Design of a Wastewater Treatment Plant DESIGN OF SECONDARY BIOLOGICAL TREATMENT PLANTAbstractTO PROVIDE A DESIGN APPRAISAL FOR INCLUSION OF A SECONDARY TREATMENT PLANT THAT IS CURRENTLY EQUIPED WIH A PRIMARY TREATMENT PLANT TABLE OF CONTENTS1. INTRODUCTION2.INTRODUCTION TO BIOLOGICAL NUTRIENT REMOVAL (BNR)3. DESIGN DATA & PARAMETERS ASSUMED 3.1 DESIGN FLOW Q 3.2 PROCESSING TEMPERATURE 3.3 INFLUENT TKN 3.4 READILY BIODEGRADABLE CHEMICAL OXYGEN DEMAND4. DESIGN PROCEDURE5. BIOWIN MODELLING6. CONCLUSION7. REFFERENCES APPENDEX Wastewater Treatment Plant Design 1.INTRODUCTIONThe Coastal Wastewater treatment plant currently has a Primary Treatment Plant only. A design appraisal has been requested for a secondary treatment plant. This report is to design a draft based on the influent characteristics of the waste water and designed for the give effluent characteristics.The accumulation of nutrients in the waste water especially nitrogen and phosphorous leads to decrease in water quality. To control and treat the waste water various treatment methods have been tested. After careful consideration of various influent parameters like BOD, COD, Ammonia-N, TSS, Total Nitrogen and Total Phosphorous etc., the Anerobic-anoxic-aerobic (A2O) process was employed due to its ease of working and diverse advantages.2.Intoduction to Biological Nutrient Removal Process (BNR)Biological Nutrient Removal Process was developed in the 1960s, it has been used since then due to is various advantages over other Chemical Process. BNR is a modification of Activated Sludge Treatment Process that incorporates an Anoxic and/or anerobic zones to enables removal of nitrogen and phosphorous from the wastewater.Anerobic-anoxic-aerobic is a type of BNR which has a 3 stage Phoredox Anerobic-Anoxic-Oxic (A2O) system. The stages in this system are Anerobic system, anoxic system, and aerobic system. Each system treats a certain type of effluent. The treatment of phosphorous takes place in the anerobic stage whereas BOD gets treated in the aerobic stage by the process of nitrification. Denitrification process removes the nitrate in the anoxic stage. (Metcalf & Eddy, 2003). Any process has certain limitation, so does A2O process. Some of the limitations of the process are, i) decrease in the reduction of the removal of the Phosphorous due to recycling of RAS along with nitrate in the anerobic stage. ii) decrease in removal of Nitrogen due to internal recycling ratio (Metcalf & Eddy, 2003). iii) reduction in activity of PAOs.Fig shows the proposed A2O process secondary treatment plant3. Design data and Parameters assumed.The designing of the Secondary wastewater Treatment Plant is based on the provided design data, Kinetic data and few important assumptions made. Some of the Kinetic data is incorrect so corrections had to be made to bring them in the recommended range as given in the Metcalf & Eddy, (2003).3.1 Design Flow Q To obtain the daily flow rate Q for the give proposed capacity of 210,000 Equivalent Population (EP), an average daily consumption of 340 L/ep (Riverina Water County Council, NSW) was taken for calculation along with an 80% recovery factor. A peaking factor of 1.93 was taken (Harmon Coefficient). So, the flow rate, Q= 340 x .8 x 1.93 x 210,000 = 110,241.6 m3/day.3.2 Processing Temperature Average processing temperature of 200 was set for easy calculation therefore there was no need for corrections for Kinetic coefficients. 