This TechNote explains how the Hydropneumatic Tank element works and its typical application in HAMMER V8i. It also provides an example model file for demonstration purposes.
The Hydropneumatic Tank element in HAMMER represents a cylindrical or spherical pressure vessel containing fluid at the bottom and an entrapped gas (usually air or nitrogen) overlying the liquid. It is sometimes referred to as a Gas Vessel, air chamber or pressurized surge tank.
When the hydropneumatic tank is being filled (usually from a pump), the water volume increases and the air is compressed. When the pump is turned off, the compressed air maintains pressure in the system until the water drains and the pressure drops. This storage of energy as compressed air allows for a high hydraulic grade to be achieved in a relatively small tank, whereas the traditional, unpressurized surge tank would need to be constructed as high as the hydraulic grade you need to achieve. This is because the hydraulic grade in a hydropneumatic tank is the elevation plus the water level PLUS the pressure head of the gas above it, whereas in a surge tank, it is the water surface elevation. Thus, a surge tank is typically not practical for a high head system.3 So, If the hydropneumatic tank contains enough (pressurized) gas to prevent water columns from separating, it can be a very effective way to avoid or reduce pressure surges.
The most common use of a hydropneumatic tank for surge protection is for controlling transients caused by rapid pump start up and shut down. In a typical emergency pump shutdown scenario, the low pressure 'downsurge' can cause severe subatmospheric pressure. Column separation can occur and severe high pressure 'upsurges' can occur upon vapor pocket collapse. So, protective equipment is often necessary to provide water and head to the system upon downsurge and also to bleed water out of the system upon upsurge. Most often the best protection for this situation is either a surge tank or hydropneumatic tank, since they can provide this water and head during a transient event.
The hydraulic grade provided by a surge suppressing hydropneumatic tank must be high, and typically will operate at normal pipeline pressure. Meaning, the normal pressure at the tank is the same pressure that would occur if the tank were not installed at all. This is different from 'normal' hydropneumatic tanks in water distribution systems, which typically cycle quickly based on hydraulic grade pump controls.
Note: Adding surge-control equipment or modifying the operating procedures may significantly change the dynamic behavior of the water system, possibly even its characteristic time. Selecting appropriate protection equipment requires a good understanding of its effect, for which HAMMER V8i is a great tool, as well as the good judgment and experience you supply.
If you have decided to model a hydropneumatic tank for surge protection, there are several considerations for its design. Each of these can impact the effectiveness and cost of the device and must be carefully evaluated. For further guidance on sizing of the hydropneumatic tank, we suggest the book 'Fluid Transients in Pipeline Systems' by A. Thorley.
A hydropneumatic tank is typically installed just downstream of a pump station, so as to keep the water column moving upon pump shutdown. It is typically installed inside an enclosed building and is sometimes 'twinned' (two of the same tank side by side) for maintenance and redundancy purposes. 3
If the hydropneumatic tank location is uncertain or if more than one may be required, you can compute the transient simulation without any protection and check your results (such as the min/max pressure envelope in the Transient Results Viewer.) By viewing these results, you can see critical areas of the pipeline and potentially find a good location candidate for the hydropneumatic tank(s). You can then add your hydropneumatic tank(s), re-compute the transient simulation, re-check the results and make adjustments as necessary.
Note: Sometimes a tank may be required on the suction side of a pump station as well, to prevent cavitation upon pump shutdown/startup. Be sure to check the minimum pressure results upstream of the pump for your transient simulation.
The pipe connecting from the main pipeline to the hydropneumatic tank can be modeled in HAMMER either implicitly or explicitly. Basically when laying out the hydropneumatic tank, it can be modeled at a 'Tee' by laying out the connecting pipe, or can be modeled directly on the main line. When modeling on the main line (the typical approach), the influence of the short piping between the main and the tank can be represented by means of the tank inlet diameter and minor loss coefficient fields.
