I recently received a phone call and subsequent email stating “my self-priming pump is not priming”. Both the phone call and the email were detailed with pictures and appropriate information to start the troubleshooting process.

The pump was a model 2796 MTO 6 X 6 – 13 with a 10.625” diameter impeller turning at 1750 RPM. The design point was 1000 GPM at 85 feet of head and the liquid was pond water at ambient temperature. The 6-inch suction piping was approximately 60 feet long and extended down to the pond with a check valve located only 30 feet from the pump. We did not know the depth or submergence of the suction piping into the pond. The suction “lift” was 23 feet. The issues with this application are at the end of the article.

 

 

In pump school we review self-priming “do’s and don’ts” and have developed
a check list of items to review if you are having a problem:

    • Even a self-priming pump must be primed initially.
      Fill the priming chamber with liquid.
    • Is the required lift is too high?
      No more than 25 feet: lower depending on temperature and altitude.
    • Pump distance from the liquid source.
      25 to 30 feet maximum.
    • Is there a leak in the suction line?
      It will pull air in; you will not see the leak.
    • Air vent.
      The air in the suction side of the system being displaced by the liquid must have somewhere to go, otherwise the pump will air bind.
    • Pipe size and geometry.
      The suction piping should be the same size as the pump suction because of the air volume that needs to be evacuated. The suction pipe should rise continuously to the pump and not create any high points that will trap air.
    • Submergence.
      The sump or source you are drawing from will likely have operating levels that are constantly changing. If you reach minimum submergence, it will be possible for air to be drawn into the pump and affect performance.
    • NPSHA.
      Calculating the NPSHA for self-primers, is a great method to identify potential problem areas. Remember, everything except atmospheric pressure is working against you (Static Lift, Vapor Pressure and Friction).

 

And Now for the Rest of the Story –
The Issues with the Application

A wise man once told me you can not violate the rules of physics
and 95% of pump problems are on the suction side of the pump.

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

Issue #1 – NPSHA is ? 6.5 feet. NPSHR at BEP is 14.6 feet. NPSHA must always be more than NPSHR with as much margin as possible.

Issue #2 – Suction pipe is ? 60 feet. Too much air to evacuate.

Issue #3 – Submergence Unknown. Minimum submergence required is ? 8 feet (without a bell mouth setup).

Issue #4 – Check / Foot Valve located 30 feet from the pond. If you are going to use a foot valve it should be located at the bottom end of the suction pipe.

As a general guideline, if your pump takes more than four minutes to prime than you should shut the pump down and look for and correct the cause of the problem.

 

 

 

For More Information
Reference These Pump & Systems Articles
by Jim Elsey:

10 Common Self Priming Pump Issues
Guidelines for Submergence & Air Entrainment
Calculate NPSHa for a Suction Lift Condition

 

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We are your Best Value by
“providing quality pumping
products in a timely manner,
at a fair market price.”

Green Bay, WI USA | Summit Pump, Inc. –

 

Summit Pump has cancelled all pump schools for 2020. With so much uncertainty over the upcoming months we felt this to be the prudent decision.

The Summit Pump school experience is classroom based, plus a factory tour with 14 educational stops and a social aspect like no other school.

Course content consists of:

    • Centrifugal Pump “101 Plus” Fundamentals: Basic hydraulics and fluid dynamics.
    • Summit Pump products and marketing, features and benefits, and tips about competitors.
    • Meet key personnel from Summit Pump, Inc, and participate in the factory tour which includes ANSI pumps, self-primers, PC pumps, IGP, manufacturing and quality checks.
    • Evening “symposiums” to meet, mix with and learn from other Summit Pump distributors from around the world.

We want to make sure all portions of the pump school are available to the students.

This break in pump school sessions provide us time to evaluate and reinvent the Summit Pump School experience to be better than ever next year.
We look forward to seeing you then.

 


Yes! Yes, we do.

First, please pardon my paraphrasing of classic movie quotes. However, I think it is a great analogy when talking about gauges in pump systems. Depending on who you talk to … Some people think gauges are extremely important to the overall efficiency of the system, but others do not. As an OEM pump manufacturer we know that gauges can be almost as important as the pump itself for creating an efficient and reliable system.

As a daily life example; Most of us would not drive a car without the basic gauges for speed, fuel, temperature and oil pressure. So why would we risk a multi-million dollar production system with no way of knowing how and where the pump operates or have the ability to troubleshoot it.

