 Open Access
 Total Downloads : 29
 Authors : Sanjay Kumar , Ijlal Ahmad Rizvi
 Paper ID : IJERTV8IS060582
 Volume & Issue : Volume 08, Issue 06 (June 2019)
 Published (First Online): 27062019
 ISSN (Online) : 22780181
 Publisher Name : IJERT
 License: This work is licensed under a Creative Commons Attribution 4.0 International License
Evaluation of Blower and Diffuser Requirement in the Aeration System
Sanjay Kumar
Department of Mechanical Engineering IEC College of Engineering & technology Greater Noida, India
Ijlal Ahmad Rizvi
Assistant Professor, Department of Mechanical Engineering IEC College of Engineering & technology
Greater Noida, India
Abstract: – Most of energy that is used for running the waste water treatment goes to biological treatment unit. 7075 percent of energy used by the waste water treatment plant is spend to run the blower to deliver the air for aeration of waste water. The energy needed by the blower depends upon the efficiency of the aeration system. The more will be the efficiency of the aeration system, lessor energy will be required by the aeration system. So it is very crucial to design the whole aeration system i.e. from blower to diffuser including piping. This research paper focuses on the need of blower and the number of diffuser required because these two are the most important part of the aeration system.
Keywords: Waste water treatment plant, Aeration system, Blower size calculations, Number of diffuser, AOTE, Oxygen requirement, SOTE, TDS Activated sludge.
INTRODUCTION
Waste water generated by the people living in metropolitan cities as well as in small cities has been a major problem and increasing industrialization aggravates this problem. So it is very necessary to handle this waste water very delicately to make our earth green and clean.
Now a days to eradicate waste water problem the developed nations are using and developing are going forward to use the waste water treatment plants. Commissioning cost of the plant is not a problem but the running cost of the plant is great cause of concern for the industries as well as for the government also.
So for a researcher is worth focusing on minimize the cost of running of the plant. Mostly the cost of running spend in the aeration system for biological treatment of the waste water. The location of the plant plays a significant role in minimizing the cost of operation of the aeration system. So we can say that the designing of aeration system is very important [4].
It is very necessary to be familiar about the few terms to understand about the most important terms:
SOLIDS IN WATER
Solids in the water are of the two types which can be classified according to their size and shape, chemical properties and size distribution. Theses solids can also be classified as organic, inorganic and immiscible liquids. The biological degradation of solids results in objectionable by products. So solids removal from water is of great importance.
TURBIDITY
The turbidity of water is the measure of ability of light passing through it. Its ability measured against a turbidity index. The water having turbidity index five allows no passage of light, while index one shows little or no turbidity.
COLOR
The pure water is colorless but foreign substances can often tint water. These foreign substances are vegetation, soils, municipal and industrial waste and aquatic organisms. Water color is measured by standard color solution or colored glass disc.
TASTE AND ODOR
Minerals, metals, salt from soil and end products of biological reaction decides the taste and odor of water. The taste and odor has little impact on safety. Potassium permanganate, chlorine and other oxidants are used to remove taste and odor by oxidation
TEMPERATURE
The temperature of water is very important for aquatic life because temperature of water affects the solubility of oxygen in the water. The temperature of waste water is also very significant for industrial purposes because the cold water needs more chemicals for efficient coagulation and flocculation.
TOTAL DISSOLVED SOLIDS
Dissolve solids can be present in the form of organic, inorganic matter in water. The dissolve solids occurs in water by the contact with substances in soil, on surfaces and in the atmosphere. Decayed vegetation, organic chemicals and gases are the major sources of organic dissolve solids. These sources causes the physiological effects and color, taste and odor problems. The dissolve solids can be separated from water by filtration, evaporation, electro dialysis, reverse osmosis and ion exchange.
ALKALINITY
Alkalinity is the measure of waters ability that how much it can neutralize the acids. In other words we can say that it is the buffering capacity of water. Bicarbonate, carbonate and hydroxyl ions are responsible for the alkalinity of the water. Carbon dioxide from the different sources is also responsible for alkalinity of the water. High alkaline water can be bitter in taste but has no serious effect on human health.
HARDNESS
Minerals of calcium and magnesium present in the water are responsible for hardness, so hardness indicates the concentration of these minerals in water. Deposits is the major problem in hot water due to these minerals in pipeline. Hard water also have many advantages i.e. it helps tooth and bone growth.
FLUORIDES
Little fluoride ions in potable water is good for dental health. Fluoride ions in large quantity can be toxic for human. The surface water has fluoride ions in appreciable quantity.
METAL
Metals in water may harm the human health even in little quantity. It can be divided into two categories i.e. toxic and nontoxic. These metals be present in natural water due to dissolution from natural deposits and discharges of industrial wastes.
ORGANICS
Color, taste and odor is affected by the organic matter present in water. Halogenated compound be formed in the water undergoing chlorine disinfection due to the presence of organic matter. Organic matter present in water affects the solubility of oxygen that interferes the water treatment process. Presence of organic matter is the most important cause of the BOD increase.
PH
PH is the measure of hydrogen ion concentration in water. In other words it can be said that it is the measure of acidity or alkalinity of water. The biological and chemical reaction are affected by the PH. Water with higher PH level has more chlorine contact time for disinfection.
CHLORIDES
Chlorides be there in groundwater naturally. Higher concentration of chloride does not have any effect to human health but it causes salty taste.
DESIGN PROCEDURE OF AERATION SYSTEM
Fig. Different stages of water treatment plant [4]

