SOURCE MODELS. Prepared by Associate Prof. Dr. Mohamad Wijayanuddin Ali Chemical Engineering Department Universiti Teknologi Malaysia.
Associate Prof. Dr. Mohamad Wijayanuddin Ali
Chemical Engineering Department
Universiti Teknologi Malaysia
Most accidents in chemical plants result in spills of toxic, flammable, and explosive materials. For example, material is released from holes and cracks in tanks and pipes, from leaks in flanges, pumps, and valves, and a large variety of other sources.
Source models represent the material release process. They provide useful information for determining the consequences of an accident, including the rate of material release, the total quantity released, and the physical state of the material. This information is valuable for evaluating new process designs, process improvements and the safety of existing processes. Alternatives must be considered if the source models predict unacceptable release characteristics.
Source models are constructed from fundamental or empirical equations representing the physico-chemical processes occurring during the release of materials. For a reasonably complex plant, many source models are needed to describe the required to fit the specific situation.
Frequently the results are only estimates since the physical properties of the materials are not adequately characterized, or the physical processes themselves are not completely understood. If uncertainty exists, the parameters should be selected to maximize the release rate and quantity. This insures that a design is “on the safe side”.
Release mechanisms are classified into the wide and limited aperture releases. In the wide aperture case, a large hole develops in the process unit, releasing a substantial amount of material in a very short time. An excellent example is the over pressuring and explosion of a storage tank. For the limited aperture case, material is released at a slow enough rate that upstream conditions are not immediately affected; the assumption of constant upstream pressure is frequently valid.
Limited aperture releases are conceptualized in Figure 1. For these releases, material is ejected from holes and crack in tanks and pipes, leaks in flanges, valves, and pumps, and severed or ruptured pipes. Relief systems, designed to prevent the over pressuring of tanks and process vessels, are also sources of released material.
Figure 1 properties of the materials are not adequately characterized, or the physical processes themselves are not completely understood. If uncertainty exists, the parameters should be selected to maximize the release rate and quantity. This insures that a design is “on the safe side”. Various types of limited aperture releases.
Figure 2 shows how the physical state of the material affects the release mechanism. For gases or vapors stored in a tank, a leak results in a jet of gas or vapor. For liquids, a leak below the liquid level in the tank results in a stream of escaping liquid. If the liquid is stored under pressure above its atmospheric boiling point, a leak below the liquid level will result in a stream of liquid flashing partially into vapor. Small liquid droplets or aerosols might also form from the flashing stream, with the possibility of transport away from the leak by wind currents. A leak in the vapor space above the liquid can result in either a vapor stream or a two-phase stream composed of vapor and liquid depending on the physical properties of the material.
Figure 2 affects the release mechanism. For gases or vapors stored in a tank, a leak results in a jet of gas or vapor. For liquids, a leak below the liquid level in the tank results in a stream of escaping liquid. If the liquid is stored under pressure above its atmospheric boiling point, a leak below the liquid level will result in a stream of liquid flashing partially into vapor. Small liquid droplets or aerosols might also form from the flashing stream, with the possibility of transport away from the leak by wind currents. A leak in the vapor space above the liquid can result in either a vapor stream or a two-phase stream composed of vapor and liquid depending on the physical properties of the material. Vapor and liquid are ejected from processes units in either single or two-phase states.
There are several basic source models that are used repeatedly and will be developed in detail here. These source models are :
1. Flow of liquids through a hole
2. Flow of liquids through a hole in a tank
3. Flow of liquids through pipes
4. Flow of vapor through holes
5. Flow of vapor through pipes
6. Flashing liquids
7. Liquid pool evaporation or boiling
Other source models, specific to certain material, will be introduced in subsequent chapters.
A mechanical energy balance describes the various energy forms associated with flowing fluids,
P is the pressure (force/area)
r is the fluid density (mass/volume)
ūis the average instantaneous velocity of the fluid (length/time)
gc is the gravitational constant (length mass/force time²)
Flow of Liquid Through a Hole
a forms associated with flowing fluids, is the unitless velocity profile correction factor with the following values;
= 0.5 for laminar flow
= 1.0 for plug flow
-->1.0 for turbulent flow
g is the acceleration due to gravity (length/time²)
z is the height above datum (length)
F is the net frictional loss term (length force/mass)
Wsis the shaft work (force length)
m is the mass flow rate (mass/time)
The Δ function represents the final minus the initial state.
For incompressible liquids the density is constant and, forms associated with flowing fluids,
Consider a process unit that develops a small hole, as shown in Figure 3. The pressure of the liquid contained within the process unit is converted to kinetic energy as the fluid escapes through the leak. Frictional forces between the moving liquid and the wall of the leak converts some of the kinetic energy of the liquid into thermal energy, resulting in a reduced velocity.
For this limited aperture release, assume a constant gauge pressure, Pg, within the process unit. The external pressure is atmospheric; so ΔP - Pg. The shaft work is zero and the velocity of the fluid within the process unit is assumed negligible.
Figure 3 forms associated with flowing fluids, Liquid escaping through a hole in a process unit. The energy of the liquid due to its pressure in the vessel is converted to kinetic energy with some frictional flow losses in the hole.