Although explicitly entering the short connecting pipes to the vessel is not incorrect in principle, it may lead to excessive adjustments in pipe length or wave speed which in turn may have an impact on the results. This adjustment commonly occurs with short pipes, due to the fact that HAMMER must have a wave be able to travel from one end of the pipe to the other end in even multiples of the time step. So, since you can model the connecting pipe head losses via the minor loss coefficient field, it is often best to model the tank inline. However, you must also consider the effects of water momentum. For example if you're modeling large flows and large diameter pipes, the effects of accelerating that relatively large volume of water (in the connecting pipe) upon emergency pump shut down may be significant.
If you are simulating an emergency pump shutdown event, it may be possible to have a condition where a single hydropneumatic tank at the pump station cannot provide adequate protection. For example, if there is an intermediate high point between the pump and the downstream boundary tank/reservoir, even if your initial hydropneumatic tank pressure is high, it will eventually drain down to a hydraulic grade that causes sub-atmospheric pressure at the high point. So, it is important to also consider the length of time that the pump will be shut down. You will likely want to simulate the worst case scenario though, so in this situation you may need additional protection, such as an air valve or additional tank near the high point. For example, consider the following pipeline profile with an emergency pump shutdown:
Dark black line = physical elevation.Dashed black line = steady state / initial conditions head.
As you can see, the addition of a hydropneumatic tank (gas vessel) just downstream of the pump station does not offer enough protection. Sub-atmospheric pressure occurs at the downstream end of the system, due to the high point. Even with an air valve at the high point, the longer the pump is off, the more air will be introduced into the system. The addition of a surge tank at said high point does well at alleviating this problem.
Note: It is important to note that using air chambers and surge tanks in treated drinking water systems can result in water quality deterioration and loss of disinfectant residual. These devices should be equipped with a mechanism for circulating the water to keep it fresh. A further complication occurs when the tanks are located in cold climates where the water can freeze. If freezing is an issue, smaller air chambers that can be housed in heated buildings are preferable.1
Although the total size of the hydropneumatic tank is important, it is not directly used in HAMMER unless you're using a bladder (which is covered later in this TechNote). Instead, you define the initial hydraulic grade and corresponding gas volume, then view the transient results to see how much the gas expanded.
Basically your hydropneumatic tank needs to be large enough so that it does not become empty during the transient simulation. HAMMER assumes that the water volume in the tank is enough so that this does not happen. In the Transient Analysis Output Log (Under Report > Transient Analysis Reports), you will see the maximum volume of gas that is needed during the transient analysis. You will then need to provide a hydropneumatic tank that will be able to accommodate that maximum volume of gas and still not become empty of water (assuming that you don't want it to become empty of course.)
When you're not using the bladder option, you must enter a total volume for the hydropneumatic tank (the "Volume (Tank)" field), but this is for reference purposes during the transient simulation. If the volume of gas during the transient simulation exceeds the total tank volume that you entered, you'll encounter a User Notification about the maximum gas volume being greater than the entered tank volume. However, HAMMER will still compute gas volumes above the total tank volume, based on the gas law. Not only will this indicate that there is something wrong, but it will also indicate by how much. Meaning, the user can view the maximum gas volume required (in the text output log) with the current tank configuration, make the necessary adjustments, then re-run the simulation.
For example, a user entered 500 L as the initial gas volume and 1500 L as the total tank volume, but the output log shows a maximum gas volume of 1640 L. This means that during the transient simulation, the head dropped so low that the expanded gas volume occupied more than 1500 L. It tells the user that their desired tank is almost big enough, but not quite.
In case this situation occurs, it's important to realize that the total tank size is not necessarily the only factor. For example, if the initial gas volume at the steady state hydraulic grade was smaller, the maximum gas volume during the transient may be less and within the desired total tank size. Other things such as a differential orifice can also influence the effectiveness of a tank that is a certain size. So, just because the reported gas volume is higher than the tank size you'd like, it doesn't necessarily mean that you need a bigger tank. You may be able to control the maximum gas volume by changing other parameters, therefore allowing the same tank size to be used. Since you may be limited (due to cost, physical space or other reasons) in terms of the largest tank size you can provide, adjustment of these other things may be necessary. With HAMMER, you can easily test different configurations of your tank to find the optimized protection for your pipeline.