Information required for designing of plant [5]
NOTE: Based on an assumption of no biological degradation in the secondary clarifier, the BOD5 in the waste activated sludge and recycle activated sludge are taken to be equal to that in the effluent stream.
The symbols used in the flow diagram at the left and the equations below are as follows:
NOTE: Based on an assumption of no biological degradation in the secondary clarifier, the BOD5 in the waste activated sludge and recycle activated sludge are taken to be equal to that in the effluent stream.
The symbols used in the flow diagram at the left and the equations below are as follows:
Q is volumetric flow rate in m3day S is BOD5 concentration in g/m3
X is total suspended solids concentration in g/m3 The subscript o refers to the primary effluent stream.
The subscript e refers to the secondary effluent stream. The subscript w refers to the waste act. Sludge stream. The subscript r refers to the recycle act. Sludge stream.
V is the volume of the aeration tank in m3.
X is the mixed liquor suspended solids concentration in he aeration tank in g/m3.
Waste water properties supplied to the plant
Waste water flow rate, Qo in (m3/d) Primary Effluent BOD5, So in (g/m3) Aeration Tank MLSS, X in (g/m3) Percentage volatile MLSS, in % Vol
Waste/recycle activated sludge properties Sludge SS concentration Xw in (g/m3) Secondary Effluent TSS, Xe in (g/m3)

Aeration tank sizing calculations
SIZING BASED ON VOLUMETRIC LOADING
Volumetric Loading: VL in g/kg) (given)
Design Aeration Tank Volume = Qo* So /(VL*1000) Values of other Design Parameters
Aeration Tank Hydraulic Retention Time = 24*V/Qo hr Aeration Tank F:M Ratio = (Qo *So)/(% Vol.*X* V) kg BOD5/day/kg MLVSS
Sizing based on hydraulic retention time [6] Hydraulic Loading: HRT = 24*V/Qo hr (given) Aeration Tank Volume = Qo*HRT/24
Values of other Design Parameters
Aeration Tank Volumetric Loading = (Qo *So)/(V*1000) kg BOD5/day/m3
Aeration Tank F:M Ratio = (Qo *So)/(%Vol*X*V) kg BOD5/day/kg MLVSS
Sizing based on F:M ratio
F:M Ratio: F:M in kg BOD5/day/kg MLVSS (given) Aeration Tank Volume = (Qo* So)/(%Vol*X* F:M Ratio) Values of other Design Parameters
Aeration Tank Volumetric Loading = (Qo* So)/(V*1000) kg BOD5/day/m3
Aeration Tank Hydraulic Retention Time = V*24/ Qo* hr

