Menu

Pressure Safety Valve Basic Design guide - Low pressure venting

Pressure Relief Valve sizing for atmospheric, low pressure tanks (pressure / vacuum)



1. Introduction and warning
2. Safety valve sizing - low pressure service

1. Introduction and warning

This design guide aims the reader at understanding the basic concepts behind the design and sizing of pressure relief valves for low pressure venting but not at designing a valve for operational purposes. It is based on published sources but should not be considered for the detail design and selection / ordering of a pressure safety valve. Indeed, pressure safety valves are of utmost importance for the safety of the process, as they are most often the last resort to avoid an explosion, their design must therefore be done only by reputable companies. Only after having clearly defined the application, the position of the valve...etc... with the valve supplier, can he advise properly the plant operator and finalize the design of the valve.

The calculation below are derived from API2000 5th edition and adapted from various sources. Those calculations are valid for gas only and for pressure < 15 Psig (1.034 bar g) and vacuum, they do not apply for external floating roof tanks or free vented internal     floating roof tanks. Other types of services will require a different calculation code. API for example has other standards for higher pressure gas service or liquid. ASME or ISO have their own guidelines.

Note that this page is not discussing the choice and calculation of the design scenario, which is the process events leading to the maximum flow released through the valve. The required flow must be defined thanks to a risk analysis and process calculations (API 2000 for example explains how to determine the required flow). Newer version of API 2000 have been published since 5th edition, the reader must consult them to get a full overview of sizing pressure safety valves for low pressure applications.

2. Safety valve sizing - low pressure service

2.1 Theory

For low pressure tanks, the following formula can be used (WARNING - This formula is not valid for gas at pressure > 1.034 barg and not valid for liquid, please refer to this page) :

Flow through low pressure safety valves

Equation 1 : flow through low pressure safety valve
With :
P1 = pressure at inlet in bar abs
P2 = backpressure at outlet in bar abs
A = minimum discharge area required of the safety valve in cm2
Q = theoretical flow through the valve in Nm3/h
k = ratio of specific heat
T = absolute temperature at inlet in K
M = molecular weight of gas
Z = compressibility factor at inlet conditions

The actual flow through the valve is lower than the theoretical flow. This non ideality is represented thanks to a coefficient of discharge of the valve, K.

K = Actual flow / Theoretical flow

The coefficient K is defined by the manufacturer. API 2000 5th edition is giving an example :Coefficient of discharge K of low pressure / vacuum safety valves

Figure 1 : Coefficient of discharge K of low pressure / vacuum safety valves

Depending on the technology of the valve chosen, either direct operated (weighed pallet valve) or pilot operated, an overpressure is required to reach the maximum flow. API 2000 is giving the following graph to estimate the overpressure per type of valve. It is very important to consider, especially for direct acting valve that will only reach their rated capacity at 100% overpressure. The tank protected must therefore be able to hold this overpressure.

Capacity / Overpressure characteristics of low pressure vents

Figure 2 : Capacity / Overpressure characteristics of low pressure vents

2.2 Practice

This kind of valve's flow is highly dependent on the design of the valve and actual overpressure allowable , it is recommended to refer to the manufacturer's flow table for a given valve, done according to API 2000. An example is give below :

Example of commercial low pressure safety valve capacity table

Once the valve is selected for the flow required for your application, then the actual flow considering the overpressure must be determined. Another table with a corrective coefficient is then given. If the overpressure acceptable is not the one of table 1, then the flow is to be corrected.

Example of correction factor commercial low pressure safety valve





WARNING
www.powderprocess.net cannot be held responsible for the use of the explanations, calculation and calculation tools presented here, the use of the information is at the user and its organization own risk and cost.

Source
Various sources based on API 2000 5th edition


Copyright www.PowderProcess.net

The content of PowderProcess.net is copyrighted but no warranty nor liability is ensured. The content of this site is to be seen as a help and important information and calculation must always be double checked by the user through the quality procedure of his organization or by checking another source. The user must always respect all applicable regulation. The use of the information is at the user and its organization own risk and own cost.

www.powderprocess.net is secured by SSL encryption

Follow us on Twitter