In some cases, you may have a requirement stating that a certain percentage of the tank volume must be liquid in the steady state conditions. You may also have a limit on the total tank size, maximum pressure, bladder pre-charge pressure, etc. So, you'll need to design around these requirements.
The piping connection between the hydropneumatic tank and the system should be sized to provide adequate hydraulic capacity when the chamber is discharging, as well as to cause a head loss sufficient to dissipate transient energy and prevent the chamber from filling too quickly. Both of these requirements are met through the use of a piping bypass as depicted below.1
In HAMMER, the headlosses associated with this can be modeled by using the "Minor Loss Coefficient", "Ratio Of Losses" and "Diameter (Tank Inlet Orifice)" attributes of the hydropneumatic tank. This is referred to as the differential orifice, because the ratio of losses allows you to have the inflow headlosses different from the outflow headlosses. In the above illustration, you can see that the check valve causes inflows to undergo larger headlosses as water passes through the bypass. So, the ratio of losses attribute is usually larger than 1.0 and applies to inflows.
The "minor loss coefficient" that you enter is used for tank outflows. For tank inflows, the minor loss coefficient is multiplied by the "ratio of losses" and the resulting coefficient is used. The effect of a differential orifice can be large for some systems.
Note: you may consider adjusting the minor loss coefficient to represent multiple losses through the tank assembly. For example you may have minor losses from bends, fittings, the tank inlet itself and the differential orifice assembly. In this case, you can set the "minor loss coefficient" value to represent all those losses, but remember that the velocity used to calculate them is based on the area of the "diameter (tank inlet)". Also, you'll need to set up the ratio of losses such that the losses through the entire tank assembly appropriately accounts for the additional loss through the bypass of the differential orifice.
Consider the below profile, showing the maximum transient head for a pipeline during an emergency pump shutdown event. The inlet orifice size was decreased by 75 mm and a minor loss coefficient of 1.5 was used, with a ratio of 2.5. As you can see, it helps reduce the maximum transient pressures in the system. This could also mean a possible reduction in total required tank size.
A flexible and expandable bladder is sometimes used to keep the gas and fluid separate in the hydropneumatic tank. Since there is no contact between the compressed air and the water, there is no dissolution. There is thus no requirement for a permanent regulation system such as an air compressor, which is otherwise typically required (since the gas slowly dissolves into the water). 2
When using a bladder, a 'pre-charge' pressure is first applied, before the tank is connected to the system and submitted to pipeline pressure. Transient protection performance when using a bladder-type tank tends to be sensitive to the pre-charge pressure, since it determines the initial gas volume and sensitivity to pressure changes. Sometimes you may have a requirement on the pre-charge pressure, such as being 5% of the normal pipeline pressure. Otherwise, you may need to use trial and error to find the best pre-charge pressure.
When using the bladder tank option, prior to and during a transient computation:
After the simulation is complete, you can look in the text output files to see what the preset pressure, pre-transient volume (at system pressure) and subsequent variations in pressure and volume have occurred.
When using a hydropneumatic tank just downstream of a pump station, check valve slam is a common concern. This is because after the low pressure transient from a pump shutdown event, the tank maintains a high downstream hydraulic grade, which quickly causes the check valve downstream of the pump to close. So, a non-slam check valve is typically used in these cases.
The user must carefully model the check valve by considering its behavior. By default, the check valve node element and check valve property of a pipe assume an instantaneous closure upon first detection of reverse flow. This means no reverse velocity will build up before closure occurs. If this doesn't match the behavior of your check valve, be sure to use the "Open Time", "Closure Time" and "Pressure Threshold" options for the check valve node element. This allow you to model the delay in opening and closing of a check valve.
As with any transient simulation, a model with a hydropneumatic tank must begin in a steady state condition. HAMMER uses the WaterGEMS hydraulic engine to compute the steady state initial conditions, which are used as the starting point for the transient simulation. For a hydropneumatic tank, the initial conditions provide a hydraulic grade and inflow/outflow to the transient calculation engine.
