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Thanks again, We have contacted the vendor specialist and waiting for the feedback. We have strainer in suction side of Expander. Regards

Thanks georgeverghes, We tried what you proposed by depressurizing it and drying it with Nitrogen, However, still having the same problem. For your information, we are having this unbalancing after reaching the inlet flowrate 300,000Stm3/hr @ the speed of 13000rpm, that means before this, we...

Hi, We have just started a new LPG train with AMB Magnetic bearing TurboExpander Technology. However, we noticed that there is a high electrical current in Recompressor side in this new TurboExpander, (Recompressor Side 17 to 20Amps; Turbine side 5 to 8Amps. This means since the current...

Hi All, We have been asked as Client for approval to make 02 Golden Joints (to avoid Hydrotest) on 18'' SS piping THK 48-50mm, in order to fix a misalignement of this line. This line has been already hydrotested (Design pressure 106bar). Can somebody give me a technical point of view, if it's...

Hi What about ASPEN-HYSYS?

Dear HTURKAK Many thanks for your collaboration. And special thank also to Mr LittleInch. Regards,

Hi HTURKAK; Thank you for your valuable information, However I did not get the second point" Follow the decision tree ( Fig. 1 Test Type Selection ) the criteria for max. stored energy alowable 271 MM-J..[/highlight]".Please Clarify, and wherecan I find it? Regards,

Dear All, Please could someone tell me , What is the max Energy Stored in Pipe volume (Calculated in ASME PCC-2–2008) that does not let us perform Pneumatic test of new piping. Knowing that we are converting some Test packs from Hydrotest to Pneumatic Test. Regards,

Thanks sshep, your explanation seems to be covering our case. However, is there any software can give answer to our phenomenon. Regards,

Thanks Mr Latexman for your technical reply that I do actually appreciate them very well. for our case, Which of the Flow patterns can be our case in order achieve this flow without problem. Regards,

Dear All, Thanks to All, I think the difference of pressure is not a good explanation, since from the outlet of Expander up to Vessel inlet the differential pressure is so low. However, Can you Mr Latexman be clearer by characterization of the Flow, to understand this matter. Regards,

Dear all, In our LPG plant, Process Gas at 95bars , 12°C @ inlet of Expander will have -41°C , 22bars @ the Oultlet of Expander and becoming Mixture Liq & Gas. However; this mixture goes through piping routed upward vertically to 15m from Expander centerline to the Vessel. In other hand...