The Hydraulic Institute publication, Optimizing Pumping Systems states, “A pump system with no means of measuring flow, pressure or power is an inefficient pumping system”. Unfortunately, in many cases gauges are not often specified for a pump project or supplied at the time of installation due to cost constraints. In many cases, an up-front investment of a few hundred or even a few thousand dollars can save tens or perhaps hundreds of thousands of dollars down the road.

 

One of the best ways to monitor pump reliability is to install two pressure gauges. One on the suction side and the other on the discharge side. With the pump curve in hand and knowledge of the speed and impeller size, the gauges will tell you exactly where and how well the pump is performing. If the pump is not on the curve refer to this article for more information.

All of us in the pump industry should be familiar with reading pump curves and we know that pumps have specific areas of operation. These areas have descriptions like; Shut Off, RIGHT or LEFT side of the curve, Run Out and Best Efficiency Point (BEP). If the pump is “running left” on the curve, this simply means that the pump is delivering relatively higher pressure and lower flow. “Running to the right” means a higher flow rate, but a decrease in discharge pressure. BEP is the point of optimum flow and efficiency. The bottom line is that without gauges you will not know where the pump is operating. Oftentimes a gauge reading is a more accurate performance indicator than a flowmeter.

Here are a few scenarios on why using gauges is important in maintaining and troubleshooting a pump.

  1. Readings from both the discharge and suction gauges are a useful tool because the difference in pressures is proportional to the total head.
  2. The pump will operate where the system curve intersects it. Your estimate of where that point truly is may be off.
  3. A shutoff head test will provide useful information in relation to the pump’s health.
  4. Static readings are useful in detecting a leak in the suction or discharge.

One last note: I frequently see gauges installed directly on the pump flanges; while a common practice this is not always the best location. For gauges to provide an accurate reading the gauge taps should be installed close to the pump, but preferably at a minimum of 3 to 6 pipe diameters away from the flanges.

If you don’t measure it, you can’t manage it.

 

 

 

 

 

 

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Today we will discuss ANSI pumps with a focus on Summit’s model 2196 product line.  


Pump Impeller Clearance 

When a pump leaves our OEM factory there are a minimum of five critical steps required (to be completed in the field) as part of commissioning and starting up the pump. One of these five key steps is setting and or verifying the impeller clearance.When asked what dimension to set the clearance many individuals will throw out a nominal number like 0.015” and sometimes that is right, but many times it is wrong. And so, it is important to realize that the clearances are different for each size, type and model of pump along with the essential factor of product temperature.

Below is a chart from the 2196 manual as a reference:

Pump Efficiency or… What happens if the clearances are opened up further then the factory recommendations?

In general: Once impeller clearances reach 0.005”- 0.010” in excess of the factory design clearances the efficiency loss will be approximately one to one. That is, there is a one percent efficiency loss for each additional 0.001” of clearance.Once you exceed 0.010” beyond the factory advised clearances the rate changes and it then becomes a two  to one loss. That is, there is an additional two percent loss for each additional 0.001” of clearance.

Efficiency continues to decrease dramatically as clearances increase. Once clearances exceed 0.015 to 0.020 over the initial clearance, the rate of efficiency decrease can become exponential, first as a square function and then by the cube and so on. Somewhere in excess of 0.030” to 0.040” the pump loses most of its ability to pump effectively.

What should I do? 

Even if you set the clearances correctly at startup… over time, wear on both the casing and impeller will inevitably take place and so the pump will experience a loss of efficiency and performance. At which point, you’ll need to readjust the impeller clearance to compensate for the wear. As a general “thumb rule” once the clearance is doubled from the original settings, the pump clearances need to be reestablished to the original dimensions. Please talk with your RSM for more information on this topic.

Why should I maintain proper pump clearances? 

Setting proper impeller clearances on pump installations is a critical and crucial step.

Note that as clearance increases…

 

 

 

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Ever wonder why some impellers, fresh and new from the factory have holes in them? Or… why some impellers have those funny mini vanes on the back side? The short answer is to reduce the axial thrust in the pump and also to reduce the pressure in the stuffing box. 


Whenever you operate a centrifugal pump of any design there are always dynamic forces at play. A good engineer will address all of the forces in the pump and create designs to reduce and or eliminate the effects. There are several dynamics to deal with in the pump, but the two main ones are the axial and radial forces.