Typically the initial conditions are computed as a steady state (by selecting "steady state" as the "time analysis type" in the steady state/EPS solver calculation options, which is the default.) If you must compute an Extended Period Simulation (EPS), be aware that you will need to select a time step for the transient calculation to use as its initial conditions (Using the "initialize transient run at time" transient calculation option). You will also likely need to use a small hydraulic time step (selected in the steady state/EPS solver calculation options), since a hydropneumatic tank typically cycles relatively quickly. With EPS, you will likely also need to set up controls for your pump based on the tank hydraulic grade. Lastly, the change in HGL/volume during the EPS is calculated using either a constant area approximation or the gas law, depending on the selection of "tank calculation model."
However, when modeling a hydropneumatic tank that is meant for transient surge protection, it typically operates under 'line' pressure, so you usually don't need to analyze changes during EPS. The typical approach is to use a steady state simulation as the initial conditions and select "true" for the "treat as junction" attribute (see below).
As mentioned above, in many cases a hydropneumatic tank may be implemented only for transient protection. During a steady state condition, the tank may simply operate under the corresponding normal / steady state head ("line pressure"). So, for simplification, it is sometimes preferable to select "true" for the "treat as junction" attribute in the tank properties. Doing this allows the initial conditions solver to compute a hydraulic grade at the tank location, and the user simply assumes that the tank has already responded to the hydraulic grade and the air volume has expanded or contracted accordingly. In this case, the user only needs to enter the initial volume of gas under the "transient" section of the tank properties that corresponds to that initial conditions hydraulic grade (unless using a bladder). It is important to remember that the tank is only treated as a junction in the initial conditions. During the transient simulation, it is still treated as a hydropneumatic tank. Basically treating it as a junction in the initial conditions is another way of establishing the initial hydraulic grade. The transient simulation will use that hydraulic grade along with the gas volume as the starting conditions. The gas will then expand and contract accordingly during the transient simulation, based on the gas law.
If you already know the hydraulic grade that you'd like to use as the initial conditions, you would choose "false" for "treat as junction?" and enter it under the "physical" section of the tank properties. The initial conditions solver will then compute the flow/head in the rest of the system, with the hydropneumatic tank as the boundary condition. In this case, the tank will likely have either a net inflow or outflow, to balance energy across the system. So, your transient simulation may not begin at a true "steady" condition.
The following attributes of the hydropneumatic tank influence the initial conditions calculation (steady state or EPS). You'll notice that they are all within the "Operating Range" or "Physical" section of the hydropneumatic tank properties.
Note that said computed hydraulic grade still represents the water surface PLUS the air pressure head - it is the total head at that point in the system (see further above for more information on the "Treat as Junction" attribute). So, let's say for example you ran a steady state, treating the tank as a junction to find the 'balanced' head in the tank (as if it already responded to the system conditions) but then wanted to change it back to being treated as a tank (for purposes of analyzing the behavior in an EPS simulation or something else), yet still begin the simulation with the same, balanced head. To do this, you would copy the computed hydraulic grade (from the results section of the properties) into memory, set "Treat as Junction?" to "False", then paste that hydraulic grade value into the "HGL (Initial)" field. When re-computing initial conditions, the initial results will then be equivalent to the original case where the tank was treated as a junction.
Note: The "atmospheric pressure head" field is not used during the transient simulation. The transient calculation engine assumes an atmospheric pressure head of 1 atm or 10.33 m.
For the initial conditions, the user must select either "gas law" or "constant area approximation" for the "Tank calculation model" attribute of the hydropneumatic tank. The constant area approximation selection exposes the "Volume (effective)," "HGL on," and "HGL off" fields. The gas law selection exposes the "Atmospheric pressure" field. These fields are primarily there to support the WaterCAD and WaterGEMS products, which can directly open a HAMMER model. They are only used to track the change in HGL/volume for EPS simulations, which typically aren't used in HAMMER. A transient analysis typically begins with a steady state simulation, which only considers the "HGL (Initial)" and "volume of gas (initial)". This is because a steady state simulation is a snapshot in time, so the head/volume are not changing. So in most cases, it does not matter which tank calculation method you choose. You will likely want to select "gas law" for simplicity, but additional information on both approaches is provided below.
Both methods typically yield similar results within the "effective" control range, but the gas law is technically more accurate.
