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Dear all. As China becomes industrialized, their need of PVC has increased and they are having trouble finding petroleum . So carbide based production of PVC is something thats hot over there. Does anyone knows this process? In what ways does it differ from the usual ethylene+choride - EDC -...

Dear all. Does anyone know how many license technologies exist for producing EDC and VCM? So far I've found vinnolit but surely there must exist more licensors out there

Hi all I got an assignment to do a quick cost estimation of an amine wash system for a petrochemical plant. This system contains a step for raising the pressure over a liquid from 2 -> 10 bara, the liquid flow is about 400 to 1000 gpm. Anyone who knows what such a pump costs and whats its called?

Montemayor. It concerns a new plant, I would be interested in the cost for all positions, the reboiler and condenser, the lean rich interchanger and the lean cooler.

Dear all Im calculating on the cost for an absorption stripping system and Im trying to estimate the installation cost in the case when shell&tubes are used and the one whrn plate heat exchangers are used. The method Im using now is distributive factors on the purchase cost. However Im afraid...

Hi everyone Im looking for engineering costs when dealing with systems such as absorption stripping or evaporization within petrochemical industry Anyone who knows anything interesting?

yes well I am just doing an estimate and I tend to vary the CO2 load between some values to get a feeling of the sixe of the equipment. The result will not serve as any designbasis for a plant, rather a cost esimation

Dear all. Im simulating a CO2 capture unit for an ethylene plant. What molar % of CO2 is resonable to apply and do you think the absorption unit will differ very much in efficiency and heat if I choose ethylene, ethylene and ethane or something else as flowgas ?

What is your concentration of MDEA?

Anyone who know the latest M&S index for 2006?

When using MDEA to remove H2S and CO2 what material is recquired in the vessels such as the columns, reboilers, leanrich..?

Dear all. I wonder if any of you know where CO2 and/or H2S capture systems are fitted in the petrochemical industy. I found them in the ammonia process and ethylene oxide process. Very often the solvent in the ammonia process is K2CO3. Can it be any amine as well? Anybody with any expiriences...

Hi again. Feed flow, Liquid flow and pressure is also of interest and the CO2 H2S concentrations of both feed and outlet

Hello everyone. Does anyone know where to find operational data of any existing aMDEA and Benfield plant? The data of interest is absorber and stripper temperature, column diameter and heigh and [CO2] and [H2S] Thanks

alechelt. Is this a major problem when dealing with MDEA as well? In my experience MDEA is less corrosive than MEA and DEA. or is this due to its lower heat of reaction so that the contactor temperature never reaches those levels? What is the limiting factor and temperature when dealing with...

thank you alechelt!

But those packages are available in ASPEN as well. I downloaded a package called KEMDEA. The simulation is done with the reaction kinetics the equlibrium modell is called ELECTRNL (I think) My guess is that its the same as HYSYS uses since ASPEN bought HYSYS a couple of years ago.

Thank you Montemayor. Yes that system is it. The "theta" is the rate between the difference between in and out temperarure and the logarithmic mean temperature. The graeter it is the more narrow the hot inlet and cold outlet can be. A PHE has a higher theta value than a s&t.

Hi everyone. Im calculating on a lean/rich interchanger for an gas sweetening system. What is done if a shell&tube with theta=1 (deltaT/deltaTL) and the desired temperature of 100C into the strippingcolumn is not achieved and the only reachable T is about 80C? Is an extra heater placed just...

one can remember n=PV/RT at 25C 1atm =101325/8.314(298)=40.9 so converting 1Nm3 to moles is always 40.9