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Dear georgeverghese Supply line transfers meg plus salt,return pipe line from reclaimer transfers meg containing small amount of salt. We have calculated pressure drop for supply pipe line at lowest temperature,it means worst case design. For return pipeline ,meg temperature at inlet is high...

Dear Dejan We are currenting working on using both 4" and 6" size in our pipeline, I mean some part of piping would be 4inch and another part is 6inch. With this strategy we omit new pump installation and on the other hand using 6 inch pipe woud be economically feasible rather than pump...

Dear Dejan, Thanks a lot for your post, You are completely right.A report considering all economic,operational and constrauction aspects will be prepared.but first of all , I need to be sure that my design is technically acceptable to be considered as an option.I mean if 6 inch case is...

Dear Dejan, Thanks a lot for your great posts,To be honest i have not compares two options(3 km ,6inch pipe against 3km ,4 inch pipe plus pump and accosiated control valve), but the main reason is that we prefer to do not touch existing package and just take a branch from tie-in point. Actually...

Dear Ivanovic Thanks a lot for your great post. Actually in our study we selected 6 inch pipe rather than 4 inch in order to use existing pump and to prevent new pump installation and because there is a good static head available in piping system(around 3 bar static head against 8 bar friction...

Is there any concern with velocity of 0.5 to 0.6 m/s?

Dear Dejan Please find simple sketch as attachment. Pipeline design is based on maximum flowrate of 40 m3/hr and 40 percent turndown. Thanks for you helphttp://files.engineering.com/getfile.aspx?folder=e7186bc1-4251-40a1-9c99-bf21f562fe1b&file=image.jpeg

Dear Dejan Thanks for your responce,about option 3 it should be explained that as exiting pump and level control valve was already designed and installed for second plants ,if client prefer to do not touch it, actually we should consider new pump and control valve for case when first plant need...

Hi everyone, We need to design supply and return pipelines from one plant to another plants in order to use existing package in second plant.package will be used occasionally by Only one of two plants. Because source of liquid is storage tank in first plant ,there is not any concern in designing...

Hi everyone; we are going to transfer chemical from storage tank trough pump and pipe line to another plant.maximum flowrate is dictated by downstream plant and it is clear. i need to define normal flowrate because i need it for calculation and also to put it in equipment and instrumentation...

thank you very much my friends

thanks a lot all friends

Dear Georgeverghese, dear LittleInch Thanks for your response, actually i have done my sizing , just wanted to make sure that there is not special consideration for MEG. Another question which i need to work on it is about turndown ratio for a MEG pipeline.is there any manual or standard which...

Hi all I am looking for some criteria for velocity and pressure drop/100m for MEG in order to perform line sizing for MEG line and pipeline. I know general criteria for liquids such as what mentioned in TOTAL or others standards, but winteresting thing for me is special criteria for MEG ...

Dear Ashtree; thanks for you reply, maybe i need to answer to matters you raise one by one: 1)flowrate of 40m3/hr is design capacity of downstream unit. 2)all activities are actually expansion in existing facilities,it means 3dmodel of boat plant is available,so new pipe length and static head...

I am going to size a centrifugal pump to transfer liquid from one plant to another plant through 2 km pipeline. maximum flowrate which could be transfered by pipeline is limited by downstream plant and is around 40 m3/hr. since maximum flowrate is fixed , i am not sure that is it still required...

Two post upper I wrote a portion of standard.To prevent misunderstanding I should write whole Section 5.2.7- BDV timers(this section is subsection of 5.2 EDP requirements): In order to prevent flare overload, local BDV timers (pneumatic or hydraulic) shall be installed to ensure that ESDVs are...

Also in the same standard in section 4.2.4.2 which explains Actions for ESD-1 (fire zone emergency shutdown) it is mentioned that: "Upon confirmed fire and/or gas detection, automatic emergency de-pressurisation (EDP) offshore, and optional onshore. Open all the BDVs (Blow-Down Valves) in the...

reference is made to TOTAL specification- GS EP SAF 261 "Emergency Shut-Down and Emergency De-Pressurisation (ESD & EDP)": Section 5.2.7- BDV timers: In order to prevent flare overload, local BDV timers (pneumatic or hydraulic) shall be installed to ensure that ESDVs are closed before BDVs are...

Dear Friends; I am not sure that whether here is a right forum to ask my question or not.If not ,please move this topic to relevant section. I want to know how can I model a piping system between two closed valves(shutdown valve) which in case of fire is being pressurized by fire.Indeed I want...