3.3 Influent TKN The TKN value is taken in the form of NH4-N3.3 Readily Biodegradable Chemical Oxygen Demand (rbCOD) A major design parameter rbCOD was not given, therefore the value of rbCOD is assumed from Metcalf & Eddy, 2003. 15% 25% of bCOD was taken at the end. To consider for the rbCOD consumed in anerobic stage, 25% was assigned for removal of Phosphorous removal and 10% was assigned for denitrification. Table containing the design data and the assumed parameters INFLUENT PARAMETERS EFFLUENT PARAMETERS Parameter Unit ValueParameter Unit ValueAlkalinitymg as CaCO3/L269BODmg/L21CODmg/L201TSSmg/L4pH7.78Ammonia-Nmg/L1TSSmg/L98Total Nmg/L27VSSmg/L80Total Pmg/L6Ammonia-Nmg/L34.7Total Nmg/L48.2Total Pmg/L7.63 PARAMETER UNITS VALUE REMARKS Kinetic DataYg MLVSS/g BOD removed0.60Given dataK1kg BOD utilized/kg VSS.day10Given dataKdday-10.1Given dataKsmgBODµ/L20Given dataKinetic Constant for Nitrifying BacteriaµNmaxd-1 at 20°C0.7Given dataKNmg NH4 + as N /L0.7Given dataYNKg VSS/ Kg NH4+ as N nitrified0.12Given dataAssumptionsMLSSmg/L2400Given dataWater consumption/per capitaL/ep. Day340(Riverina Water County Council, NSW)Recovery factorPercentage80Peaking factor (Harmon coefficient)1.93rbCOD/bCOD0.25(Metcalf & Eddy)rbCOD/bCOD1.6(Metcalf & Eddy)FS (TKN peak /TKN average)1.5(Metcalf & Eddy)DOmg/L2(Metcalf & Eddy)BOD/COD Ratio0.5 Average process temperature0C 20Kog/m30.5(Metcalf & Eddy)Kdng VSS/g VSS.d0.08(Metcalf & Eddy)Fd0.15(Metcalf & Eddy)Nox/TKN0.78(Metcalf & Eddy)VSS/TSS0.8(Metcalf & Eddy)Px,bio = Px,vssrbCOD/NO3-Ng/g6.6(Metcalf & Eddy)rbCOD/Pg/g8(Metcalf & Eddy)Detention time in the anoxic tankH1(Metcalf & Eddy)4. Design Procedure The various design data was changed to need for calculation purpose. Some of the kinetic constants were assumed. The assumed constants and other design data are mentioned in the above Table. Some of the missing data were also assumed for calculations. All these data and constants were obtained for Metcalf & Eddy,2003.The design process was carried out in 3 stages. The first stage was the design for BOD and Nitrification. The second stage was for removal of Phosphorous. The third stage was designed for Denitrification process. An Activated Sludge process, single sludge bio-N removal process and an Anoxic/Aerobic process design was considered. (Metcalf & Eddy,2003).BOD & NitrificationThe BOD and Nitrification removal process by Activated Sludge process was carried out by the following steps.1. The DO concentration was assumed to 2 mg/L to calculate growth rate aimed at Nitrification µn by means of Eq.1. The nitrification factor of 1.5 was taken. Design SRT was computed using Eq.3 (Metcalf & Eddy,2003).2. Using the Eq.4 the max Specific growth rate µm was calculated. Based on the Kinetic constants Y & K1, the effluent substrate (S) was calculated by means of Eq.53. Px,bio (Biomass Production) was calculated by means of Eq.9 grounded on the ideals of A, B and C using Eqs. 6, 7, 8. The NOx was assumed to be approximately equal to 0.8 TKN (Metcalf & Eddy,2003). But the real value was calculated using the Eq. 10. The obtained value was found to be similar to that of the assumed value.4. The mass of VSS and TSS was calculated using Eqs. 12 and 13. The concentration of VSS was