SPREADSHEET FOR ACTIVATED SLUDGE PROCESS

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Document No.: / /Section: Design Data

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Design by: Hemant Kale Checked by: Rev:

Date: Date: Date:

Design CriteriaInlet Parameters

1 Design Flow

Minimum Flow = 40000

1666.66667

Average Flow = 80000

3333.33333Peak factor f = 2

= 160000

6666.666672 Population

= 275 lpd

Population = 290909

3 BOD

= 110 gm/c/d

BOD load on STP = 32000000 gm/d= 32000 kg/d

BODin conc = 400 mg/l

4 = 40 mg/l

5 Suspended Solids*

= 0.09 kg/c/dSS load on STP SS*Population = 26182 kg/d

SSin conc = 327 mg/l

6 T = 20

7 Elevation above Mean sea Level, Altitude = 100 m

8 Ambient Air Temperature = 25Outlet Parameters

Before Filtration

1 BOD = 10 mg/l

2 TSS = 10 mg/l After Filtration

1 BOD = 5 mg/l

2 TSS = 5 mg/l3 Ammonia Ne < 1 mg/l4 Total Nitrogen < 15 mg/l5 pH = 6.5 to 8.56 Coliforms < 100/100ml

7 Salinity < 4000 micromho/cmREFERENCES

(1) Design Standard Manual : SPC/DSM Sect 4 ,4.3.4,Pg 18(2) Design Standard Manual : SPC/DSM Sect 4 ,4.1.5.1,Pg 6(3) Design Standard Manual : SPC/DSM Sect 1 ,Appendix -2 Sewage Analysis ,Pg 36(4) KEO/M&E preliminary report of Dec 2004 : Appendix -C , average of Temp recorded

Qm m3/d

m3/hr

Qa m3/d

m3/hr

Peak Flow (1) Qp f * Qa m3/d

m3/hr

Flow / capita (1) Qc

Qa*1000/Qc

BOD load per capita (1)

Qa*BODload/capita

Si BODload*1000/Qa

TKN / Ammonia (3) Ni

SSi

SS load per capita (2)

SSi

Temperature(4) oC

oC

So

SSo

Se

SSe

Client:

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Document No.: / /Section: Inlet works- Screens

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Date: Date: Date:

Design Flow

Minimum Flow 40000.001666.67 m3/hr 0.46296 m3/s

Average Flow = 80000.00 3333.33 0.92593 m3/s

Peak Flow = 160000.006666.67 1.85185 m3/s

1 Inlet ChannelAssume Water Depth = 1.00 mVelocity at Qp = 1.00 m/sWidth of Channel = 1.85 m

Say = 1.50 m ChecksVelocity at = 0.31 m/s

= 0.62 m/s

1 Screens No of Screen channels = 3.00No of duty Chanels = 2.00No of stand by = 1.00

Flow per channel = 0.23 m3/s= 0.46 m3/s= 0.93 m3/s

PER CHANNEL DETAILSChannel Width =Channel depth =

Vel thro'screens = 1.00 m/s at peak flowBar spacing a = 15 mm Bar width b = 10 mm

Angle of inclination θ = 50 degVert.Liquid Depth dv = 0.75 m

Area of openings = 0.926 Slant areaWidth of openings Wn = 1.235 mNo of Bars n (n*b)+[n+1)*a]=w = 48.8

say = 36 n

= 0.92say = 1 m

Area openings vert. = 0.709

Wn*d = 0.750 Checks At Peak flow

Velocity thro screens Vs = 1.235 m/s

Velocity in channel Vc = 0.74 m/sAt Average Flow

Velocity thro screens Vs = 0.617 m/s

Velocity in channel Vc = 0.37 m/s

at Peak Flow , clean screens = 0.069 m 68.81 mmat 50 % clogging of screens, velocity is doubled Velocity thro screens Vs Vs /0.5 = 2.469

Qm m3/d

Qa m3/dm3/hr

Qp m3/dm3/hr

Qm

Qa

Qm

Qa

Qp

Vs

Aopen Qp / (Vs ) m2

Hence width of channel based on n, Wn

Aopen-v Aopen *Sinθ m2

Cross section of channel, Ca,c/s m2

Qp / (Ca,c/s)

Vs/ (a/(a+b))

Qa / ( Ca,c/s)

