That depends on how many of the 20 you want to be able to use at the same time. That is why these valves are rated for 14 bar. If you have fewer valves open the pressure will increase (assuming you are using a centrifugal pump). If you decide that the most valves you want open at the same time...
Your sketch is exactly what I had in mind, so we are talking of the same problem now.
In line with the principle of conservation of mass, if the pump is delivering 900 LPM and there is only 1 spray nozzle open then there must be 900 LPM flowing out of that valve. The problem of getting balanced...
Without a sketch of what is confusing you, I am also a bit confused. There are two separate aspects to this calculation. The first is the system consisting of the fire water pump, the piping to the landing valve and the landing valve itself. It might well be that the piping is a ring main or a...
The pressure at the hydrant (sometimes called residual pressure) is required to generate sufficient velocity in the monitor or nozzle that will be used to fight the fire. The velocity from a fire fighting nozzle will typically be 25 to 30 m/s to allow the sprayed water to reach a reasonable...
I have not worked through the article in detail but it looks questionable to me and I would advise you to compare it with other sources.
I agree with Latexman and TiCl4 that gc is wrong. And it is wrongly described in the article as being the gravitational constant, which it is not (although it...
The residence time is a function of only the volumetric flowrate and the volume of the oxidizer, so you have no need to measure the density.
All you want to measure is the volumetric flowrate - regardless of what the density is. This makes a laminar flow meter the obvious choice. It is a...
You need to take a step back and look at the bigger picture.
Why do you want to measure the flowrate? Does the flow to the oxidizer need to be varied according to the organic content of the off-gas? If yes, how will you measure the organic content? If you do measure the organic content then you...
If you are talking of just the manifold section where the branch pipes connect into then I am with you on the 36" section. I took it as the size for the complete header and 36" is unnecessarily big for that. But for the short section where the other branches need to be connected into having it a...
Rules of thumb (ROTs) are useful as starting points for iterative calculations but using them for real design is wasteful at best and dangerous at worst.
The total flowrate of 1069 kg/s in a 36" pipe would give a velocity of 1.7 m/s and a pressure drop of 2.0 kPa/100m (0.1 psi/100ft). Unless...
If the coolers are all close together the individual branch lines will be short and designing on the basis of velocity will give you a safe design, but you might be able to get away with smaller diameter pipes.
For example, if the line to Cooler 6 is 20" Sch 40 then the velocity would be 2.4...
To answer your original question - the operating point must fall on or below the "including conductance" curve.
As I stated earlier, I have not worked with these conductance curves before, and although the Leybold web page is quite comprehensive it is a nightmare of unit conversions, nomograms...
According to the reference LittleInch gave, the conductance is not the pressure drop but it is the multiplier that must be applied to the pressure drop to calculate the flow rate in volumetric terms.
Under vacuum conditions the density of the gas is usually low enough to ensure that the...
I see that while I was typing up my rant, Pierre has posted a perfect example of what I was getting at.
Each branch of hydraulics, from fire water to vacuum systems, developed their own arcane terminology and methods of problem solution. Back in the day this allowed them to solve routine...
If the main pipe is 41 m long and 25 NB Sch 40 then I would agree with the supplier that it is too small.
But first, a rant. Whenever volumetric flows of gas are given it is essential that the basis be given with the flowrate. It is meaningless to say 60 m3/h without stating whether it is free...
I strongly suspect that the X-axis on the charts is the pressure in mbara and not the pipe length. I see in both cases the operating point is at an X value of 15 and this corresponds to the pressure and not to the pipe length.
I have not seen this type of chart with the two curves before. You...
If the valve at the end of the line is open then the 5 bar that you read at the pump discharge is the pressure drop due to friction caused by the flow from the pump to the end of the pipe.
If you throttle the valve at the end of the line then the pressure drop will increase because you have...
With the additional information you have provided I have "run the numbers" using Darcy-Weisbach and my results are significantly lower than yours. Most of the information you can see in the included graphic but what is not shown is that you need to include the entrance losses of getting the oil...
When the pipe is full you can use Darcy-Weisbach, but it seems that you want to be able to estimate flows for part-full pipes as well. There are plenty of online references and calculators for open channel or part-full pipes - such as the one linked by LittleInch.
As you have mentioned, open...
georgeverghese - you are correct that there is not enough information to definitively conclude that the tank will overflow. But I have seen overflowing in similar setups before and Pavan has confirmed that it did previously overflow when discharging into the second tank. There are two mechanisms...
The reason why I would prefer a constantly sloped pipe is that it will be easier to fill than a vertical pipe and it is only once the pipe is full that it starts generating a static head. But the advantage of the sloped pipe over what your sketch shows will be small and if you use a 12" overflow...