taken to be same as Px,bio as there was no info about the nbVSS. The concentration of TSS was calculated using Eq.11 presuming that VSS = 80% TSS (Metcalf & Eddy,2003).5. The volume of the aeration tank was figured by Eq.14 for the given MLSS. Four number of basins were assumed with a depth of 6.5m and a width ratio of 1.5 : 1(Metcalf & Eddy,2003).Phosphorous Removal The removal of Phosphorous takes place in the anerobic stage in the A2O Process. The following are the procedures of the removal:1. The determination of the rbCOD available for the removal of Phosphorous, Eq.25 was used. The nitrate mass balance was performed at the influent using Eq.22 bearing in mind no NO3 concentration in the influent. Taking rbCOD/nitrate = 6.6, bCOD/BOD= 1.6 and rbCOD/bCOD = 0.25 equivalent rbCOD was computed (Metcalf & Eddy,2003).2. The P removed by Biological Phosphorous Removal was computed by Eq.26 taking 8g of rbCOD/g Phosphorous is removed BPR (Metcalf & Eddy,2003).3. The concentration of Phosphorous removed was calculated by Eq.29 taking that the concentration of Bio P removed and the concentration of P used for biomass growth.Denitrification The anoxic stage is responsible for the denitrification. A recycle stream from aerobic zone with oxygen form nitrification being removed is considered. The design process carried out is as follows;1. The biomass concentration was calculated by Eq.32, the volume of nitrite nursed into the anoxic tank is computed by Eq.33, Eq.34 and Eq.35. The volume of anoxic zone is computed by Eq.36 for a suitable detention time.2. The amount of nitrate reduced was calculated by Eq.38. when the nitrate fed is not equal to the nitrate reduced, detention times must be varied. Specific Denitrification Rate as a function of MLSS with observed were computed, the SDNR was got using Eq.39.3. The oxygen credit and the net oxygen needed was calculated using Eq.40 and Eq.41. The air flow rate was computed using Eq.42 and Eq.43. The equation 43 was used to convert mass flow rate to volumetric flow rate.4. The required alkalinity was as conc of CaCO3 was computed by Eq.46 and Eq.47. It is an important factor as some of the reactions have the propensity to change the pH which impacts the system performance.Design of Secondary Clarifier Secondary clarifier was needed to settle and remove the suspended solids that include the nutrients. The design is a 3-step process, defining the return sludge recycle ratio, determine the clarifier size and loading volume of solid. The area of clarifier was determined using Eq.54 as a purpose of design flowrate and supposed hydraulic application rate. The diameter of the basin was designed based on the number clarifiers. The loading volume of solids was computed based on the Eq.58. The number of clarifiers varies based on the loading rate of solids.5.BioWin Modeling:BioWin is simulator used in designing of a wastewater treatment process, that bonds together the biological, chemical and the process models. BioWin is used all over the world to design, advancement and enhance wastewater treatment plants of all types. The core of BioWin is an exclusive biological model which is accompanied with other process models (e.g. water chemistry models for calculation of pH, mass transfer models for oxygen modelling and other gas-liquid interactions).The Biowin modeling was