4 replies to this topic

Gentlemen,

I am facing some issues in designing the Nitrogen Blanketting system for a Methanol Injection Skid. The P & I D for the Methanol Injection Skid is attached for your reference. The data that are not mentioned in the attachment are as mentioned below. This data is from the client. And we already have the order for these Methanol Injection Skids. But we do not have much idea regarding Nitrogen Blanketting.

Specific Gravity of Methanol: 0.793 @ 1.5 barg & 45 deg C
Viscosity of Methanol: 0.42 cP
Filling rate or Flow rate of Methanol into the Tank: 1.8 m3/h
Outflow rate or Flow rate of Methanol out of the tank to the Pump Suction: 0.99 m3/h
Tank Volume (working): 4.5 cu.m
Dimensions of the tank: 1650 mm ID x 2300 mm (T to T) with 2:1 ellipsoidal Dish ends
Tank Volume: 6.1 cu.m (actual)
Design Pressure of the tank: 3.5 barg / FV
Normal Operating Pressure of the tank: 1.5 barg
Volumetric flow rate of Nitrogen: 1.8 m3/h
Density of Nitrogen: 2.649 @ 3.5 barg and 45 deg C
Design pressure of inlet Nitrogen to the tank: 3.5 barg
Molecular weight of Nitrogen: 28
Compression Factor of Nitrogen: 1
Viscosity of Nitrogen: 0.02 cP
Design Temperature of the entire system: 7 / 85 deg C
PCV0004 reduces the pressure of the incoming nitrogen from 3.5 barg to 1.5 barg
Set pressure of PSV0001 is 1.5 barg. PSV0001 is not a pressure cum vacuum relief valve, but a normal safety relief valve (This has been confirmed from the client, and they are sticking to this, even though we feel that this is not correct).
PCV0005 is a back pressure regulator, which shall be used to ensure that the pressure in the tank always stays below 1.5 barg

Based on the above data, I have the following queries.

1. I am not sure how the volumetric Flow rate of Nitrogen has been calculated or mentioned as 1.8 m3/h. Any details on this
2. PCV0005 is a back pressure regulator, which shall be used to ensure that the pressure in the tank always stays below 1.5 barg. DO you think this is correct. What should be the correct pressure setting for the Back pressure regulator?
3. Is API2000 applicable in this case, because the design pressure of the tank is 3.5 barg, which I think does not fall under the preview of API2000?
4. Even though the tank is designed for Full Vacuum. There is no protection of the tank from FV. But the client has confirmed that breather valve is not required in this case. How is this correct?
5. How can we size the PSV?
6. The line sizes mentioned for the PSV outlet is 4". How is this sized?
7. The Back pressure regulator outlet is sized to 2". The incoming Nitrogen lines are sized to 1". How is this sizing done?
8. What implication does the vapor pressure of Methanol have on the Nitrogen Blanketting
9. Given these scenarios, what should be the set pressures for the PCVs and PSV?
10. What are the hazards involved in this case, when related to fire and explosion, based on the set points of the pressure.

I know these are a lot of questions. But I would like to get the help of a professional.


I tried contacting Mr. Ostand on the phone, but was not able to reach him. If someone could me provide some information regarding this problem, it would be of really great help.

Regards,
George Paulose.  nitrogen.xls   66KB   132 downloads

Edited by George paulose, 16 December 2009 - 01:30 PM.

[proinwv]

George, my apologies for not replying faster. Your question is extensive and I simply do not have the time to go through it today. I am loaded until December 22. If you can wait I will look at this. Possibly someone else will before then. You can contact me through my website, www.ostand.com

If you do, please let me know where you are located.

Paul

[fallah]

With lack of some required information (e.g. flowrates of other outflow/inflow than you mentioned) you can see below my response:

1-This is equal to maximum flowrate of methanol out of tank to the pump suction ( corresponding flowrate of pump end of curve if pump would be centrifugal).
2-I think it is correct.
3-Your thinking is correct.The tank is a pressure vessel.
4-Tank would be protected mechanically against FV.
5-By definition all possible scenarios and selecting worst case as a base for PSV sizing.
6-It should have been sized based on relief load in worst case and also available delta P between PSV outlet and end of discharge line (safe location).
7-Based on relevant maximum flowrate and corresponding delta P.
8-I think in your case higher the vapor pressure,lower the nitrogen consumption.
9-I think as:PCV0004 a little bit less than 1.5 barg(let say 1.45 barg)
PCV0005 1.5 barg
PSV0001 3.5 barg
10-Safety issue,if fire case would be applicable it should be considered in PSV sizing in overpressure point of veiw,....

Hope my inputs included points being useful for you.

Hi Fallah,

Thanks a lot for the info provided. All seems fine, except that the pumps which are used for the injection of Methanol are Triplex API 675 pumps (reciprocating pumps) having max capacity of 0.99 cu.m /hr. How did the client calculate the rate of Nitrogen required, since I feel that API 2000 shall not be applicable?

Quoting from API 2000:
"This standard covers the normal and emergency vapor venting requirements for aboveground liquid petroleum or petroleum products storage tanks and aboveground and underground refrigerated storage tanks designed for operation at pressures from vacuum through 15 pounds per square inch gauge (1.034 bar gauge"
Unquote

Regards,
George Paulose

[fallah]

How did the client calculate the rate of Nitrogen required, since I feel that API 2000 shall not be applicable?

Glad those info is useful for you.Certainly Mr. Ostand and other profissional members in this field can complete and modify my input.
In my opinion,1.8 m3/h as volumetric flowrate of Nitrogen submitted by your client is probably calculated as per normal condition (20 C,1 atm) rather than operating one (? C,1.5 barg).You may ask your client to explain in this regard.