Aeration tank operation calculations
Standard pressure and temperature for Sm3/m calculation (per ASME & CAGI) – changeable by user
Standard Pressure, PS
1.014
bar
Standard Temperature, TS
20 oC
Standard pressure and temperature for Sm3/m calculation (per ASME & CAGI) – changeable by user
Standard Pressure, PS
1.014
bar
Standard Temperature, TS
20 oC
ESSENTIAL DATA REQUIRED
Constants and conversion factors used in the calculations
Temp. coeff
for kd
1.024
Saturation D.O. in water at 20oC & 1 atm, Css
9.17
g/m3
Ideal Gas Law Constant, R
8.3145
kN m/kgmoleK
Molecular weight of air
28.97
Specific Weight of water, H2O
9.807
kN/m3
Molecular weight of oxygen
32
Conversion
g Factor, Cf1
1000
g/kg
Atmospheric Press. at sea level, Pstd
1.014
bar
o Conversion
n Factor, Cf2
60
min/hr or sec/min
Oxygen mole fraction in air
0.209
CbCOD
e (BODult)
equivalent of VSS:
1.42
kg COD/kg VSS
Conversion Factor, Cf3
24
hr/day
O2 equivalent
e of NH3N:
4.57
kg O2/kg NH3N
Conversion Factor, Cf4
100
kPa/bar
Constants and conversion factors used in the calculations
Temp. coeff
for kd
1.024
Saturation D.O. in water at 20oC & 1 atm, Css
9.17
g/m3
Ideal Gas Law Constant, R
8.3145
kN m/kgmoleK
Molecular weight of air
28.97
Specific Weight of water, H2O
9.807
kN/m3
Molecular weight of oxygen
32
Conversion
g Factor, Cf1
1000
g/kg
Atmospheric Press. at sea level, Pstd
1.014
bar
o Conversion
n Factor, Cf2
60
min/hr or sec/min
Oxygen mole fraction in air
0.209
CbCOD
e (BODult)
equivalent of VSS:
1.42
kg COD/kg VSS
Conversion Factor, Cf3
24
hr/day
O2 equivalent
e of NH3N:
4.57
kg O2/kg NH3N
Conversion Factor, Cf4
100
kPa/bar
Aeration Tank Volume, V in m3 (given)
Target Sludge Retention Time in SRT days (given)
Activated sludge operational parameters calculation
Recycle Act. Sludge Rate, Qr = QoX/(XwX) m3/d
Waste Act. Sludge Rate, Qw = (V*X/SRTQo*Xe)/Xw m3/d Aer. Tank F:M Ratio, F:M = (Qo*So)/(%VOL*X*V) k BOD/day/kg MLVSS
Note: In Calculating Qw, the effluent flow rate, Qe is taken t be equal to the influent flow rate, Qo, based on the assumptio that liquid streams separated from the waste activated sludg are sent back into the wastewater stream.