The following section explains how HAMMER handles hydropneumatic tanks during the transient simulation. There are two distinct tank configurations: with a bladder and without a bladder.
The transient simulation uses the hydraulic grade from the initial conditions, along with the initial gas volume, which is either user-entered (if "treat as junction" = true") or calculated based on the difference between the "Volume (tank)" and "Liquid Volume (Initial)" (if "treat as junction" = false). As pressure in the system drops due to a downsurge, this gas volume expands and water injects into the system. Pressure upsurges cause the gas to compress as water re-enters the tank. This compression and expansion occurs in accordance with the isothermal gas law. A constant number of moles / mass of gas in the tank and constant temperature is assumed, so the 'nRT' term in the gas law equation is replaced by a constant, K. Thus, the equation used is PVk=K, Where P = absolute pressure (feet or meters), V = gas volume (cubic feet or cubic meters) and k is the Gas Law Exponent specified in the tank properties. Thus, the constant K is computed from the initial gas volume raised to the exponent, multiplied by the initial pressure. The pressure P is the initial hydraulic grade minus the tank physical elevation, plus atmospheric pressure (1 atm or 10.33 m). This way, a new air volume can be computed based on pressure changes during the transient simulation.
For example, consider a tank who's initial gas volume is 0.8 m3 , initial hydraulic grade is 150 m, physical elevation is 100 m and gas law exponent is 1.1. From this, HAMMER computes the "K" constant as: (150 - 100 + 10.33)(0.81.1) = 47.2. Since K is known now, the change in pressure can be computed based on changes in volume due to inflow/outflow. For example, say that the tank filled such that the gas volume was compressed to 0.5 m3. Based on the K constant of 47.2, this means that the corresponding pressure = (47.2) / (0.51.1) = 101.175 - 10.33 = 90.845 m. (a hydraulic grade of 100 + 90.845 = 190.845 m)
Note: In the formula above, the pressure P is measured from the bottom of the tank (the physical elevation). This is because by default, HAMMER does not track the liquid level in the hydropneumatic tank. This assumption should be fine in most cases, because these tanks are usually relatively small and thus the change in liquid level would have a minimal impact. However if you'd like HAMMER to be able to account for the liquid level (water height), check out the section further down in the TechNote called "Tracking the Liquid Level".
Note: In HAMMER 08.11.01.32+, the "Volume of gas (Initial)" field only needs to be entered if your hydropneumatic tank is treated as a junction or if you are choosing to specify custom initial conditions (and are not using a bladder). In other cases, the initial gas volume is derived from the total tank volume minus the initial liquid volume.
If your hydropneumatic tank has its gas contained within a bladder, then you must enter a gas preset pressure. This is the pressure inside the bladder before the tank is submitted to pipeline pressure. Since this means that the gas takes up the entire tank volume, the constant K in the gas law (PV = K) is computed based on this preset pressure and the full tank volume, "Volume (Tank)." The transient simulation's initial gas volume is then computed based on the K constant and the initial conditions hydraulic grade. The initial conditions hydraulic grade is either the user-entered value in the "HGL (Initial)" field, or the computed steady state hydraulic grade, depending on the "treat as Junction?" selection.
For example, consider a tank that has been given a full volume of 500 L and the initial conditions pressure head is 50 m. Assume that the pre-charge pressure is 5% of the steady state pipeline pressure. So, the gas preset pressure is set to 2.5 m. In this case, the 'K' constant is computed as (2.5 m + 10.33 m)(0.5 m3) = 6.415. Since K is known now, the initial gas volume for the transient simulation (after the bladder is submitted to pipeline pressure) is computed as V = K/P = (6.415)/(50 m+10.33 m) = 0.106 m3 = 106 L.
Note that the gas law exponent is assumed to be 1.0 in this particular calculation for finding the initial gas volume of the transient simulation. Once the transient simulation begins, the gas law exponent entered in the tank properties (which defaults to 1.2) is used for calculating changes in gas pressure/volume.
