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Dear Members, In Centrifugal Compressors we calculate Polytropic efficiency only -Why not adiabatic efficiency ? Where we calculate and use adiabatic efficiency? Thanks in advance.

DEAR 25362, With floating end you are correct(no one will like the floating end nozzle extending through the rear end cover in an odd pass STHE). In the case of fixed tube sheetSTHE, is there any advantage in having both tube-side inlet and outlet piping connections at the same end.

Dear members, Though add no of tube passes are not unknown, most STHE have an even number so that both tube-side inlet and outlet piping connections are made at the same end.What are the advantage? Thanks in advance.

joisy Did u try Compressor handbook by Lapina?

Thanks for the replies. If the natural gas contains heavier hydrocarbons also as liquid alongwith water, molecular weight of 36.7 may workout.

Dear friends, The following are the equations: Page : 106 The following common equation is used for both desuperheating and condensing. 1 1 ---- = ---- + ro U(dir) ho Page 58 / Page 62: 1 1 Lw { Ao } 1 ---- =...

Dear members, In March 1981 issue of HYDROCARBON PROCESSING page 135, an example is given for partial condensers. Some-one could clarify what is the dry gas flow and dry gas molecular weight. The gas stream is being natural gas how molecular weight could be 36.7 against natural gas molecular...

Dear members, As in page no- 62 of Applied process design for chemical and petrochemical plants by E.E. Ludwig volume three, how to incorporate tube material thickness and conductivity in the worked out example in page no-106(Condensation in the presence of non condensables).Any suitable...

Dear TD2K,Montemayor &Rashesh, Thanks a lot.

Pressure drop values given in the STHE data sheets are inclusive of nozzle pressure drops or exclusive of nozzle pressure drops. Thanks

K M PILLAI, Is the equation you have used is from CARL YAWS. Is there any accurate equation to calculate liquid waterviscosity. Thanks in advnce

HI Guidoo (Chemical), Encore thanks for your reply.

HI Guidoo (Chemical), Does it mean that there is no press drop in the vessel, other than mesh and i/l & o/l nozzles. Thanks in advance.

HI Guidoo (Chemical), Thanks for the very useful info.

How to calculate pressure drop in two phase separators.Relevent references? Thanks in advance

Someone could help me on the following: What material is suitable for 70% Conc Sulphuric Acid.Pump(Impeller) and Piping. Temp is 40°C. Suction is from road tanker(open to atomosphere), it is to be transferred to storage tank of about 10 Mts Height. Thanks in advance

DEar TD2K, You are very much correct, there is a fault. I should have used MW of water in lieu of the dry gas. With MW of water I get the value of 23032.7 as shown below: Wat cont at IL=6.791/(14.116-6.791)x 32500/22.414x18.016=24218.6 kg/hr. Water content at outlet = 0.613 / (14.116 - 0.613)...

Dear Td2K, Could you please comment where I am wrong? Why the difference between my calculation and aberta's. Thanks in advance

For the given density of 0.147 kg/M3, the pressure works out to 18.71 psia as shown below : Density = PM/(ZRT)= 0.0293lb/ft3 or 0.147kg/M3. Pressure = 0.0293x1545x(80x1.8+492)/1x144x10.7 =18.71Psia How you are getting pressure as 14.116 Psia? Vapour pressure at 80°C = 6.791 Psia. Vapour...

Thanks for the info moltenmetal.