Hi guys.
I'm not process engineer and I don't have any knowledge about reservoir. But in our last study we find that our off gases for injecting into well heads stand in supercritical regime. In other word we want to compress our off gases to inject into well heads. But as we compress the gas in...
Hi guys.
I'm not process engineer and I don't have any knowledge about reservoir. But in our last study we find that our off gases for injecting into well heads stand in supercritical regime. In other word we want to compress our off gases to inject into well heads. But as we compress the gas in...
Hi everybody
I have a little problem with required NPSH of hydraulic driven diaphragm pump. Based on pump calculations available NPSH for this type is about 1m for Q=10m3/hr & delta p=90 bar. Searching milton roy and lewa products i couldnt find suitable pump for my application. Can anyone help...
Hi Everybody.
Let's start a discussion about pump type selection. It might be so easy for some of you but i want to consider all the corners and points for best selection.
We want to transfer 1.8 m3/hr hydrocarbon condensate via a 3" & 500 m pipe to a 8" & 110 bar transfer pipeline continuously...
Hi all.
I want to know can we use separate purge gas and buffer gas in type in distance piece of reciprocating compressors? In the other word we want sweet fuel gas as a purge gas and nitrogen as a buffer gas. Is this choice true? I doubt.
API 618 use " should " and not "shall" for preference...
Hi all
I want to know about advantages and disadvantages of horizontal storage of spare rotor from point of maintenance, balancing ...
Is there any preference when selecting one of these two method?
Is there any criterion about size, weight,... To choose one of these 2 methods?
Hi all. We have a flare knock-out drum centrifugal pump in an arrangement of 1+1, and hydrocarbon with 80000ppm h2s and 150000ppm chloride. Our design temperature is -100c . What class do you suggest?
Thanks
Hi all. We have a flare knock-out drum centrifugal pump in an arrangement of 1+1, and hydrocarbon with 80000ppm h2s and 150000ppm chloride. Our design temprature is -100c . What class do you suggest?
Thanks
Hi all.
I want to know about advantages and disadvantages of these 2 configurations form your approach.
I want to compress 780 m3/h from suction condition of t=65 & p=5bara to discharge pressure of 126bara. Molecular weight is about 32 and i have sour gas to compress.
I want to use LP,MP,HP...
Hi Guys
I stated before my question about designing a field compressor station to boost pressure of a gas field upstream a gas refinery. The condition of our reservoir varies in years. The Compressor Suction pressure changes from 70 barg to 25 barg after 5 years and then remain constant for 10...
Hi all
I want to know about the influence of variation in temperature, pressure , molecular weight , specific gravity in suction of centrifugal compressors on their efficiency and operation condition? i want to know about your referenced experiences not about the general subjects in compressor...
Hi All
I Want to know about allowable operating range and also preferred operating range for centrifugal compressors. Is there such concepts for centrifugal compressors? and also i want to know does manufacturer guarantee the whole operating range of centrifugal compressors or only guarantee...
Hi all. I want to know details about engineering and procurement of glycol type dehydration package. Can you explain me more and introduce me some useful references? Thanks
Hi All,
I am wondering about how to fill out API mechanical data sheet supposed to cover 2 different operation condition? in the other hand, we have a 2+1 condensate transfer pumps with specified conditions . but this pump's capacity will be different after 5 years. how it can be?