The change in elevation of the fluid during the discharge through the hole is also negligible; so Δz = 0. The frictional losses in the leak are approximated by a constant discharge coefficient, C1, defines as
The above modifications are substituted into the mechanical energy balance, Equation 1, to determine ū, the average discharge velocity from the leak;
A new discharge coefficient, through the hole is also negligible; so C0, is defined as
The resulting equation for the velocity of fluid exiting the leak is
The mass flow rate, Qm, due to a hole of area A is given by
The total mass of liquid spilled is dependent on the total time the leak is active.
The discharge coefficient, through the hole is also negligible; so Co, is a complicated function of the Reynolds number of the fluid escaping through the leak and the diameter of the hole. The following guidelines are suggested.
1. For sharp-edged orifices and for Reynolds number greater than 30,000, Co approaches the value 0.61. For these conditions, the exit velocity of the fluid is independent of the size of the hole.
2. For a well-rounded nozzle the discharge coefficient approaches unity.
3. For short sections of pipe attached to a vessel (with a length-diameter ratio not less than 3), the discharge coefficient is approximately 0.81.
4. For cases where the discharge coefficient is unknown or uncertain, use a value of 1.0 to maximize the computed flows.
Example 1 through the hole is also negligible; so
At 1 p.m. the plant operator notices a drop in pressure in a pipeline transporting benzene. The pressure is immediately restored to 100 psig. At 2.30 p.m. a ¼-inch diameter leak is found in the pipeline and immediately repaired. Estimate the total amount of benzene spilled. The specific gravity of benzene is 0.8794.
The drop in pressure observed at 1 p.m. is indicative of a leak in the pipeline. The leak is assumed to be active between 1 p.m and 2.30 p.m., a total of 90 minutes. The area of the hole is
The density of the benzene is,
The leak mass flow rate is given by Equation 7. A discharge coefficient of 0.61 is assumed for this orifice-type leak.
The total quantity of benzene spilled is
A storage tank is shown in Figure 4. A hole develops at a height hL below the fluid level. The flow of liquid through this hole is represented by the mechanical energy balance, Equation 1, and the incompressible assumption as shown in Equation 2.
The gauge pressure on the tank is Pg and the external gauge pressure is atmospheric, or 0. The shaft work, Ws is zero and the velocity of the fluid in the tank is zero.
A dimensionless discharge coefficient, C1, is defined as follows.
Flow of Liquid Through a Hole in a Tank
Figure 4 height An orifice-type leak in a process vessel. The energy due to the pressure of the fluid height above the leak is converted to kinetic energy as the fluid exits through the hole. Some energy is lost due to frictional fluid flow.
The mechanical energy balance, Equation 1, is solved for height ū, the average instantaneous discharge velocity form the leak
where hL is the liquid height above the leak. A new discharge coefficient, C0, is defined as
the resulting equation for the instantaneous velocity of fluid existing the leak is
The instantaneous mass flow rate, height Qm, due to a hole of area A is given by
As the tank empties, the liquid height decreases and the velocity and mass flow rate will decrease.
Assume that the gauge pressure, Pg, on the surface of the liquid is constant. This would occur if the vessel were padded with an inert gas to prevent explosion or were vented to the atmosphere. For a tank of constant cross-sectional area At, the total mass of liquid in the tank above the leak is
where Qm is given by Equation 12. By substituting Equations 12 and 13 into Equation 14 and assuming constant tank cross section and liquid density, a differential equation representing the change in the fluid height is obtained.
Equation 15 is rearranged and integrated from an initial height hLo to any height hL.
The equation is integrated to
Solving for hL, the liquid level height in the tank, yields
Equation 18 is substituted into Equation 12 to obtain the mass discharge rate at any time t.
The first term on the RHS of Equation 19 is the initial mass discharge rate at hL = hLo.
The time for the vessel to empty to the level of the leak, te, is found by solving Equation 18 for t after setting hL = 0.
If the vessel is at atmospheric pressure, Pg= 0 and Equation 20 reduces to
Example 2 mass discharge rate at any time
A cylindrical tank 20-feet high and 8-feet in diameter is used to store benzene. The tank is padded with nitrogen to a constant, regulated pressure of 1 atm gauge to prevent explosion. The liquid level within the tank is presently at 17 feet. A 1-inch puncture occurs in the tank 5 feet off the ground due to the careless driving of a fork lift truck. Estimate
a. the gallons of benzene spilled,
b. the time required for the benzene to leak out, and
c. the maximum mass flow rate of benzene through the leak.
The specific gravity of benzene at there conditions is 0.8794.
The density of the benzene is mass discharge rate at any time
The area of the tank is
The area of the leak is
The gauge pressure is
a mass discharge rate at any time . The volume of benzene above the leak is
This is the total benzene that will leak out.
b. The length of time for the benzene to leak out is given by Equation 20
This appears to be more than adequate time to stop the leak or to invoke an emergency procedure to reduce the impact of the leak. However, the maximum discharge occurs when the hole is first opened.
c. The maximum discharge occurs at t = 0 at a liquid level of 17.0 feet. Equation 19 is used to compute the mass flow rate.