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The following approach can be used to estimate oxygen requirements

Ro = (1 - b * Yg ) * Rs  + b * d * X ,     mg O2/L-hr          

Rs = rate of COD conversion, mg COD/L-hr (usually COD load * removal efficiency), 
Ro = rate of oxygen uptake, mg/L-hr,
X = microorganism concentration, mgVSS/L
Yg = biomass yield coefficient, mass VSS/mg COD removed (usually 0.3 kg VSS/kg COD removed)
b         = 1.42
d = endogenous decay rate (usually 0.1/day)

     So for 42 mg COD/L-hr maximum COD loading rate ( = 1 g COD/L-d) and an assumed 2,000 mg/L VSS in the mixed liquor and an endogenous decay rate of 0.00417/hr (= 0.1/day), the oxygen uptake rate would be:

Ro = (1 - 1.42*0.3) * (42 * 90%) + 1.42 * 0.00417 * 2000 mg/L = 34 mg O2/L/hr 

     The aeration equipment would have to equal or exceed this rate to insure positive DO in the aeration basin. Of course, you will need to make sure you calculate the loading rates correctly in the zone of interest. For example, for plug flow type processes, the COD loading rate would be that in the first section of the basin. 

     Most manufacturers and equipment vendors have readily available software for preliminary designs and will generally assist you with proper equipment/unit selection including recommended/minimum/maximum depth, oxygen dispersion diameter, complete mix diameter and so on.

     We can't go much higher in MLVSS than about 2,000 mg/L and still get good oxygen transfer in the aeration basins.


     The volatile solids content of the mixed liquor in an activated sludge process typically is considered to represent the mass of microorganisms that is available for waste treatment.  However, not all volatile solids are active microorganisms.  Inert cell matter and volatile but nonbiodegradable influent solids also contribute to the mixed liquor volatile solids.  Oxygen uptake occurs when active microorganisms consume biodegradable constituents of the wastewater.  Respirometer-aided methods can provide oxygen uptake measurements which can be used to estimate actual active biomass in mixed liquors.  Case studies show that mixed liquor volatile solids typically range from 5 to 25% active microorganisms.

     We can't go much higher in MLVSS than about 2,000 mg/L and still get good oxygen transfer in the aeration basins. 


     For conventional activated sludge of average rate, i.e. medium rate, it is generally recommended approximately 50 lbBOD/1,000 cu.ft. as maximum.  For process stability and better assurances of performance, [fine pore/fine bubble] diffused aeration systems favor the use of low f/m and that is generally restricted to about 10-15 lbBOD/1,000 cu.ft.  This significantly lower rate sizing tip takes into account process recommendations (extended aeration) as well as diffuser technology old hands recommendations.


     Design of the aeration tanks is also important for optimum efficiency.  Fine bubble diffusers can work at 2.5 water depth but deeper basins will give greater efficiency and superior results on capital costs.  Diffusers are directly dependent on liquid depth for their aggregate efficiency.  As a result, if the basin depth is doubled, it will approximayely use the same horsepower but it will take only roughly one-half the number of required diffusers, i.e. capital cost of the diffusers is about 50%.  Using deeper basins, e.g. 5m, and larger volumes offer much better assurances of performance.  It must be said that one of the authors once witnessed a probably still exisiting wastewater treatment plant at an edible oil plant having a detention time of ... [only] ten (10) minutes.


     A common rule of thumb indicates the air volume required to mix a tank is 0.12 cfm of air per sq.ft. of flat floor area in the tank  This is a way of showing or representing the actual energy requirements per square foot of tank floor.  The reason the 0.12 cfm per square foot of tank is used is to eliminate the variable of depth from the calculation.  Regardless of the depth of the tank one ends up with a proportional energy per unit volume.  Using a value of 20-30 cfm of air per 1,000 cu.ft. as some engineers do, may be a disproportionate amount of energy requirement for deep tanks which may not be realistic.  One must understand the 0.12 value as pertaining to biological solids only.  If it were a tannery wastewater with a lot of heavy material or difficult solids, one could suggest the energy level for mixing be increased to 0.15 or possibly even approach 0.2 cfm per floor square foot.  This is a determination based on the characteristics of the solids to be handled.  For instance, for aerobic digesters one could/would specify0.2 to 0.3 cfm per square foot because of the high concentration of solids and more difficult mixing conditions.


For the purpose of rough calculations we can, whatever the units used, and using say COD as constituent, combine these two formulas:

Yn = Yo * ( 1 + 0.2 * Kd * SRT) / ( 1 + 1.2 * Kd * SRT)

Yn = bugs in tank * 100 / ( SRT * kgCOD/day * COD removal points)

Thus we have
bugs in tank * 100 / ( SRT * kgCOD/day * COD removal points) = Yo * ( 1 + 0.2 * Kd * SRT) / ( 1 + 1.2 * Kd * SRT)

Solving for one of the SRT we get the coveted iteration formula:

SRT = bugs in tank * 100 * ( 1 + 1.2 * Kd * SRT) / ( kgCOD/day * COD removal points * Yo * ( 1 + 0.2 * Kd * SRT) )

From now on it's just a matter of allowing Excel to perform circular reference iterations (you may have to enable this setting in your Excel version).

For those unfamiliar with iterative methods (a numerical analysis classic) one way to find a root of an equation is to solve for the variable and give iterative methods a try.
Were we to find a root for say
a * x^2 + b * x = (a * x + b) * x = 0

One possible iteration formula to try could be solving for x as follows:

x = 1 / (a * x + b)

While it may seem laughable to do it for this case the truth is that it works great for the not so immediate cases. With minor tweaks it can be used for BNR, AO2, other biological types of all sorts including anaerobic stages..


It is not wise to use air stripping for nitrogen removal. Aerobic nitrification/denitrification is much more economical. Some possible treatment train may be as follows:

1. Anoxic/aerobic nitrification/denitrification in tanks-in-series arrangement (ie. AO2, Bardenpho, UCT, etc.)
2. Alum precipitation in an independent flocculation-clarifier from the aerobic process to remove phosphorus and to precipitate suspended solids (This separate clarifier avoids adding chemicals directly to the aeration system). Some powdered activated carbon may have to be added to remove color and soluble organics if color and additional COD removal is required.
3. Granular media filtration for final suspended solids removal
4. disinfection as needed.


The focus of nanobubble technology has been on methods for generation of nanobubbles and much less on applications. There are now some who are trying to commercialize the technology, but it is not clear concerning applications where it will offer advantages. With regard to wastewater treatment applications, historically the oxygen transfer (aeration) system has played the dual role of providing mixing energy to suspend biomass in the process. Nanobubbles, of course, do not do this. Thus, for nanobubble technology as it is being developed the applications will not be for traditional oxygen transfer in wastewater treatment systems.


Need Some Help? - James C. Young Environmental - Balestie, Irwin & Balestie