Throttled pumps result in throttled profits.
Using valves to throttle pumps is not an ideal solution (I’m trying to be polite here), and here’s why.
Throttling is a reality that many plant operators and engineers are faced with, so let’s start by explaining what the dynamics of the process are and then look at the associated costs.
Throttling pumps is a counterproductive process as it implies spending money by adding energy to a fluid and then converting a portion of this energy to heat (to no useful purpose) using an expensive valve.
Very often, the valve is not suitable for this purpose and the result is high levels of cavitation and bad control characteristics. In the process, we create noise and vibration that have negative implications for the health and safety of staff.
Of course, there is also the matter of a marked increase in the operator’s energy bill.
To all of this, we need to add diminished plant reliability because of repetitive pump failures due to operation on a bad point of the curve.
Finally, to rub salt in the wound, when the valve needs to be closed so that maintenance can be done on the pump, the operator is likely to make an inconvenient discovery... 10% of the seat has been eroded by cavitation and the valve will not seal.
If the pipeline is long or there is a pressure vessel at the end of the line this could turn into a nasty situation.
Throttling example
Here’s an example. The diagram below shows two system curves superimposed on a pump’s performance curves. Curve A shows the as-designed curve while Curve B represents the curve obtained during commissioning.
- Duty point 1 represents the expected head and capacity as calculated by the design team.
- Duty point 2 represents the head and flow rate that were measured during commissioning.
- Duty point 3 represents the actual system head at the required capacity.
What went wrong?
The pump was oversized for its application.
Most often this results from conservative selection practices (e.g. multiple members of the design team add another 10% each ‘just in case’). Is this a common occurrence? According to European Pump Manufacturers Association (Europump) “most rotodynamic pumps, which constitute 80% of all pumps installed, are between 20% and 30% oversized”.
Whatever caused this pump to be oversized could be the subject of a whole new article.
Right now, I'm going to focus on the user’s approach to correcting the situation.
Essentially this revolves around partially closing the discharge valve in order to bend Curve B back to Curve A and the capacity from 352m3/hr to the designed 270m3/hr (full diameter impeller). The closing of the discharge valve increases the friction losses and forces the duty point back to the required flow.
At first glance, there appears to be no problem. The capacity is back to spec and the efficiency has risen from 70% to 82%. However, the partially closed valve has now increased the head from 35m (point 3) to 51m (point 1). We will look at the financial implications of this later.
The valve used to throttle the pump
It’s the standard knife/wedge/resilient seal gate or basic butterfly (rubber-lined) valve that is primarily designed for isolating duties. This being the case, the valve can only have two positions, fully open or fully closed — nothing in between.
But this application calls for the throttling valve to remain in a partially closed position. Because this is a control application, it requires the application of control valve sizing rules.
The two duty points show that there is a 17m (1,7 bar) difference in head (52m – 35m). At a flow rate of 270m3/hr, the Kv (flow coefficient) is:
A 150mm globe control valve, approximately 55% open is indicated from a number of manufacturer’s Kv tables. If a 100mm butterfly valve was used, then a +/-55° (61%) opening is called for.
What of the discharge pipe size?
A 150mm NB pipe will give a velocity in the region of 3,6m/s. Much too high.
The 2,2m/s of a 200mm NB pipe is better but is still a bit quick with limits on the possibility for future growth.
A 250mm pipe will give a velocity of +/-1,4m/s. There’s room for growth and the occurrence of pressure transients (hammer) is reduced. This is very attractive but would carry a higher capital cost (this could be offset by lower losses).
These sizes give some idea of the difference in dimensions between a pipe and any control valve that has to be incorporated into the system. In the case of the butterfly valve, it is quite possible to see a 100mm valve installed in a 250mm line! Not an everyday sight.
Here are some considerations for the selection of the valve types and materials of construction:
- Gate valves of any description are not suited for this application.
- Keep the throttling valve at least 5 X D from the pump discharge.
- The valve installed must have some form of facility that allows it to be locked out to avoid tampering.
- This type of installation usually has an operating life span of 15 years+ so a better-quality butterfly valve (if this is the pattern of choice) in a metal seat triple offset should be considered.
- A pressure gauge or sensor installed downstream of the valve is strongly recommended.
- There are cavitation consequences, even for this relatively low pressure drop. See the sigma calculation below.
So what’s so wrong about throttling?
Here are some points that quite frankly stick a knife in the throttling approach to pump control.
Cavitation and the Sigma Calculation
The point at which cavitation occurs and its relative severity can be estimated by calculating the cavitation index (sigma s) for a given application.
As a general rule of thumb, a sigma value of 2,7 will see the onset of incipient cavitation. Our figure of 3,1 indicates that cavitation will be present at the upper end of incipient to the lower end of constant.
The excess energy requirements and monetary costs (the final death knell for throttling!)
Some comments from a capital cost point of view
- Duty 1 will require a 55kW motor and appropriate supply transformer and controls.
- Duty 2 will require a 75kW motor
- Duty 3 will use a 37kW motor
In each case, the correctly sized transformer, switchgear, and baseplate will need to be provided. Duty 3 represents a very significant saving in all departments.
Additional power required for throttled operation:
If nothing was done to correct the "as commissioned" situation, then the increased power requirement would be 21,8kW.
If the pump was run for, say, 7000 hours per annum, and electricity cost R1/kW-hr, then energy costs would increase 7000 x 21,8 x R1 = R152 600 per year.
There would also be some serious maintenance issues that arise due to the bad duty point if the operator decided to open the throttle valve fully. This is a common occurrence.