Axial forces are those that act on the rotor in a direction parallel to the shaft. These forces exist due to higher pressures acting on one side of a surface and/or acting on a larger area. The main surface area is the impeller shroud(s).

In large multistage pumps the axial force is mostly neutralized by the use of a balance drum. In other multistage pumps it can be managed by using the opposed impellers method. For example, in a 6 stage pump, 3 impellers face one direction and the other 3 face the opposite way.  Another example is the horizontal split case pump where the impeller has two inlet eyes that are opposed at 180 degrees to each other. The net effect is an almost balanced (negating) axial force.

ANSI style (B73.1) pumps are end suction types that use semi open impellers 99% of the time. These impellers have a shroud on one side only. This geometry makes them easy and less expensive to manufacture. However, a downside consequence is an impeller with higher unbalanced axial forces.

Under normal operating conditions there will be a much higher force on the back of the impeller than on the front. The resultant force will attempt to push the pump impeller towards the suction. The thrust bearing counteracts that force. It is not uncommon for a medium frame size ANSI pump to develop up to 850 pounds of force exerting in the direction towards suction. The axial force will lessen with higher suction pressures.

A designer could simply install bigger thrust bearings and not worry about the axial force, but the bigger bearings require bigger shafts and that requires bigger housings and all those things result in a pump that has both a bigger initial cost and a bigger maintenance cost.

The method most pump engineers use is to reduce the axial force behind the impeller. This is where impeller balance holes and or pump out vanes come into play as an axial force reduction method. You can’t get something for nothing so there is a small tradeoff with efficiency and power when using this approach.

For those of you that are interested in the details as to how and why pump out vanes and balance holes actually work, I will compose a more detailed article for Pumps and Systems magazine in the near future.

 

 

 

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We have all heard the term “flush” used when discussing mechanical seals. The definition of a flush is “a stream brought in from an external source to the mechanical seal.” This plan (API Plan 32) is almost always used in conjunction with a close clearance throat bushing. The flush fluid must be brought into the stuffing box at a minimum of 15 PSIG higher than stuffing box pressure.

The advantage is that the external flush fluid, when selected properly, can result in extended seal life. When an outside flush source is used, concerns regarding product dilution and/or economics must be considered by the user. The picture below shows API Plan 32 arrangement.

API Plan 32
Piping illustration used are copyright material and have been used with permission from AESSEAL

The confusion arises when our customers call a discharge recirculation (API Plan 11) a “flush”. Although this terminology is often used, this is where the confusion lies. This plan takes fluid from the pump discharge (or from an intermediate stage), through an orifice(s) and directs it to the seal chamber to provide cooling and lubrication to the seal faces. The advantage is no product contamination and piping is simple.

You must remember the fluid is coming back to the seal at a higher pressure. If the fluid contains particulate, you are bringing dirt and contaminants to the seal at high pressure. Think sandblaster. This is a good piping plan to control vapor pressure. Think hot water and flashing between the seal faces. The picture below shows a Plan 11 arrangement.

API Plan 32
Piping illustration used are copyright material and have been used with permission from AESSEAL

A primary factor in achieving highly reliable, effective sealing performance is to create the best fluid environment around the seal. Selection of the right piping plan and associated fluid control equipment requires a knowledge and understanding of the seal design and arrangement. As well as awareness of the fluids in which the seals operate and the rotating equipment to which they are fitted.

Provision of clean, cool face lubrication, effective heat removal and consideration of personnel and environmental safety, leakage management and controlling system costs are among the specific factors that must be considered. It is proven to prevent premature mechanical seal failure you must use a reliable seal support system.

 

 

 

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Snoring pumps… ever heard of such a thing?

I knew that pumps could run, burp, leak, stall and die (people “kill” them all the time),
but I didn’t know that pumps could snore.


Kidding aside, by definition a pump that is pumping a mixture of liquid and air is technically snoring. The term originates from the process noises associated with the phenomena.

Does your pump have the ability to pump normally, then operate dry for some length of time and then self-re-prime and return to pumping? And then…does it have the ability to repeat that process over and over? Probably not. Pump snoring is a condition that leads to reduced reliability and shorter pump life.