used to validate the theoretical values obtained. It was found that the theoretical values satisfied curtained parameters but did not satisfy other parameter. The model was edited to obtain the required effluent parameters. Parameter like Ammonia and COD obtained by the theoretical calculations were not in the required effluent range. Hence the model was reconfigured, like the theoretical volume of the aeration tank was very less and thus Ammonia couldnt be reduced to the required effluent range. Therefore, the volume of the Aeration tank was increased by trial and error method to achieve the effluent standards.The kinetic constants were entered. Mixers were used to mix the influent before it was inlet into the aeration tank. Splitters with a constant of 0.6 were used to recycle the RAS back to the Aeration tank from the Clarifiers. The treated biowaste was collected as sludge and was disposed. All the given Influent parameters were reduced successfully in the Biowin model.Changes made in the design for attaining the given range was very sensitive. Change in dimensions in the Aeration tank or the clarifiers had subtle changes in the output.6.Conclusion To achieve the given effluent values for the influent values an Anerobic-Anoxic-Aerobic process was adopted for the design purpose. The 3-stage process consisted of BOD removal, Nitrification, Phosphorous removal & Denitrification in addition to design of clarifiers for settling and removal of biological suspended solids. Due to insufficient data given for designing several kinetic data and certain values were assumed as per requirement.(Metcalf & Eddy 2003). A few changes were made to the obtained values from the theoretical calculations to achieve the required effluent parameters.The anticipated effluent values were achieved based on the proposed design. The Treatment plant can be implemented based on the proposed design and will have a high success rate in removal of the influent parameters.APPENDEX-AASSUMPTIONSPARAMETERS UNITVALUEREMARKS Depth of basinm6.5(Metcalf & Eddy)Width to depth ratio1.5 : 1(Metcalf & Eddy)CS,20mg/L9.08(Metcalf & Eddy)?0.65(Metcalf & Eddy)?0.95(Metcalf & Eddy)F0.9(Metcalf & Eddy)CS,TH=CS,TH=CS,20(Metcalf & Eddy)Fine bubble ceramic diffusers with an aeration clean water O2 transfer efficiency35%(Metcalf & Eddy)Required alkalinity to transform ammonium to nitrateg CaCO3/g NH4-N7.14Residual alkalinity concentration to maintain pH in range 6.8-7g/m380(Metcalf & Eddy)Influent alkalinityg/m3 as CaCO3140(Metcalf & Eddy)Return sludge mass concentrationg/m38Design MLSS XTSS concentrationg/m33Hydraulic application ratem3/m2.d22(Metcalf & Eddy)Number of clarifiers3Phosphorus content of heterotrophicg P/g0.015(Metcalf & Eddy)Alkalinity as CaCO3 produced per NO3-N Oxidizedg/g3.57(Metcalf & Eddy)APPENDEX-BSUMMARAY OF RESULTS PARAMETERS UNIT VALUE REMARKS BOD REMOVAL AND NITRIFICATIONAverage wastewater flowm3/d110,241.61ep =340 L/dayAverage BOD loadkg/d100.5Average TKN loadkg/d18Aerobic SRTd3.198>7, (Metcalf & Eddy)Aeration tanks44 tanks (Metcalf & Eddy)Aeration tank volume, eachm34600Aeration Tank LengthM31approx. 