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Hello all, One very quick query please. We have a high pressure trip on reactor set at 12barg which stops the reactor reactor pump. Once the reaction is completed, reactor is depressurised to atmospheric pressure and then vacuum of say 800mbara is applied. There was a discussion that our...

Hello all, Need your help please. I want to calculate amount of component x condensed along with water vapour during reaction. The reactor batch is 10 tonne. The reaction takes place at 180 degC at which component x is removed and condensed. Vapour pressure of the component x at 180 degC =...

Hi all, Need your help. We have bought bare shaft centrifugal pump (without motor)which requires 20kW motor however we have motor with power rating of 27kW on site from old pump and we are planning use this motor. Please note there is no change in operating point (flowrate and head) of the pump...

Hi all, I need your help/input please. Please see below link where I have attached a simple drawing of the system. As you can see, pump P1 (7m3/HR) pumps hydrocarbons to dryer (D1) via heat exchanger (HX1). In the dryer, liquid is sprayed and pressure is maintained at atmospheric pressure and...

Dear all, I need your help please. Currently we have high pressure boiler (to generate saturated steam at 60barg, 2000kg/hr) feed pumps with the below stated configuration. The boiler feed water pumps are high pressure PD pumps (duty and standby) on inverters with the operation pressure of...

Hi all How would I check if my vent line or vent header is blocked? Is there any cost effective technology that I can use to make sure if it's blocked or not? Do you think ultrasound or thermal imaging camera are useful? Please note, the vent lines in questions are steam traced due to the...

Hi all I am working on a FEED stage of a project and I want to estimate operating cost (OPEX). Agree, from name it's evident that operating cost e.f. Running pumps, compressors and utility cost should be considered at the least. What else should be considered please? Any example template...

Dear all I have come across another thing which made me puzzled. One of the existing relief valve is 3/4" X 1" with orifice area of 0.04in2. Supplier confirmed it is an ASME certified valve. If we compare this with the smallest orifice D of API, it hour be 0.11in2 and equivalent of ASME, it's...

Dear all I have a vessel with design pressure of 10barg. MAWP (max allowable working pressure) is not known. Therefore I will use design pressure for relief valve set pressure. Also, vessel code is not known and hence I don't know what is accumulation pressure or % accumulation is allowable...

Dear all One more query please Vessel operating pressure is 5barg Vessel design pressure is 8barg Our team has decided following 1) 1" relief valve set pressure 7barg. Assume, it's designed for 300kg/hr steam. 2) 1.5" relief valve set pressure 8barg. Assume it's designed for 600kg/hr steam...

Dear all Can I install an expander at the inlet of the relief valve? Say existing nozzle is 3/4" (assume this the only available nozzle) and the new required valve is 1.5" (orifice F) and the valve is set at 6barg for the valve maximum capacity of 0.25kg/sec of saturated steam. At the valve...

Dear all I need your help please. I believe/read multiple relief devices are installed when 1) sparing (duty and standby) philosophy is required (maintenance purpose) 2) release rate is large and is to be compensated by more than one relief valve/device 3) two very different release rate are...

Dear all, I need your help. I am confused with VOC calculation. During tanker offloading, the outbreathing rate from a tank is 50Nm3/hr. The breather valve was originally set at +25mbarg which was then reset at +35mbarg. The original design document says the increased set pressure has reduced...

Dear all, I am not sure if this the right place for this thread but I believe we all share the pain of not having good document system so it should be fine here? I used to work in a small scale EPCM company in past where we had developed an internal manual system of handling various projects...

Hello all, One of our clients have a very old vessel for which original design documents are not available. I want to size the suitable relief valve for that vessel but it can’t be possible unless I know the design pressure of the vessel. Please let me know how to find out design pressure? If...

Hello All, I am reviewing venting requirement for flammable solvent tank [all atmospheric] farm site located in Europe. I am tasked to look at normal and emergency venting requirement. There are many horizontal spit tanks, each tank containing 3 compartment and each compartment containing...

Hello all, I wish to calculate vent area required for two phase release by Leung’s method. There is a term called ‘q’ with units W/kg i.e. total heat input per unit mass. I wish to consider a release scenario and confused with LMTD. Say reactor jacket is 95% full of water [at 20 degC] and...

Hello all, I have a bit of confusion and need your help please. A reactor has got an independent bursting disc [designed for two phase release] and a relief valve [designed for vapour release] both relieving to atmosphere. Reactor design pressure: 6barg Maximum accumulation pressure: 6.6barg...

Hello all, I need your help. We have a reactor with an internal coil [coil dia 2”, 40 schedule, coil design pressure is 15barg and vessel design pressure is 6barg] carrying saturated steam at 20barg [temperature 214.93 degC]. In fact 2” coil is supplied steam with a 1” line The steam inlet...

Hello all, Just a quick query please. How do we decide the design temperature and design pressure for shell side and tube side of a heat exchanger condensers? I have following conditions Shell side: water vapour with nitrogen at 3barg and max at 180degC Tube side: Cooling water at 4.5barg and...