Oxygen requirements/blower sizing calculations
Note: To aid in setting the design WW flow rate for thes calculations, it is recommended that the maximum, minimum and average WW flow rates be identified and that the oxygen requirement rates be calculated for each.
ESSENTIAL DATA REQUIRED
Permitted Secondary effluent BOD, BODe in g/m3 Permitted Secondary effluent TSS, TSSe in g/m3
% volatile solids in effluent TSS in % Vol Sludge Retention Time, SRT in days
Synthesis Yield Coefficient, Y in kg VSS/kg BOD5 Endogenous Decay Coefficient (at 20oC), kd20 in kg VSS/d/kg VSS
Std. O2 transfer Efficiency, SOTE in % (from diffuser mfr or vendor)
Press.drop across diffuser, Pdiff in bar (from diffuser mfr or vendor)
Depth of Diffuser, ddiff in m (from installation or plans) Design ambient air Temperature, Ta in o C
Influent TKN, TKNo in g/m3
Effluent NH4N Concentration, Ne in g/m3
Design Barometric Press., Patm in bar (ambient pressure at site)
Design wastewater Temperature Tw in o C Ratio of BOD5/BODu, f in ratio
Blower efficiency, h in %
Ratio of oxygen transfer rate in wastewater to that in clean water, a in ratio
Ratio of D.O. saturation in wastewater to that in clean water at same T & P, B in ratio
D.O. saturation concentration for clean water at waste water temp. & 1 atm, Cs in g/m3
D.O conc. to be maintained for WW treatment operation, CL in g/m3
Diffuser fouling factor, F = 0.8
Pressure drop at blower inlet, Pin = in bar (due to filter, silencer, etc.)
Oxygen requirement/blower specifications (BOD Removal Only)
AIR REQUIREMENT/BLOWER DESIGN CALCULATIONS
Effluent Soluble BOD, Se = BODe(f*cbCOD*%VOL*TSSe) g/m3
Endog. Decay Coeff. (at 20oC), kd20 = kd20*( ^(Tw20) kg VSS/d/kg VSS
Observed Yield (with recycle), Yobs =Y/(1+ kd20*SRT) kg VSS/kg BOD5
Required O2 flow rate = Qo/Cf1)*(SoSe)((1/fcbCOD*
Yobs)/Cf3) kg/hr
Act. O2 transfer Efficiency, AOTE*
=SOTE**F*(((B*(PD/Pstd)*C5)CL)/C55)* ^(Tw20) % Pressure at Mid Depth, PD = Patm+( H2O*(ddiff/2)/Cf4 bar Standard Air Density, air = Mole. Wt .of air*(Ps*100)/(R(Ts+273.15)) kg/m3 (from Ideal Gas Law)
Design Air Flow Rate, SCMM = (Req.O2 flow rate/AOTE)*Mol. Wt. of air/(O2 mole frction in air*Mol. Wt. of O2* air* Cf2) mstd3/min
Design Air Flow Rate, ACMM = SCMM*(Pstd/PB2)*(Ta+273.15)/(Ts+273.15) m3/min (at delivery point)
Blower outlet pressure, PB2 = Patm+Pdiff +(H2O* ddiff / Cf4) bar
constants
Standard O2 solubility (DO.std)
9.08
mg/L, DO solubility in clean water at
20 Â°C and at 1 ATMambient atmospheric pressure
Process temperature correction factor, (theta)
1.024
unit less
Atmospheric temperature lapse coefficient (B.atm)
0.0065
K/m, used with normal atmospheric pressure computation
Universal gas constant (R.univ)
0.082057
(m3ATM)/(k molK)
Massbased gas constant for air (R.M)
286.9
J/(kgK), used with normal atmospheric pressure computation
Standard meteorlogical temperature (T.met)
288
K, used with normal atmospheric pressure computation
Gravitational acceleration (g)
9.806
m/s2, used with normal atmospheric pressure computation
Standard process temperature (T.std)
20
Â°C, base T for process computation and for use of standard cubic meter
Standard atmospheric pressure (P.std)
1
ATM (much more convenient than kPa), normal ambient pressure at sea level
Specific weight of water (SW.w)
9.789
kN/m3, taken at 20 Â°C and considered constant with process temperature
Standard atmospheric O2 content (Y.O2.std)
0.209
(molO2/molair)
Molecular mass of O2 (MW.O2)
32
kg/kmol
Molar specific volume of ideal gas at STP (SV.stp)
24.0427
m3/kmol; SV.air
=ROUND(R.univ*(T.std+273)/P.std, 4)
Conversion from ATM to kPa (kpa.atm)
101.325
kPa/ATM
The a.DO – d.DO coefficients fit a thirdorder polynomial to the data presented at right from the USGS database
a.DO
0.00007021
constants
Standard O2 solubility (DO.std)
9.08
mg/L, DO solubility in clean water at
20 Â°C and at 1 ATM ambient atmospheric pressure
Process temperature correction factor, (theta)
1.024
unit less
Atmospheric temperature lapse coefficient (B.atm)
0.0065
K/m, used with normal atmospheric pressure computation
Universal gas constant (R.univ)
0.082057
(m3ATM)/(k molK)
Massbased gas constant for air (R.M)
286.9
J/(kgK), used with normal atmospheric pressure computation
Standard meteorlogical temperature (T.met)
288
K, used with normal atmospheric pressure computation
Gravitational acceleration (g)
9.806
m/s2, used with normal atmospheric pressure computation
Standard process temperature (T.std)
20
Â°C, base T for process computation and for use of standard cubic meter
Standard atmospheric pressure (P.std)
1
ATM (much more convenient than kPa), normal ambient pressure at sea level
Specific weight of water (SW.w)
9.789
kN/m3, taken at 20 Â°C and considered constant with process temperature
Standard atmospheric O2 content (Y.O2.std)
0.209
(molO2/molair)
Molecular mass of O2 (MW.O2)
32
kg/kmol
Molar specific volume of ideal gas at STP (SV.stp)
24.0427
m3/kmol; SV.air
=ROUND(R.univ*(T.std+273)/P.std, 4)
Conversion from ATM to kPa (kpa.atm)
101.325
kPa/ATM
The a.DO – d.DO coefficients fit a thirdorder polynomial to the data presented at right from the USGS database
a.DO
0.00007021