150m per tank, (Metcalf &eddy)Aeration Tank WidthM15W:D ratio 1.5, (Metcalf & Eddy)Aeration Tank Depthm10AssumedHydraulic retention timeh6.5MLSSg/m32400MLVSSg/m31582.642F/Mg/g.d0.5930.04-1, (Metcalf & Eddy)BOD loadingkg BOD/m3.d0.9390.04-1, (Metcalf & Eddy)Observed yieldkg TSS/kg bCOD0.810kg VSS/kg BOD1.296Oxygen requiredkg/h1393.62Air flowrate at average wastewater flowm3/min396.50RAS ratio0.6Clarifier hydraulic application ratem3/m2.d2216-24, (Metcalf & Eddy Table 8.7)ClarifiersNos3Diameter ,m46Alkalinity addition as Na(HCO3)kg/d27410.47BIOLOGICAL PHOSPHOROUS REMOVALP used for biomass growthg/m31.22P removedmg/L5.7387P content of waste sludge%7.146DENITRIFICATIONEffluent NO3-Ng/m36Internal recycle ratio6.266RAS recycle ratio0.6Anoxic volumem36429.98Overall SDNRg NO3-N/g MLSS.d0.140Detention timeh1.2Alkalinity requiredkg/d as CaCO316316.08EFFLUENT QUALITY PARAMETERSEffluent BODmg/L19.02Target value achievedEffluent NH4-Nmg/L0.17Target value achievedEffluent Nmg/L15.37Target value achievedEffluent Pmg/L3.92Target value achievedEffluent TSSmg/L0Target value achievedAPPENDEX CNOMENCLATUREQ: influent wastewater flowrate (m3/d)Ko: oxygen inhibition coefficient, g/m3µm: Maximum specific growth rate (d)BOD: Biological oxygen demand (mg/L)DO: Dissolved oxygen, mg/LFd: cell debris fraction (unitless)TSS: Total suspended solids (mg/L)µNmax: Maximum specific growth rate of nitrifying bacteria, g new cells/g cells . dMLSS: mixed-liquor suspended solids, mg/LTKN: influent TKN concentration (mg/L)µm: Maximum specific growth rate, (d)PX,bio: Biomass production (kg VSS/d)Ne: effluent NH4-N concentration, mg/Lµn: Specific growth rate for nitrification (d-1)PX,VSS: Solid production as VSS (kg/d)Total P: Total phosphorus (mg/L)µ: Specific growth rate (d-1)PX,TSS: Solid production as TSS (kg/d)NH4-N: Ammonia as Nitrogen (mg/L)SRT: Solid retention time (d)Fraction VSS: fraction of VSS over TSS, unitlessY: Heterotrophic yield coefficient (kg VSS produced/Kg BODFS: Safety FactorXVSS * V: Mass of VSS (kg)K1: Maximum specific substrate utilization rate (Kg BOD/Kg VSS.d)So: Influent substrate concentration (mg/L)XTSS * V: Mass of TSS (kg)Kd: Microbial decay coefficient (d-1)S: Effluent substrate concentration (mg/L)V: Total volume of aeration tanks (m3)Ks: Saturation coefficient (mg/L)A: heterotrophic biomass, kg/day?: Detention time (h)YN: Nitrifier yield coefficient (Kg VSS produced/Kg NH4+ N nitrified)B: cell debris, kg/dLorg: Volumetric BOD (kg/m3.d)Kdn: Endogenous decay coefficient for nitrifying organisms (g VSS/g VSS?d)C: nitrifying bacteria biomass, kg/dayYobs,TSS: Observed yield base on TSS (g TSS/gBOD)KN: Half-velocity constant, substrate concentration at one-half the maximum specific substrate utilization rate (g/m3)D: Nonbiodegradable VSS in influent, kg/dayYobs,VSS: Observed yield base on VSS (g VSS/gBOD)rbCOD: Readily biodegradable chemical oxygen demand (mg/L)TSSo: influent wastewater TSS concentration (mg/L)NOx influent: Concentration of NH4-N in the influent flow that is nitrified (mg/L)N: nitrogen concentration, g/m3VSSo: influent wastewater VSS concentration (mg/L)?: Salinity-surface tension correction factor (unitless)Xb : active biomass concentration (mg/L)F/Mb: BOD F/M ratio based on activated biomass concentration (gBOD/g biomass .d)F: fouling factor (unitless)kd: endogenous decay coeff. (1/day)NOr: nitrate removed (g/d)CS,T,H: Oxygen saturation concentration in clean water at temperature t and altitude h (mg/L)NOx effluent: nitrogen oxides in the effluent (mg/L)SDNR (MLSS): specific denitrification rate referred