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So I got another problem that I could use some advice on. It has come time to create a datasheet on a conventional inlet scrubber for use in a typically sweet and dry compressor station (Horizontal with cyclone tubes) and I have to input conditions (density viscosity) for the liquids even though...

Thanks for your help unfortunatly it looks like I cannot ignore the pressure drop in the header. At least if I have to do it the hard way next time it should be easier.

HYSYS works fine for cyrogenic air seperation, we use it all the time. PROII works well also it is just not as common in industry

I agree with your post, just 1 point of clarification. If pressure drop is like voltage and flow is like current is "resistance" the same variable as described in Crane Flow of Fluids Technical Paper No. 410 (HL=K*v^2/2g

Ok I have never been asked this question before so I need some help. Currently I have 8 aerial coolers in a first in last out configuration (also called "U" configuration I believe) and people i.e my boss is concerned that the first cooler will have more flow due to its smaller pressure drop...

While I do not subscribe too or condone the illegal trafficking of pirated software www.emule-project.net provides a file-sharing program that has access to many such programs. I fear this is the only manner in which you may get to use these programs besides signing up for a course at U of T

My faith in HYSYS has not faltered. I just get asked alot of questions about its validtiy (I work with alot of old guys that dont trust "That new fangled technology") and I find that I must provide the burden of proof for every new application we use it in. Let this be a lesson to those who...

So for comparitive purposes between sets of T and P as long as you use the same source (HYSYS or API) you should be good? I guess I find the absoulte values easier to understand cause I can see and reproduce the calculations that lead to them. As for HYSYS I just can't see any calculations.

I am curious as to why the values for enthalpy in HYSYS (Peng-Robinson with Lee Kesler Enthalpy Correction EOS) are negitive for typical natural gas. Does this mean that HYSYS compares the enthalpy to a refernce value because when I look up the enthalpy value in the API databook the value is...

Sorry about the wrong title on the thread

In HYSYS using Peng-Robinson EOS the mass enthalpy values are all negative, does this mean that HYSYS is comparing the enthalpy at you T and P to that of some refernce state? or is it the enthalpy of formation?

Wow those are alot smaller then I would have thought.

I need to know a typical reid vapour pressure for diesel, I fear that such a number doesnt exist from a quick literature search

Dawe.Matthew@colteng.com

I was wondering if any one has experince in designing pipeline equipment for dense phase natural gas. Our gas is 18 MPa and -2 C. I am curious to see the effects this phase has had on their equipment ( pressure drops, psv sizings and such) Dawe.Matthew@colteng.ca

Thats a really interesting process, particually if you are trating sour gas offshore. Let me know what you find

I stear clear of HYSYS when dealing with such things such as failures and relieving rates

Hmm I maybe off here but after you combust H2S you get SO2 and then you scrub it with sea water and the results are sulfates is that what your getting at?

Well I want my program to be able to calculate Lee-kesler values based off the Tc and Pc alone irregardless of the sitiuation. It seems to me like a value such as V in the aformentioned equation is a specific value dependent on your conditions but if that is the case how do people use the Lee...

I have been trying to create a spreadsheet to come up with residual properties via Lee-Kesler EOS I have however hit a snag. In Lee-Keslers paper he describes a term Vr=Pc*V/Tc*R where V is the volume of a simple fluid. The paper I am refering to is called "A Generalized thermodynamic...