Computation of actual oxygen transfer efficiency and diffuser requirements – diffuser aeration systems [5] Constants (from literature and computed) used in AOTE computations.
b.DO 
0.007635 
c.DO 
0.4004 
d.DO 
14.59 
DO.sat.T = a.DO*T.des3 + b.DO*T.des2 + c.DO*T.des + d.DO 
Input data required for sitespecific conditions
Parameter 
value 
description 
Maximum actual oxygen transfer rate (AOTR.max), kgO2/day 
10000 
design maximum mass of O2 needed per day (exactly equal to the oxygen utilization rate, OUR) – use this to determine the number of diffusers necessary 
nonmaximum AOTR to be investigated(AOTR), kgO2/day 
5000 
Use this to investigate air delivery for min, average and other special cases once the number of diffusers is set 
Elevation of process site (H.site), m 
3000 
site elevation above mean sea level 
Diffuser submergence (D.sub), m 
7 
depth of centerline of diffuser below air/liquid interface 
Diffuser transfer rate ratio (alpha), dimensionless 
0.95 
ratio of KLa in process water to KLa in clean water at standard temperature 
Oxygen solubility ratio (beta), dimensionless 
0.9 
ratio of DOsat in process to DOsat in clean water at standard temperature 
Diffuser fouling factor (F.foul), dimensionless 
0.8 
ratio of KLa for fouled diffuser to KLa for clean diffuser 
Process temperature (T.des), Â°C 
25 
process temperature for computation of necessary gas flow requirement 
Design process O2 level (DO), mg/L 
1 
oxygen concentration level to be maintained in process mixed liquor 
If highpurity O2 is used, enter the purity 
0.95 
molO2/molgas 
Computed parameter values for sitespecific conditions
The saturation value of DO at a specified T.des is given by: DO.sat.T = a.DO*T.des3 + b.DO*T.des2 + c.DO*T.des + d.DO DO.sat.T = a.DO*T.des3 + b.DO*T.des2 + c.DO*T.des + d.DO mg/L
P.H = P.std*(1B.atm*H.site/T.std)^(g/R.M+B.atm) atm P.mid = P.H+(SW.w*D.sub/2)/P.std.kPa atm
P.disch = P.H+SW.w*D.sub/P.std.kPa atm DO.sat.T.H=DO.sat.T*P.H/P.std mg/L
Calculation for the number of diffuser required
Calculation of actual (Field) oxygen transfer efficiency (AOTE) requires manufacturers value of standard oxygen transfer efficiency (SOTE). By using AOTE the number of diffusers necessary at the design maximum case is computed. For these computations manufacturers data correlating with gas flow per diffusers are necessary for the computation of AOTE and number of diffusers required.
q 
SOTE 
m3/(min diff) 
% 
0.071 
44.4 
0.129 
42.3 
0.183 
40.5 
0.238 
39.3 
0.296 
38.58 
0.354 
38.22 
The following graph and eqution is obtained by using excel with the help of manufacturers data of sote and gas flow rate for a particular diffuser.
The number of diffusers necessary to deliver air at the maximum OUR is determined by simultaneously solving following set of equation yielding Yo2.avg, Csat.avg and AOTE.
sote vs gas flow rate
The images of excel sheet is provided as below.
I. Computations for the maximum oxygen demand case – sets the number of diffusers
I. Computations for the maximum oxygen demand case – sets the number of diffusers
Enter the desired gas loading rate for the design diffuser in cell C7 (consider that some capacity should be reserved for the potential that loading exceeds the maximum anticipated ). 
m3/(mindiff) % SOTE = a.3p*q.des + b.3p*q.des2 + c.3p*q.des3 + d.3p 
The initial guess for AOTE (95% of SOTE.des) from cell D11 into cell C11 to start the numeric computation of the field AOTE. 
The initial guess will be replaced by the solver gas Y.O2.avg = Y.O2.std/2*(1+(1C11/100)/(1Y.O2.std*C11/100)) C.sat.avg = DO.sat.T.H*(P.mid/P.H*C12/Y.O2.std) 
Use the solver (Data – solver) to iteratively solve the set of equations in cells C12, C13 and C15 – set the value in cell C15 
f(AOTE) = SOTE.des*((beta*C13DO)/DO.std)*theta^(T.desT.std)*alpha*F.foulC11 
f(AOTE) should be on the order of 107 or lower, once the solver does its work. 
% This is the actual oxygen transfer efficiency at the maximum condition kgO2/day (from user input) kgO2/day OAR = ROUND(AOTR.max*100/C11,0) mstd3/min Q.std.air = ROUND(C19/(MW.O2*Y.O2.std)*SV.stp/1440,1) Number of diffusers (CEILING(C20/q.des,1)) needed to supply O2 at the design conditions ATM Static discharge pressure. Add the diffuser dynamic wet pressure loss and the air delivery kPa friction losses to this value to obtain the total blower delivery pressure 