Intuitively, as long as the gas preset pressure is lower than the pipeline pressure in steady state, the initial volume of gas in the tank will be less than the total volume. Typically, the preset pressure is relatively small, but that may not always be the case. Below is a comparison of two possible bladder tank configurations (at opposite extremes of the spectrum) for a particular system, with an emergency pump shut down event.
Observe the graph of time vs. head at the tank location, summary of min/max gas pressure (in meters) and gas volume (in cubic meters) along with transient profile envelope (blue line is minimum head, red line is maximum head.)
In the first case, the pre-charge pressure is 5% of the pipeline pressure, with a 500 L tank. In the second case, the pre-charge pressure is 80% of the pipeline pressure, with a 13,000 L tank. With a low preset pressure, the bladder is initially compressed to a relatively small size. So, it is less likely for the tank to drain completely, and thus a relatively small tank size is used without becoming empty. However, per the gas law, the rate of pressure decrease will be higher for a vessel with a lower preset pressure. So, the graph and profile show minimum and maximum transient pressures that may be too extreme for this system. On the other hand, with the high preset pressure case, the bladder isn't compressed by very much when submitted to pipeline pressure. So, a much larger tank size is required to prevent the entire tank from draining of water. However, in contrast to the low preset pressure case, the minimum and maximum transient pressures are much more reasonable. As you can see, the modeler needs to closely examine what is happening in the results for certain tank configurations. Testing different preset pressure values is something you can easily do in HAMMER to see the effects of either option. The text output logs can show you the gas volumes are pressures during your simulation.
Note: Remember that HAMMER assumes that the size of your hydropneumatic tank is large enough so that it does not become completely empty. So, regardless of whether you are using a bladder or not, if the volume of gas exceeds the total tank volume during the transient simulation, a notification will be displayed, but gas volumes above the total tank/bladder volume will still be calculated since HAMMER cannot model an empty tank. A gas volume in excess of tank volume tells you is that the tank you used is not sufficient and you will likely need to consider a different preset pressure, larger tank, different configuration, additional protection, etc.
The following hydropnematic tank attributes influence the transient simulation calculation:
Note: In version 08.11.01.XX and greater, if you are not specifying initial conditions and not treating the tank as a junction, then the initial gas volume is not required and the field will not show up. This is because it is either computed from the initial conditions gas volume (which is the full tank volume minus the initial liquid volume for a steady state) or based on the preset pressure (if using the bladder option)
Note: In some cases, you may want to analyze a range of different initial conditions, which could potentially change the starting hydraulic grade of your hydropneumatic tank. The gas law can be employed in this case. For example, if you know the initial gas volume is 300 L at a steady state pressure head of 50 m, you can compute the 'K' constant using the gas law, PVk=K: (50 m + 10.33 m)(0.3 m3) = 18.099. (gas law exponent assumed to be 1.0) So, if your new steady state pressure head is 30 m, the new initial gas volume (which you must enter) is computed as V = (18.099)/(30 m+10.33 m) = 0.449 m3 = 449 L.
Note: The transient calculation engine always uses an atmospheric pressure head of 1 atm or 10.33 m when solving the gas law equation.
There are many ways to view the results of your transient simulation. For a hydropneumatic tank, some results are available in the powerful Transient Results Viewer tool and some are found in the text output.
Note: Do not confuse initial conditions results with transient results. The result fields in the "Results" section of the hydropneumatic tank properties pertain to the initial conditions calculations only. For example, if you right click the tank, choose "graph" and choose "gas volume (calculated)", this will not show you the gas volume during the transient simulation - it will be for the initial conditions only (specifically EPS initial conditions).
The primary tool for viewing results is the Transient Results Viewer. To prepare for its use, first ensure that your transient calculation options are set up correctly (Analysis > Calculation Options). Choose some elements under "Report points", choose the desired report times and select "true" for "generate animation data". Next, create a profile of your pipeline under View > Profiles. Next, compute your model and go to Analysis > Transient Results Viewer.
To see the transient envelope, select your profile path and click "plot". To see how the head and vapor volume changes over time throughout your profile, click the "animate" button and use the animation controls. This will give you a good visualization of how the hydropneumatic tank performs. To see graphs of HGL, flow and/or vapor volume over time, select one of your report points under "Time Histories", select the attribute to graph and click plot. For example, you may want to see the flow and head at the hydropneumatic tank location.
