Recent content by Canoman

25362 & EGT01, Thanks for your responses, and that's an excellent point about steam backflow. However, I have been taken off the project, as I had started working on it to help colleagues. Apparently, I didn't have the proper approval. I had approval from my boss, and the person in the other...

Weird. I finished my reply, hit preview, and it took me to a page that had only two characters on it. It showed "<." So I'll try my best to recreate my response. 25362, I think I may not have described the scenario very well. Here's how I'm looking at it. The outlet cooling water line...

I'm looking at an existing thermal relief valve and trying to calculate a relief load for it. (The client doesn't have this information). The valve is on the cooling water (tubeside) side of a shell and tube exchanger. The case I'm examining is a blocked exit of the cooling water, while the...

I actually started with looking up the data from "Elementary Principles of Chemical Processes" 2nd. Ed. by Felder & Rousseau, but it had more errors than Perry's. [thumbsdown]

Thanks Montemayor... Didn't even think of checking NIST for this.

I'm looking at Perry's 7th Ed., Table 2-5, Vapor Pressure of Liquid Water from 0 to 100°C. Is this a typo? 33.2°C, Pvap = 38.155 mmHg 33.3°C, Pvap = 38.369 mmHg 33.4°C, Pvap = 33.584 mmHg (Should this be 38.584??) 33.5°C, Pvap = 38.801 mmHg 33.6°C, Pvap = 39.018 mmHg 33.7°C, Pvap = 39.237 mmHg...

McMidkiff, The thing you've got to worry about when heating liquid sulfur is the viscosity. Liquid sulfur has an odd viscosity curve. I can't find a very good online source of the curve, but if you look in this PDF file, you can see what it looks like. Lewis Sulfur Pump...

Sorry, forgot a link. http://www.bre.com

I suggest looking into software from BR&E titled TSweet. It will allow you to run multiple cases with different amines for comparison's sake. For the gas stream you've mentioned, there will probably be a number of amines that would work. I would check into DGA, DEA and MDEA. DGA, like MEA...

Just to throw it out there, I work for a process engineering firm in the refining industry that has clients worldwide, and we ALWAYS use PFD's and P&ID's. I've seen PFD's and P&ID's for projects in the USA, Canada, Mexico, Brazil, Venezuela, England, Sweeden, Isreal, Ghana, Korea, India...

Thank you very much for the direction. That exerpt helped a lot. I looked at the code, and it's exactly what I was looking for. Thanks again.

Are there any guidelines anywhere that would say if it's alright to exceed flange ratings in an upset case? My client has installed a new pump, and we are designing a vessel that goes downstream of the pump. In order to set the design pressure of this vessel, I've investigated two cases. One...

He is right. The fact that there is H2S dissolved in the liquid sulfur does change its viscosity significantly. Depending on what you are trying to design, you need to look at whether or not the liquid sulfur has been "degassed" in a sulfur pit or tank. If so, then the viscosity will be much...

I had originally specified a small vessel (filter shell) with a design pressure of 150psig and a design temperature of 350°F, but after looking more closely at the specified pump and the PSV loads, I realized that the design temperature and pressure might need to be changed. I changed the...

At home, I run WinXP Pro on a machine with a PIII 800mhz with ~640mb pc133 RAM. The only problem I have had is when I tell the machine to power down, it just reboots itself instead of shutting off. Internet Explorer crashes occasionally, but it never affects the stability of the OS. I've run...