Most all centrifugal pumps DO NOT have the ability to pump liquids with air entrainment above 10% and almost never much above 14%. As a matter of fact, most all centrifugal pumps will have issues starting as low as 2% air entrainment. Note: that self-primers, recessed impeller (vortex) pumps and disc friction pumps can possibly pump mixtures at higher percentages.

 

 

 

Snoring is usually a term reserved for submersible pumps on dewatering applications at construction sites, but the phenomena can apply to most any centrifugal pump type and application.

Another application where this phenomena shows up is pumping a tank down to empty and/or for transfer. The snoring issue occurs frequently with batch process operations and if the operator (or the process control system) are “out to lunch” the pump consequently suffers mortal damage to the clearances, mechanical seals and bearings.

Sometimes it is not the operator, but the system design that creates the issue such as dissolved – air flotation (DAF) systems and waste water treatments that require additives such as surfactants, alcohols and soaps.

 

 

One of the main culprits for pump snoring is simply poor sump design, where the influent is dumped into the sump at elevations high above the liquid level at or near the pump suction intake without the benefit of weirs or baffles. This improper geometrical arrangement contributes to a “waterfall effect” pulling air into the liquid…it probably should be called the “water torture” method.

Other common causes for air entrainment are sumps that are too shallow, frequently experienced on cooling tower applications and in underground mining applications (minimum overhead space) where the air gets mixed into the liquid due to inadequate submergence thereby creating a vortex action.

Why do we care?
Entrained air is directly related to:

  • Reduced pump performance, both head and flow and often to the point of stall
  • Increase in vibrations and noise (the reduction in efficiency manifests as these)
  • Overheating
  • Higher incidents of shaft breakage

Furthermore…
Don’t confuse air entrainment with cavitation as they are two different things, but they can sometimes be related by a root cause and both can occur at the same time. Lastly, do not confuse dissolved air with entrained air.

Stop your pumps from snoring, don’t let them drink air before they go to bed.

 

 

 

 

For added background refer to my articles in Pumps and Systems magazine.
The links are below for your convenience.

How to Reduce or Eliminate Air Entrainment:
https://www.pumpsandsystems.com/how-reduce-or-eliminate-air-entrainment

Guidelines for Submergence & Air Entrainment
https://www.pumpsandsystems.com/guidelines-submergence-air-entrainment

 

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Green Bay, WI USA | Summit Pump, Inc. Remains open to continue supporting critical infrastructure sectors.

 

 

Effective Tuesday, March 24th 2020, Wisconsin Gov. Tony Evers has ordered closure of all non-essential businesses, and urging citizens to “stay-at-home” to slow the spread of the COVID-19 virus. 

Summit Pump, Inc. has been identified as a component of the Critical Manufacturing group of workers necessary for the manufacturing of materials and products needed for the food and agriculture, energy, chemical manufacturing, water and wastewater treatment, and paper industries. 

Summit Pump, Inc. will remain open, and continue to support these essential infrastructure sectors. 

We have taken every precaution to ensure the health and safety of our employees, and will continue to monitor the updates from CDC and WHO. 

 

Sincerely, 

Scott R. Keller 

President 

This issue compliments an earlier issue (Volume 1 issue 12 from April 2018)
on the same subject. 

I am frequently asked; should the discharge valve be open or closed when the pump is started? My answer is….it depends, but regardless the suction valve better be open.


First Things First

Let me state that as visitors to client facilities we should never supersede their operating procedures.

Next, let’s look at the impeller. There are many things to consider, but the primary question we want to answer today is; what is the geometry of the impeller? From that shape we will determine the range of Specific Speed (NS). Ok, I may have lost you now because I used the nerdy “Specific Speed” term, but let me explain. Just for today’s purpose, let’s focus on the directional path of the liquid and specifically how it enters and exits the impeller.

Specific Speed is a predictive indicator for the shape of the curves for head, power and efficiency.

Low Ns

If the liquid enters the impeller on a path parallel with the shaft centerline and exits the impeller at an angle 90 degrees to the shaft centerline (at a right angle) then the impeller is in the low Specific Speed range. This would be a typical radial impeller like the Summit Pump model CC-FM.

Medium Ns

If the liquid enters the impeller on a path parallel with the shaft centerline and exits somewhere close to a 45 degree angle, then the impeller is in a medium Specific Speed range. These are mixed flow or Francis-Vane type impellers.

