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IlY7 cf2NR1.1ir Pr.':L <br /> Where V = reactor volume, gallons <br /> FIM = food to microorganism ratio, g BODS/g MLVSS.d <br /> Q = flowrate, gpd <br /> So = influent BODS concentration, mg/L <br /> XMLvss = biomass concentration in reactor, mg/L MLVSS <br /> BIOS )LIDS PRODUCTIONS <br /> Total Biosolids Productions: <br /> QY(So —S) J d kd QY(So —S)SRT QY„(NOX) <br /> Px,vss = 1+kdSRT l +kdSRT l+kd„SRT <br /> Where Px,vss = total solids wasted daily, Ib VSS/d <br /> S = effluent BODS concentration, mg/L <br /> X0'; = non-biodegradable VSS in influent, mg/L <br /> SRT = solids retention time, d <br /> Y = biomass yield, g VSS/g BODS (typical 0.30-0.50) <br /> kd = endogenous decay coefficient (typical 0.10) <br /> fd = fraction of biomass that remains as cell debris (typical 0.10-0.15) <br /> Y„ = biomass yield in nitrification, g VSS/g BODS (typical 0.12) <br /> kd„ = endogenous decay coefficient for nitrifying organisms (typical 0.08) <br /> NOX = concentration of NH4-N in influent that is nitrified, mg/L <br /> OXYGEN REQUIREMENTS CALCULATIONS <br /> Total Oxygen Required: <br /> Ro = Q(So —S)—1.42Px,vss +4.33QNO,, <br /> NO, = TKN—Ne —0.12Px,vss l Q <br /> Where Ro = total oxygen required, Ib/d <br /> TKN = influent TKN concentration, mg/L <br /> Ne = effluent NH4-N concentration, mg/L <br /> The detailed process design calculations are presented in Appendix i. <br /> 3.3 DAF UNITS <br /> DAF units are responsible for the separation of microorganisms from the effluent. The major <br /> advantage of the DAF unit over the secondary clarifier is that the very small or light particles <br /> which settle slowly by gravity can be removed more completely and in a shorter time period. <br /> This design completely eliminates the concern of sludge bulking problems that may occur in the <br /> Wine Cup Motor Coach Resort WWTP Page 6 of 10 8/22/2007 <br /> Preliminary Design Report <br />