28.31 
molO2/mol mgO2/L 

0.672 
29.8 
20.4805522 
0.191 
9.214 
5.7593E10 
20.48 
10000 
48827 
121.9 
182 
1.558 
157.9 

q.des = OTE.des = 
AOTE = Y.O2.avg = C.sat.avg = 
f(AOTE) = 
AOTE = AOTR = OAR = Q.std.air = N.diff.air = P.disch = 
Enter the desired gas loading rate for the design diffuser in cell C7 (consider that some capacity should be reserved for the potential that loading exceeds the maximum anticipated ). 
m3/(mindiff) % SOTE = a.3p*q.des + b.3p*q.des2 + c.3p*q.des3 + d.3p 
The initial guess for AOTE (95% of SOTE.des) from cell D11 into cell C11 to start the numeric computation of the field AOTE. 
The initial guess will be replaced by the solver gas Y.O2.avg = Y.O2.std/2*(1+(1C11/100)/(1Y.O2.std*C11/100)) C.sat.avg = DO.sat.T.H*(P.mid/P.H*C12/Y.O2.std) 
Use the solver (Data – solver) to iteratively solve the set of equations in cells C12, C13 and C15 – set the value in cell C15 
f(AOTE) = SOTE.des*((beta*C13DO)/DO.std)*theta^(T.desT.std)*alpha*F.foulC11 
f(AOTE) should be on the order of 107 or lower, once the solver does its work. 
% This is the actual oxygen transfer efficiency at the maximum condition kgO2/day (from user input) kgO2/day OAR = ROUND(AOTR.max*100/C11,0) mstd3/min Q.std.air = ROUND(C19/(MW.O2*Y.O2.std)*SV.stp/1440,1) Number of diffusers (CEILING(C20/q.des,1)) needed to supply O2 at the design conditions ATM Static discharge pressure. Add the diffuser dynamic wet pressure loss and the air delivery kPa friction losses to this value to obtain the total blower delivery pressure 