Note: the "volume" reported in the transient results viewer is only air or gas introduced into the pipeline. It does not show the volume of gas inside the hydropneumatic tank itself. The same applies to the "air volume (maximum, transient)" field shown in the "Results (Transient)" section of the hydropneumatic tank properties.
Beginning with HAMMER V8i SELECTseries 5, additional results are available in the Transient Results Viewer. These were previously only available in text reports. For hydropneumatic tanks, these include results for gas volume, gas pressure, water level, and water inflow. To access these, choose the Extended Node Data tab in the Transient Results Viewer.
HAMMER's text output results also offer important information for hydropneumatic tanks. To prepare for viewing this information, first check your transient calculation options. "Show standard output log" and "Enable Text Reports" should be set to "true". Next, enter a number for the "report period" field of your hydropneumatic tank. This represents how often extended text results will be reported. For example, if your time step is 0.01 seconds and you enter '10' for the report period, it means you'll see extended text results every 10 time steps or every 0.1 seconds.
As mentioned above, some of these results are available in the Extended Node Data tab in the Transient Results Viewer. For users with older versions of HAMMER, they will still need to use the steps below to view the results.
The first text report of importance is the Transient Analysis Output Log, under Report > Transient Analysis Reports. Scroll down to the section starting with "THE EXTREME PRESSURES AND VOLUMES". This part of the report summarizes the maximum and minimum gas pressure and volume for the transient simulation.
Lastly, to see a table of extended hydropneumatic tank results, open the Transient Analysis Detailed Report, under Report > Transient Analysis Reports. Scroll down near the bottom, to the section starting with " ** Gas vessel at node" and you will find a table of gas volume, tank hydraulic grade, pipeline hydraulic grade and tank inflow, over time. The difference between the "head-gas" and "head-pipe" is the headloss induced by the minor loss coefficient at the tank's connecting pipe. Negative values for "inflow" represent tank outflow.
Currently HAMMER cannot automatically provide a graph of this data - you must manually generate a graph using an external application such as Microsoft Excel. Here are the steps, assuming Microsoft Excel 2007:
In previous versions of HAMMER (08.11.00.30 and below), HAMMER did not track the liquid level (elevation of the interface between the liquid and the gas) and essentially assumed that it was fixed. As of HAMMER V8i SELECTseries 1 (08.11.01.32), HAMMER now supports tracking of the liquid/gas interface, via the "Elevation Type" field in the Hydropneumatic tank properties. This field presents 3 options, Fixed, Mean Elevation and Variable Elevation.
This is the default option for the "Elevation Type" field and is consistent with the behavior of previous versions. The liquid elevation is assumed to be at a fixed location during the transient simulation, equal to the bottom of the tank. The gas pressure used in the gas law equation is the pressure above the user-entered "elevation" field, accounting for liquid pressure plus the air pressure.
This is acceptable for most cases, mainly because the elevation difference between the range of possible liquid levels is typically quite small. So, it does not account for much of a pressure difference. This can be observed by adjusting the "Elevation" attribute in the tank properties.
Selecting "Mean Elevation" exposes the "Liquid Elevation (Mean)" field, which allows you to specify a custom liquid (water surface) elevation, instead of assuming it is equal to the tank bottom (as is with the "fixed" option). It represents the average elevation of the liquid/gas interface throughout a transient. This is useful in cases where the liquid elevation is significantly higher than the tank bottom, but doesn't move significantly during a transient simulation. So, although no tracking of changes in liquid elevation occurs, it allows you to get a more accurate calculation in some cases. The gas pressure used in the gas law equation during the calculations is the pressure above the mean elevation that you enter.
Selecting "Variable Elevation" exposes the "Variable Elevation Curve" field, which allows you to enter a table of liquid elevation versus equivalent diameter. The variable level hydropneumatic tank type is for users who have detailed information about the tank's geometry and want to perform as accurate a simulation as possible. Typically, this type of representation would be selected in the detailed design stage. It would also be appropriate in the case of low-pressure systems and/or relatively tall tanks with large movements of the interface relative to the HGL of the gas. The initial liquid level is determined from the initial gas volume which is an input parameter. The tank cross-sectional area at any elevation is interpolated from an input table of the vessel's geometry spanning the range from the pipe connection at the bottom to the top of the tank.
