. To your specific Q i.e. to avoid the wastage of energy: Flaring in upset plant is un avoidable. This option you would like to have, otherwise you being the neighbour of refinery will be effected as well. 2. Whereas...

What you have said is correct only in simple systems. Often in the reninaries that is not true. There may be scenarios where the control valve dp is higher for higher flow. This could be dictated by the downstream conditions. Keep in mind that you should never look at the control valve...

Two things (1) keep the temperature high enough in the visbreaker heater to avoid any king of coke formation. (2) steam purge in the heater cross over can also avoid coking in the heater. You need to keep the appropriate velocity inside the heater and the feed piping. Impact of caustic to...