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Hi there! Can anyone help me in giving some information about estimating the cross-contamination in a multiproduct pipeline when the transported fluids are separated by a mechanical device (i.e "a pig")? We have used the Austin-Palfrey Equation to calculate the interface volume, when not using...

Hi there! I am working on a simulation for a gas conditioning system. I am confronting the following problem: When I expand the gas from 1330 psig down to the desired pressure in order to achieve the required properties (i.e., %methane), the simulator predicts gas hydrates in the two-phase...

Hi there! I am working on a simulation for a gas conditioning system. I am confronting the following problem: When I expand the gas from 1330 psig down to the desired pressure in order to achieve the required properties (i.e., %methane), the simulator predicts gas hydrates in the two-phase...

Hello! We are designing a new unit for recovering liquid hydrocarbons from a gas stream, which has a CO2 content of 10% molar. The stream is taken downstream from a gas dehydration (Tri-ethylene glycol) unit, and the water content of this stream is 12 lb/MMSCF of gas. The system pressure is...

Hello! We are designing a new unit for recovering liquid hydrocarbons from a gas stream, which has a CO2 content of 10% molar. The stream is taken downstream from a gas dehydration (Tri-ethylene glycol) unit, and the water content of this stream is 12 lb/MMSCF of gas. The system pressure is...

Hi there, We need to design a heating coil in a tank containing a heavy crude oil, in order to maintain it at 160 - 170 °F. Can anyone provide us the equations for estimating the heat transfer coefficient on the oil side? We intend to use a coil which is to be located at the tank bottom. The...

Hi there! Is there any design criteria for determining flushing oil requirements for equipment (i.e., flow rate)? Any help is well appreciated.

Hi there! Is there any limitation in installing a control valve (i.e. flow control valve), in a flare Knock out drum pumps discharge line?. The issue is that some vendors are recommending us to consider a centrifugal pump (I would rather use a positive displacement pump...) to pump out the...

We are reviewing a vessel design where during depressurizing the fluid temperature can reach a temperature of -46 °C @ atm. pressure. The vessel material is not low temperature carbon steel. In some specification we found following "When depressurizing results in temperatures lower than the...

We would like to know for which king of hydrocarbons blower assisted flares shall be used when smokeless flaring is needed.

HI FOLKS, We are dealing with the following problem: The line that feeds a Crude Unit, coming from a heating train,which is 100 m away from the tower, handles a mixed phase product (vapor/liquid). The product leaving the heater is at 453 °F, and the tower pressure is 15 psig. The pipe that...

Hi All! Can anyone help us in finding out what would be the best possible location of a pitot tube for the flow measurement in a blower? Currently, we are locating it at the discharge line, but we have seen some arrangements showing it at the suction of the blower. Is there any significant...

Hi ALL! What would be the criteria for the separation of the top tray and tangent line in a stripper column? Can I assume a 24-36" spacing for this tray to allow a proper disengagement? (Column Diameter is approx. 3 ft) Is there any quantitative criteria (i.e. 0.5 x Column Diameter) to...

Hey Folks! Does anyone know if there is any inconvenience in using a mist eliminator (Vane Type) in a sour water stripper? The concern is that if there is a temperature drop in the tower, or just because of the nature of the process, possible solids accumulation could occur, and therefore, the...

I need to select an ANSI pump for a water treatment plant, with the following problem: According to the Process data we have calculated, the pump differential and flow rate, we have to select a 1x1.5 pump (outlet x inlet nozzle diameters). However, due to the nature of the fluid we are...

Hi Folks! I have been using the V = C/(Density^0.5) criteria for sizing lines, where C ranges from 90-160 and the Density is in lb/ft3. V is the critical velocity in ft/s. If C=160, then we tend to reach erosional velocity limits in the pipe. This rule is applicable for single and two-phase...

Can anyone help me in finding the recommended correlations for the heat transfer coefficient and deltaP for the shell side in a multitube (hairpin) exchanger? Is there any table to determine the number tubes that fit in these shells, like in a normal Shell and tube exchanger?