High Ns

If the liquid enters the impeller on a path parallel with the shaft centerline and exits in a path parallel to the shaft centerline, this is a high Specific Speed impeller. This axial flow type of impeller would look similar to a boat or airplane propeller.

Plan B

Don’t know the Specific Speed (NS) of the impeller? Ask the manufacturer.

Now for the Really Interesting Part

For low Specific Speed (NS) pumps the Brake Horse Power (BHP) required increases as you open the discharge valve and increase the flow rate, this is a direct relationship just as you would intuitively expect. For medium NS pumps the BHP curve and its maximum point moves back to the left some nominal amount … in the past you may have not noticed this change. Axial flow pumps, of high NS, the BHP is near its maximum point at the lower flow rates and actually reduces as the flow rate increases. Perhaps the opposite of what you would expect? Notice how the slope of the power graph also changes when the impeller design goes from low to high specific speed.

And…Answering the Original Question

I recommend that the discharge valve be closed on the startup of low Npumps and to be open on high Npumps. Note, this is a “thumb rule” and there are numerous caveats that can and will modify the answer.

  1. If the low Specific Speed (NS) pump is of any consequential size (Flow, Head and BHP) you may need to have the discharge valve slightly open to reduce the differential pressure across the valve. This step will minimize the effort to open the valve. Some pump systems will have a bypass line for this purpose.
  2. Systems that have downstream pressure (from another source) with no check valves (or check valves that are leaking by) can force the pump to spin backwards when the discharge valve is open.
  3. If you are starting a pump that will operate in parallel with another pump(s) you need to consider check valve lift points and controlling instrumentation (PID); this is a subject too cumbersome to explain in the “Sixty Seconds” platform.
  4. Normally, high Specific Speed (NS) pumps are started with the discharge valve open to reduce the electrical load and resultant stresses on the driver. In many cases the driver may not be adequately sized (on purpose) to handle the low flow power requirements and will trip offline.

 

 

 

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Rolling Stone’s front man Mick Jagger’s second favorite song verse is
“start me up”…”I’ve been running hot”.  

Did you also know there are restrictive limits regarding the number of times an induction motor can be started in a given time period? The restrictions are due to (“running hot”) temperatures and for that singular reason it is always prudent to know the pump’s application and duty cycle. This issue doesn’t normally come up unless you are troubleshooting or testing a system; but even then, there is never a good time to kill the motor.


Reason for Motor Failure
The biggest number one cause of motor failure is basically an argument, and it depends on if you consider both mechanical and electrical reasons. Regardless, always in the top few electrical reasons, is failure due to the insulation system.

3D Model ©ABB. Used with Permission.

A simple explanation for the motor starting restrictions is to mitigate thermal damage to the insulation system because the life of a motor is directly related to the insulation system. The amount of amps (I) (quantity squared) in a unit of time (I2T) will determine the amount of heat generated and the resulting high temperatures will shorten the insulation life. On average the heating effect of the I2T during startup is over a 100 times the full load heat effect during normal operations.

Thumb Rules
There is an industry rule for motors, coils and transformers that can be adapted to approximate the relationship between insulation life and total operating temperature. Simply stated, if a motor’s total operating temperature is reduced by 10°C (18°F) the thermal life of the insulation system is approximately doubled. The antithesis follows; if the total operating temperature is raised by 10°C (18°F) , the thermal life expectancy of the insulation system is reduced by one half.

Motor startups create copious amounts of heat in the windings. Due to manufacturing variances in motor construction the industry normally simplifies these heating effect factors as I2T. In reality it is much more complicated.

As a general motor “thumb rule” …the more horsepower and speed…the fewer number of starts that are allowed per hour. Just to add more rules and restrictions, there is also a minimum time allowance between starts. And last…it is always a good idea to let the motor run for at least a minute or two once it is started, if at all feasible.


Bonus Section
Sixty seconds is up, but if you want a little extra bonus information please read on.

Lessons from the field
Many cases of recurring motor failure (due to excessive startups) have been incorrectly addressed by increasing the horsepower rating of the motor. Typically this action has the opposite intended effect and actually shortens the time between failures. The root cause analysis later showed the real reason for these failures was the excessive frequency of starts and stops.

Guidelines
As a general guideline for NEMA design B motors, use the above chart as a guide. Note that most all of the motors you will encounter for centrifugal pump drivers will be NEMA design B.

Always check with the manufacturer to be sure.

 

 

 

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products in a timely manner,
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