based on MLSS (g NO3-N/g MLVSS. d)CS,20: Dissolved oxygen saturation concentration in clean water at 20C and 1 atm or 760 mmHg (mg/L)IR : internal recycle ratio (unitless)R1: Oxygen credit (kg/h)CL : operating oxygen concentrationQanoxic : flow rate to anoxic tank (m3 /d)Ro: Net oxygen required (kg/h)E: diffusers oxygen transfer efficiencyNOx feed: NO3 N fed to the anoxic tank (kg/d)AOTR: actual oxygen transfer rate under field conditions(kg O2/h)Alk produced-denitrification: alkalinity produced in denitrification (g/m3)Vnox: volume anoxic tank (m3)SOTR: Standard Oxygen Transfer Rate in Tap Water at20°C and zero dissolved oxygen (kg O2/h)NOx RAS: nitrogen oxides in the effluent in the return activated sludge (mg/L)SDNR: Specific denitrification rate (g NO3-N /g MLVSS.d)?: Oxygen transfer correction factor for waste (unitless)D: diameter (m)Qr: RAS flowrate (m3/d)R: return activated sludge (RAS) recycle ratio (unitless)A: total area of clarifier (m2)Xr: Return sludge mass concentration (g/m3)X: Mixed-liquor suspended solids (mg/L) APPENDEX DFORMUAL USED EQUATIONNOFORMULAEQUATIONNOFORMULABOD REMOVAL AND NITRIFICATION 1 =2.132 * 1.5=3.198 dMax Specific Growth rate µm = K1 * Y =10 *0.6 = 6Effluent Substrate Conc (BOD Effluent)S=Ks1+kd.SRTSRT?mkd1S=201+0.1*3.1983.19860.11S=1.47726 mg/LBiomass ProductionA (heterotopic Biomass)A=QY(SoS(1kg103g)1+(kd)SRT=11024106*0.6(100.51.47721+0.13.198=4962.760 Kg/dB (Cell Debris)B=fdkdQYSOSSRT(1kg103g)1+(kd)SRTB=0.150.1110241.6*06100.151.47723.1981+0.1198=396.772 Kg/dC (Nitrifying Bacteria Biomass)C=QYNOx1kg103g1+kdnSRTC=110241.6*0.12(47.1994)1+0.13.198=477.10325 Kg/dPX,bio=A+B+CPX,bio=4962.760+396.772+477.10325=5836.6352 Kg VSS/dOxidation of Ammonia to NitrateNOx=TKNNe0.12?PX,bio/QNOx=48.210.12?5836.6352/110241.6=47.1994 g/m3Concentration of VSS and TSSPX,TSS=A0.85+B0.85+C0.85+D+Q?(TSSoVSSo)PX,TSS=4962.7600.85+396.7720.85+477.18320.85+0+110241.6?(9880/1000)=8850.97 Kg/dMass of VSS and TSSXVSS?V=(PX,VSS)?SRTXVSS?V=(5836.6352)?3.198=18665.55 KgXTSS?V=PX,TSS?SRTXTSS?V=(8850.97)?3.198=28305.402 KgDesign of Aeration TankV=XVSS?VMLSSV=28305.4022400=11793.91 m3Assumed no of Tanks = 4Volume of basin = V/4=11793.91 / 4=2948.44 m3Assumed Depth = 6.5Width to depth ratio = 1.5 : 1Width = 6.5*1.5 = 9.5=10 mLength of the tank = Volume of tank /width * depth=2948.44/ 10*6.5=46 mDetention time?=VQ?=29900110241.6=6.5 hFraction of VSSFraction VSS=XVSS?VXTSS?VFraction VSS=18665.5528305.402=0.659MLVSSMLVSS=Fraction VSS*MLSS=0.659*2400=1582.642 g/m3Volumetric BODLorg=Q*SOVLorg=110241.6*100.511793.91=0.939 Kg/m3.dObserved Yield based on VSSYobs,TSS=PX,TSSQ?(SOS)Yobs,TSS=8850.97110241.6?100.51.4774=0.810 gTSS/g bCODYobs,VSS=Yobs,TSS*VSSTSSYobs,VSS=0.63*0.816=0.5142 g VSS/gBODOxygen DemandRo=Q (So S) 1.42Px,bio + 4.33 Q (NO3)=110241.6(100.5-1.499) 1.42*5836.63 + 4.33*110241.6*47.1994=1393.62 Kg/hMass of Alk needed as CaCO3 for nitrification Alk used for nitrification = 7.14g CaCO3 g NH4 N*NOx g/m3=7.14*47.1994=337 g/m3 used as CaCO3Alk to be added = Alkalinity pH -Influent Alk + Alk used=80 269 +337=148Alk to be added = 110241.6*148/1000=16315.756 Kg/d as CaCO3Na(HCO3) needed =Alkalinity needed as CaCO3 * Equivalent amt of Na(HCO3) / Equivalent weight of CaCO3=(163150456 +80)/ 50=27410.47 Kg/d Na(HCO3)Phosphorous RemovalP removal design requirementNO3 = 27 mg/LNO3-N in RASNO3-N in RAS = NO3-N = Total N -NH4-N=27-1=26 mg/LNitrate mass balance at influent in the reactorNO3-Nreact = NO3 RAS * Q / Q + Qr=(26*110241.6*0.6) / (110241.6 + (110241.6 * 0.6))=9.75 mg/LrbCOD available for P removalrbCOD equivalent = NO3 react * 6.6=9.75*6.6=64.35 mg/LrbCOD available for P removalrbCOD available for P removal =rbCOD influent rbCOD equivalentbut rbCOD influent = 0.25(1.6*BOD)=0.25(1.6*100.5)=36.15 mg/LPhosphorous removed by BPR mechanismBio P removal = rbCOD available for P removal / (ratio of rbCOD/BOD)=36.15 / 8=4.518 mg/LP used for heterotrophic biomass synthesis in addition to phosphorous storage due to BODPx,bio= A + B= 4962.760 + 477.10325=5439.86 Kg/dP used for biomass growth = pH content of heterotrophic biomass * Px,bio=0.015 * 5439.8=1.22 mg/LP removed = Bio p removed + Pused for biomass=4.158 + 1.22=5.7387 mg/LP content of waste sludgeTotal P in sludge = p removed * Q / 1000=(5.7387 * 110241.6) / 1000=632.54 Kg/dP % = ( Total P in sludge/ Px,TSS) * 100=(632.54 * 100) / 8850.97= 7.146 %DenitrificationActive biomass calculationXb=Q?SRTVY?(SoS1+kdSRTXb=110241.6?3.198117930.6?(100.51.49971+0.13.198=1345.78 mg/LInternal recycle ratioIR=NOXNoxeffluent1RIR=47.1994610.6=6.266Amount of NO3-N to the anoxic tankFlowrate to anoxic tank = IR * Q + R * Q=6.266*110241.6 + 110241.6 * 0.6=756980.93 m3/dNOx= feed = Qanoxic * NOx effluent(756980.93 * 6) / 1000=4541.88 Kg/dVolume of anoxic tankVnox = ? * Q=0.05 * 110241.6=6429.98 m3SDNRSDNR = 0.42Amount of NO3-N that can be reducedNOr = Vnox * SDNR * MLVSS=6429.98 * 0.42 * 1582.642=7094.68 kg/dCapacity ratioCapacity ratio = NOx / NOx feed =7097.68 / 4541.88=1.56 >T =1.4 therefore acceptableAirflow rateSOTR=AOTRCs,20??F?(??CS,T,HCLSOTR=766.669.080.65?0.9?(0.95?9082=1795.8 Kg/LAir Flow Rate=SORTE*0.27*60Air Flow Rate=1795.80.3*0.27*60=369.50 m3/minAlk to be added = alkalinity pH influent Alk + Alk used Alk produced denitrification=80 269 -337.003=148.003 g/m3Mass of alkalinity neededMass of alk needed = Alk to be added * Q /1000=(148.003 * 110241.6) / 1000=16316.098 Kg/d CaCO3Anoxic zone mixing energyAnoxic zone mixing energy = V * Mixing energy=6429.98 *10 / 1000=64.29 KWSecondary clarifier DesignReturn sludge recycle ratioRAS recycle ratio = Qr / Q=(110241.6 * 0.6) /110241.6=0.6Size of clarifierArea = Q / hydraulic application rate=110241.6 / 22=5010.98 m3Area per clarifier = Area / No of clarifier=5010.98 / 3=1670 m3D= 4*Area?D= 4*1670?=46.12=46 mA=?4*D2*3A=?4*462*3=4983 m3Solid loadingSolid Loading=1+RQMLSSASolid Loading=1+0.6110241.6*2400)4983*24=3.53 kg MLSS / m2 hAPPENDEX -FBIOWIN MODEL 7.References( ; BioWin ; Chapter 7 Metcaf Eddy 2015 ; Chapter 8 Metcaf Eddy 2015 ; Enhanced biological phosphorus removal and its modeling for the a.pdf ; Finalthesis_TU ; lagoon-pond-treatment-2011 ; Model history ; Seasonal influent characterization model calibration SRT and en ; A.Sathasivan ; Bechmann ; Bekir Ersu et al. 2008; Council ; E MOrgenroth ; Jokela et al. 2002; Metcalf, amp & Eddy 2003; Metcalf et al. 2002; N.Banadda ; Sh.Mardani ; Stensel & Shell 1974; Tomaszewska & Mozia 2002; Zeng et al. 2010; Zeng et al. 2011) .A.Sathasivan, Biological Phosphorous Removal Process for Wastewaster Treatment.Bechmann, H., Modeling of Wastewater Systems.Bekir Ersu, C., Ong, S.K., Arslankaya, E. & Brown, P. 2008, 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