Vc* (a/(a+b))

Head Loss , Hf Vs2-Vc

2/(2*9.81*0.852)

Velocity in channel Vc = 1.48 Hence head loss = 0.273 m 273 mm

Client:

Project Name:

Document No.: / /Section: Inlet works- Grit Removal System

Page: 1 of


Date: Date: Date:

Vs* (a/(a+b))

Depth of Channel= DcFree Board FB = 0.5 mHENCE Dc 1.52 m

Say 1 m

2 GRIT Removal systemNo of Grit System 3No of Duty Grit system 2No of Stand by Grit system = 1 m3/hr

Flow per channel = 0.00 m3/s

= 0.00 m3/s

= 0.00 m3/s

Client:

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Date: Date: Date:

Section: Inlet Works/Biological TreatmentFile:

Design Flow

Average Flow = 80000 3333.33333 0.92593 m3/s

Peak Flow = 160000 6666.66667 1.85185 m3/s4 Anoxic Tank (Anx Tank)

No of Anoxic Tanks = 2 nos

Flow to each Tank Qa = 40000

Influent Ammonia = 40 mg/l

Effluent Ammonia = 1 mg/l

Effluent Nitrates = 8 mg/lMLSS in Aer. Tank X = 3500 mg/l

MLVSS in Anx Tank 0.70 *X = 2450 mg/lD.O in An Tank C = 0.1 mg/l

Denitrification Rate = 0.15 at 20 Deg C

= 0.135 at Field conditions

t = 2.322 hrsSafety Factor f = 1.2

Anx Tank Volume Qa*t*f/24 = 4643.99

R ((Ni-Ne/NO3e)-1)*Qa = 3.88

RAS = 1 100% recycle)

Mixed liquor return = 2.88 = 115000

Hence Provide two Pumps (1 D+ 1S) Each of c capacity = 4791.67

where

Power per unit vol

multiplication factor μ = 1.0087 at 20 Deg C

multiplication factor = 1.000 at Field conditions

= 0.0107Total power required P = 49.677 Kw

dv+FB+Hf

Qm

Qa

Qp

Qa m3/d m3/hr

Qp m3/d m3/hr

m3/d

Ni

Ne

NO3e

Xv Xv / X = 0.7 to 0.8

μdn20 d-1

Denitrif. Rate (6) μdnT μdn20*1.09(T-20)*(1-C) d-1

Anx Tank HRT (7) (Ni-Ne)*24/(Xv * μdnT)

Vanx m3

Recyle Ratio(8)

where R = Overall recycle ratio (Mixed liquor,Qr+Return Sludge,QRAS)

QRAS

Qr (R- QRAS) m3/d

m3/hr

Mixing Requirements per tank (9) (P/Vanx)=0.00094*(μ)0.3*(X)0.298

P/Vanx kw/m3

μT μ(T-20)

P/Vanx

= 66.680 HpAvailable nearest mixer = 1.50 HpTank DimensionsWidth (C/wall with Aeration Tank ) = 8 m

Depth(based on Hydraulics) = 3.80 mLength = 152.76 msay = 152.80 mVolume = 4645.12 m3

REFERENCES(6) Phosphorus and Nitrogen Removal from Municipal Wastewater- Principles and Practice- Richard Sedlak- Page-20(7) Phosphorus and Nitrogen Removal from Municipal Wastewater- Principles and Practice- Richard Sedlak- Page-19(8) Phosphorus and Nitrogen Removal from Municipal Wastewater- Principles and Practice- Richard Sedlak- Page-25(9) Design &retrofit of wastewater treatment plants for biological nutrient removal- Randall,Barnard, Stensel- Page-118

Client:

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Date: Date: Date:

Section: Biological TreatmentFile:

5 Aeration Tank ( Aer Tank) No of tanksNo of Tanks = 2 nosFlow to each tank Qa = 40000 m3/d

Qp = 80000 m3/d

BODin = 400 mg/l

BODout = 5 mg/l Mixed Liquor Suspended Solids(MLSS), X = 3500 mg/l

Mean Cell Residence Time (MCRT) = 25 days 20-30 range

(also termed as Sludge Retention Time (SRT))

