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Thank you all for your suggestions. The mixing should be done inline so vessel is not applicable. I will try to arrange a test to check IONE and MORTENA suggestions. For the sake of good practice, let’s consider the following options: 1. Flashing the saturated fluid on a valve and enlarging the...

MortenA It will be not responsible to say that I am sure that it is not from the valve. The all line was taking the bumps and the valve is very close to the mixing point. It is very hard to identify if the bumps are from the valve or from the mixer. For the mixer, and that goes for RustBuster as...

Case description: Saturated brine (9 bara) is flashed (5 bara) over a valve. The two phase fluid is than mixed with cold brine (<100oC) discharged from a heat exchanger. What we see (or hear) on field are heavy and noisy bumps that seem close to take the pipe out of the concrete. 1. Are there...

thread378-218923 I want to use the above thread as a reference to my question. I consider designing a 3000 ft line carrying ~60000 mg/kg TDS brine with 1.2%w NCG (mainly free carbon dioxide?) at 350oF and 400 psig. Pipe route is horizontal but includes some vertical cross roads (10-20 feet...

I used winsim (design II) for this. There is no need for more complicated tools. Do you have any recommendation regarding the friction factor and friction loss correlation?

Thanks. My “thumb” guess was that I am dealing with flashed two phase flow that will finally be vapor (in line or tank). I made a T&E simulation taking a 21 barg saturated liquid going into a 40 m 2” line (CS) and change the flow until I got 8 barg in the end of the line. Larger flow will drop...

Dear Biginch, 1. I agree that most accidents happen during maintenance and that is why I am looking for your wise advice. This system already exists and valve cannot be added (maybe on the future design). I need to deal with this line as is. 2. An orifice plate is not acceptable since this is a...

BigInch, thanks for your quick reply. Since the low pressure vessel is used for maintenance only I prefer not using control valves (the spoken scenario is a mistake and not a operational procedure). My aim is to define the pressure relief valve on the top of the low pressure vessel (see sketch...

I am trying to find a way to evaluate the N-Pentane flow through a 2” pipe leading from the bottom of a pentane vaporizer (saturated liquid area) operating at 21 barg to a low pressure vessel designed for up to 8 barg (nominal pressure is atmospheric). The 2” pipe equivalent length is about 40...

Morten, The vaporizer works at 22 bara. liquid is flashing via 2" pipe connected to the bottom of the vaporizer (liquid area). How can i calculate the gas flow in this pipe in order to calculate PSV that fits the pump casing pressure (8 bara). Hope i am clear.

Hello, My question is about the following model. I have a 22 bara vaporizer with organic fluid. a 2" pipe is connected to the bottom of the HE (with blocking valve) for filling and evacuation service when process is shut and no pressure at HE. This pipe is connected to a pneumatic pump with 8...

Hello, I am trying to optimize an air vent system in a close diesel room. The problem is that the room must stay at a constant temperature and while the vent is operating the temperature increase and the air condition cannot compensate. Since i have no experience in this issue, Is there any...

Pete, Thanks for sharing this experience. I will try to implement it in my work. Yet I think annular flow in 20% quality is a little ambitious. Do you think 65 ft/sec should be the preferred mean velocity at any quality? The two phase line is leading into a separator so i dont mind the phase...

Thanks for your kind reply. Hanon - this is one of the methods I used before I applied the forum. David - Thanks for your comment. I will flip the coin....

All, I thoroughly red thread469-22342 and it almost gave me all the answers i needed. Yet, I am designing a 700m horizontal 20% quality, 10-16 bara, two phase line (steam and water). I am trying to optimize pressure drop, velocity and flow regime. There is a disagreement between the designers...

Thank you both. Zdas04, This is a filling evacuation system. Swing checks valve of any kind will cause a problem. Do you think double block by gate or ball is enough to make this case "non credible"?

This is the case i am dealing with: A 2" pipe connecting a pressure vessel (200.5 psia) to a pump. The pump is designed to fill and evacuate the cold and not pressurized fluid. I must protect the pump from 145 psia. In case of leaking (or open from some reson) 2" valve there will be high...

This is the case i am dealing with: A 2" pipe connecting a pressure vessel (200.5 psia) to a pump. The pump is designed to fill and evacuate the cold and not pressurized fluid. I must protect the pump from 145 psia. In case of leaking (or open from some reson) 2" valve there will be high...

Thanks, Im done for now....

After consulting with NALCO like MJCronin advised i decided to use the NALCOL 2000 with addition of NALCOL 73532. Thank you all for your replies...