After computing the transient simulation with a variable elevation hydropneumatic tank, you can view the liquid level over time by looking at the Transient Analysis Detailed Report. This report is found under Report > Transient Analysis Reports and will show this extended, tabular data for the tank when you've entered a value for the "report period" property of that tank (see "Text Reports" further above).
Note: You must be using at least version 08.11.02.31 of HAMMER in order to use the variable elevation option with a bladder.
There are other types of hydropneumatic tanks which can be modeled in HAMMER. Detailed information on how this work can be found in HAMMER's Help documentation. In addition, the hydropneumatic model sample file in HAMMER V8i SELECTseries 5 and later has a scenario that includes dipping tube and vented hydropneumatic tanks. These can be used to get a general idea of how the input is entered for these.
This type of hydropneumatic tank has an air valve that admits air into the system from the atmosphere, when the tank drops below atmospheric pressure. (Walski, 2007). A vented hydropneumatic tank is effectively a sealed tank with the addition of an air valve at the top. This allows air at atmospheric pressure to enter the tank during a downsurge so that the device behaves like a one-way surge tank. During an upsurge, the air valve typically throttles the air outflow so that the gas within the tank is compressed and acts as a 'cushion' against transients (just like a sealed hydropneumatic tank). This device offers several practical benefits - for example since the tank typically has no gas inside, there is no need for compressors or a bladder to ensure a required gas volume is maintained.
A dipping tube hydropneumatic tank has a dipping (or ventilation) tube inside with an air valve at the top. During normal operation the air valve is closed, the water level is above the bottom of the dipping tube, and gas is compressed in the 'compression chamber'. If the hydraulic grade line drops (e.g. after a pump stop) the dipping tube tank acts like a regular (sealed) hydropneumatic tank until the water surface drops below the bottom of the dipping tube, after which the air valve opens and allows air to enter at atmospheric pressure. At this point the tank is acting like a surge tank that is open to atmosphere. If the hydraulic grade line increases again (e.g. if pumps come on), air will be expelled until the hydraulic grade line rise enough to close the air valve. At this point the water surface will be above the bottom of the dipping tube and the tank will act like a regular sealed hydropneumatic tank once again. HAMMER uses air inflow orifice diameter in venting calculation.
For Dipping tube type hydro-pneumatic tank, the tank elevation-area curve is used to calculate the tank volume. Before the air in the dipping tube tank is compressed, the air volume is the tank volume above the bottom elevation of the dipping tube. When the air is compressed, gas law equation and Newton iteration method is used to calculate the water level and air volume in the tank.
Before the air is compressed, the air pressure is Atmospheric pressure, the air volume is the tank volume above the bottom of the dipping tube. When the air is compressed, the water level is calculated using Newton method. Using the gas law equation, iterative method Newton method is used to calculate water level in the tank (in the gas law equation calculation, the pressure of the air is: Atmospheric pressure + pressure head - level). The air volume calculated in the dipping tube vessel depends on the Gas Volume. If the Gas Volume includes the air volume in dipping tube, the existing way is correct. If the Gas Volume does not include the air in the dipping tube, we should exclude dipping cross-section area from the tank cross-section area.
To calculate the initial air volume, the elevation-area curve is used, along with the initial HGL and the elevation of the bottom of the dipping tube. Depending on the configuration, the compression chamber volume may be derived from the elevation-area table alone, not from the "Volume (compression chamber)". Since the volume of the dipping tube itself was not subtracted, this may cause an the unexpected initial gas volume.
In an update to HAMMER V8i SELECTseries 5, the volume of the dipping tube is excluded from the volume of the compression chamber (which again is derived from the elevation-area curve.)
Addition information can be found here: http://www.charlatte.fr/2006/csae/dc/spt0140.pdf
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Note: the above model is for example purposes only. It can be opened in version 08.11.01.32 and above and you can find additional information under File > Project Properties.
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