28.31 
molO2/mol mgO2/L 

0.672 
29.8 
20.4805522 
0.191 
9.214 
5.7593E10 
20.48 
10000 
48827 
121.9 
182 
1.558 
157.9 

q.des = OTE.des = 
AOTE = Y.O2.avg = C.sat.avg = 
f(AOTE) = 
AOTE = AOTR = OAR = Q.std.air = N.diff.air = P.disch = 
45
y = 21.71×3 + 60.298×2 – 50.855x + 47.725
44 RÂ² = 0.9994
43
sote
sote
42
41
40
39
38
37
0 0.1 0.2 0.3 0.4
gas flow rate
Yo2.avg =Yo2.std* (1+(1AOTE/100)/(1 Yo2.std* AOTE/100)) Csat.avg =Csat.T.H*(PD/2Yo2.avg/(PH* Yo2.std)) AOTE=SOTE*((Csat.avgCMLSS)/ Csat.avg))*(TdesTstd) **F
The corresponding oxygen application rate is determined using the following equation.
OAR=AOTE*100/AOTE
The total air delivery rate is computed from the following equation.
Qstd.air=OAR*Vair.spec/(MWo2* Yo2.std)
The number of diffusers necessary is computed from the following relation.
Ndiff= Qstd.air/qdiff
Once the number of diffusers is known for non maximum OUR the air deliver per diffuser is computed by simultaneous solution of the following two equation with the three from the above.
qdiff=AOTR*Runiv*(Tstd+273)/((AOTE/100)* Ndiff* MWo2* Yo2.std*Pstd)
SOTE=asote*qdiff+ bsote*qdiff2+ csote*qdiff3+ dsote
(The values of coefficients of this equation will be equal to the coefficients of the equation obtained from the graph by using excel tool.)
We can solve the simultaneous system of equation by using the excel solver tool by using established relation between sote and gas flow rate and can compute the number of diffusers for maximum oxygen demand case and required gas delivery for non max oxygen delivery case.
CONCLUSION
The goal of this research paper is to understand the necessity and design of the aeration system. In this research paper we have learned about parameters affecting the operation and design procedure of aeration system. So we can summarize that this research paper dealt with aeration tank sizing, aeration tank operations, activated sludge operational parameters, oxygen requirements, blower sizing, air requirement, computation of actual oxygen transfer efficiency and number of diffuser required.
Published by :
Published by :
International Journal of Engineering Research & Technology (IJERT)
ISSN: 22780181
Vol. 8 Issue 06, June2019
International Journal of Engineering Research & Technology (IJERT)
ISSN: 22780181
Vol. 8 Issue 06, June2019
REFERENCES
REFERENCES
[1] [2] [3] [4] [1] [2] [3] [4]
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Design of Municipal Wastewater Treatment Plants, WEF MOP No. 8, 5th Ed., Sec. 14.1.3 Activated Sludge Environment, McGraw Hill Education
Standard Handbook of Environmental Engineering, 2nd Ed, Sec
6.5.1 Activated Sludge, McGrawHill Education
Oliver Marunlu, Elena Elisabeta Manea. Research on the Aeration Systems Efficiency of a LabScale Wastewater Treatment Plant, International Journal of Environmental and Ecological Engineering, Vol:9, No:9, 2015
Water &WASTE WTER TREATMENT,A Gulide for the Nonengineering Profssiondl ,Joanne E. Drinan
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Fundamentals of Biological Wastewater Treatment Biological Wastewater Treatment by Arun Mittal.
https://www.wikipedia.org/ https://www.google.com/ http://water.usgs.gov
Shriram, Manogaran, "Economic life cycle assessment of aeration blowers used in waste water treatment systems" (2013)
Design of Municipal Wastewater Treatment Plants, WEF MOP No. 8, 5th Ed., Sec. 14.1.3 Activated Sludge Environment, McGraw Hill Education
Standard Handbook of Environmental Engineering, 2nd Ed, Sec
6.5.1 Activated Sludge, McGrawHill Education
Oliver Marunlu, Elena Elisabeta Manea. Research on the Aeration Systems Efficiency of a LabScale Wastewater Treatment Plant, International Journal of Environmental and Ecological Engineering, Vol:9, No:9, 2015
Water &WASTE WATER TREATMENT,A Gulide for the Nonengineering Profssiondl ,Joanne E. Drinan
Udo Wiesmann, In Su Choi, EvaMaria Dombrowski,
Fundamentals of Biological Wastewater Treatment Biological Wastewater Treatment by Arun Mittal.
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930
IJERTV8IS060582
IJERTV8IS060582
www.ijert.org
(This work is licensed under a Creative Commons Attribution 4.0 International License.)
www.ijert.org
(This work is licensed under a Creative Commons Attribution 4.0 International License.)
II. Computations for a nonmax oxygen demand case – computes required gas delivery
AOTR = 
5000 
kgO2/day, nonmax oxygen requirement (from user input) 

Enter the final AOTE value from Cell C17 (copy and paste as value) in cell C30 to begin the iterative solution. 

AOTE = 
22.3108647 
The initial guess 
for 
the nonmax case AOTE will be replaced by the solver 
Cells C32 – C35 and C37 contain a set 
of 
five equations solved simultaneously to obtain the nonmax case solution 

q = 
0.307 
m3/(diffmin) 
q = AOTR*R.univ*(T.std+273)/(C30/100*N.diff.air*1440*MW.O2*Y.O2.std* 

SOTE = 
32.8 
% 
SOTE = c.3p*C32^3 +b.3p*C32^2+a.3p*C32+d.3p 

Y.O2.avg = 
0.1897 
molO2/molgas 
Y.O2.avg = Y.O2.std/2*(1+(1C30/100)/(1Y.O2.std*C30/100)) 

C.sat.avg = 
9.134 
mgO2/L 
C.sat.avg = DO.sat.T.H*P.mid/P.H*C34/Y.O2.std 

set C37 to zero by changing C30. 

f(AOTE) = 
5.463E11 
f(AOTE) = C33*(beta*C35DO)/DO.std*theta^(T.desT.std)*alpha*F.foulC30 

f(AOTE) should be on the order of 107 or lower, once the solver does its work. 

AOTE = Q.std.air = P.disch = 
22.31 
% This is the AOTE (ROUND(C30,2)) at the nonmaximum condition mstd3/min Q.std.air = ROUND(N.diff.air*C32,1) ATM Static discharge pressure. Add the diffuser dynamic wet pressure loss and the air delivery kPa friction losses to this value to obtain the total blower delivery pressure 

55.9 

1.558 

157.9 