Search results for query: *

Hi Najeeb, I wanted to be concise and focussed, and not vague. Your third point is what I am focussed on now. Is this somewhere in API-650? If not where can this be located. Thanks Again for your response. Regards Nov

Hi Engineering Colleagues, How do you calculate size of surge drum for steam condensate if you have all design flows? Cheers Nov

thanks for the responses. Highly appreciated

An example of a bad actor is a piece of equipment that fails frequently. A pump that fails frequently due to seal leaks. This pump would be marked as a bad actor for further assessment by Engineers.

Dear Engineering Professionals, I am working on improving our steam turbine reliability in Downstream (O&G). We are looking into developing a Bad Actor list so that we can work with Maintenance Engineering to resolve problems as they arise. What would be a good definition of Bad Actor related...

Dear Engineers, I am a Facility Engineer at a Naphtha Jet Hydrotreater producing Low sulfur diesel as the main product that goes direct to Market. The diesel quality related to cloud point is a challenge to maintain especially during winter when the spec is very low (-40 degC). We take product...

Hi All, I have read through all the comments and valuable insights regarding the use of both nitrogen and NG/FG. I appreciate all the valuable information based on both your experience and judgement. I will definitely be digging deeper into the feasibility of using NG, based on all the...

Hi All, I am gonna try responding to all in the one thread here. The N2 will vent to atm in the event of overpressure through PVRV on the tanks. The plant used NG as the blanketing medium initially for +/- 10 years before switching to N2. This was during the mid-late 90's. We are looking at...

Hi Fellow Engineers, We have several floating roof storage tanks at our refinery that we are currently using LP Nitrogen for blanketing. The reason being for process safety/fire hazard concerns. We have been using LP N2 for around 20 years with success. We are considering moving to NG...

ok thanks

Thanks for the response and the suggestions. We have lowered feedrate and have decided to shutdown sooner.

Dear Engineers. I need some suggestions on a Gas Oil Hydrotreater I am currently working at as process engineer. The reactors have a Ni-Mo type catalyst (fixed bed) that have prematurely come to the EOR (end of run). We have a 3-4 months to go before out shutdown and I need to ensure we...

Dear Engineers. I need some suggestions on a Gas Oil Hydrotreater I am currently working at as process engineer. The reactors have a Ni-Mo type catalyst (fixed bed) that have prematurely come to the EOR (end of run). We have a 3-4 months to go before out shutdown and I need to ensure we product...

Fellow Engineers, thank you for the detailed responses. We are exploring PSV's now as a suitable option.

I am in the process of designing a relief device for a PD pump. I have 2 questions regarding the rupture disc as a relieving device for the PD pump. 1) Is the discharge from the Rupture disc allowed to go back into the pump suction? 2) The pump inlet and discharge piping is 1/2" diameter. I...

Thanks for the recommendations. I will be done a final process audit of the entire line and thereafter will action the suggested solutions. Thanks Again to All.

These scenarios sound promising towards resolving the issue. My first step will be to get Maintenance to check the NRV, as it could be passing. The steam/heat tracing also could be a contributing factor to the pressure shock. Thanks Again.

The max operating pressure in the receiver is 1 atm - vented to atm. The static head is 12.25kPa between source vessel and pump. The dead head differential of the pump is 380kPa. Thanks for the tip on the steam tracing. We will check the loops out to make sure all is working.

Thanks Again, I will start afresh and do another process audit. Will post any further findings and deviations. 1. The heat tracing is for the -40 degrees temp that can occur in winter and piping runs outside. 2. The line is designed for 1035kPa max, which is same as PSV setting. 3. Discharge...

Georgeverhese, although I cannot share the P&ID due to policy, I will try to describe the system better. 1. A condensate receiver tank (1m dia x 2.5m high), followed by 4" hand valve, followed by 400kPa centrifugal pump. 2. 4" check valve, followed by hand valve 4" 3. a 2" flow nozzle (and...