Food to Microorganism ratio, F/M = 0.1 0.05-0.15 range

= 45143 Checks

Mass loading rates = 0.125 kg BOD/kg Xv/d

Vol. loading rate Cv = 0.35 kg BOD/m3/d HRT, t Vaer/Qa = 1.129 d Sudge Recycle

Return sludge conc = 0.8 % = 8000 mg/l 8 kg/m3

Sludge Production( per tank) Sludge Yeild co efficient, Y = 0.6 kg TSS/kg BODremoved

= 790.00 m3/d

= 6510 kg/dSludge produced (11) (Si-So)*Qa*Y/1000 = 9480 kg/d

Sludge Wasting based on SRT = 6320.0 kg/d Take which ever is higher for sludge handling equipment = 9480.0 kg/d

Total sludge = 18960.0 kg/dOxygen Requirement per Tank

=where

= 0.68

Sludge Produced = Yobs*Qa*(Si-So)/1000

Sludge yield =

Sludge decay coeff. = 0.05

= 0.26666667

= 4213.33Hence AOR = 24381.56 kg/dDenitirification credit available ( this is the safety factor)

= 2.86*(Ni-Ne)*Qa/1000 = 4461.6 kg/dHowever only 75 % is considered as available for design = 3346.2 kg/dAOR after considering denitirification credit AOR-Credit = 21035.36 kg/dSafety factor available = 1.16Side water depth SWD = 3.8 mWidth of the tank W = 8.00 mLength of tank L = 1485 m

Volume of AT = 45144.00 m3REFERENCES

(10) Wastewater Engineering Treatment and Resue-Metcalf & Eddy-pg 679 table -8.5 equation 7-60(11) Wastewater Engineering Treatment and Resue-Metcalf & Eddy-pg 693 Equation 8-34

Si

So

θc

d-1

Aer Tank Vol, each ( 10) Vaer =Qa*(Si-So)/(F/M *X) m3

Cm (Si-So)*Qa/(Vaer*X*0.8)

(Si-So)*Qa/(Vaer)

Xr

Sludge Wasting basis (11) Vaer * X/(θc*Xr)

((Vaer *X)/(1000))/θc

Actual Oxygen Requirements, AOR, kg/d (12) (Qa*(Si-So)/(1000*f)-1.42*Px +4.33*(Qa*(Ni-Ne)/1000)

BOD5 to BODL factor, f

Px

Yobs Y/(1+ Kd*θc)

Kd

Yobs

Px

Credit of O2 ,released per kg of Ammonia denitrified

Vaer

(12) Wastewater Engineering Treatment and Resue-Metcalf & Eddy-pg 683 Equation 8-17

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6 Secondary ClarifierNo of Clarifiers = 2Flow to each tank Qa = 40000 m3/d

Qp = 80000 m3/d

Overflow rate at Qa = 10 8-16 is the range

Overflow rate at Qp = 32 24-32 is the rangeSide water Depth SWD = 3.5 m 3.5 to 6 m

Area of each clarifier Qp/OFRp = 2500Dia of the clarifier d = 56.42 m

say = 9.50 m

area at rounded off dia = 70.85

Vol. of clarifier A * SWD = 247.96 Checks

OFR at Qa OFRa = 564.60 ok Hydraulic Retention Time, t

at Qa = 0.1 hr

at Qp = 0.1 hr

164.7 at average flow

= 247.0 at peak flow Clarifiers Dimensions Diameter = 9.50 m SWD = 3.5 m

7 Continuos Backwash FiltersQpeak = 160000

Filter Size ( each cell) L = 2.16 mW = 2.16 m

No of Cells) N = 4 Total filtration area = 18.6624 m2

Filtration rate at Qp = 357.225 m3/m2/hr 8 CCT inlet chamber

HRT at Qpeak flow = 90 secVolume = 166.666667 m3Depth = 1.5

Area = 111.111111 m2Length = 2 mWidth = 56 m

9 Chlorine Contact TankNo of Tanks = 2HRT in tanks at Qp = 30 minutes (15 to 45 at Qp)Volume of each tank = 1666.66667 m3SWD = 1.5 mLength to width ratio L: W ratio = 2Width W = 24.00 mLength L = 48.0 m

OFRa m3/m2/d

OFRp m3/m2/d

Acl m2

m2

Vcl m3

Qa/Acl m3/m2/d

Vcl*24/Qa

Vcl*24/Qp

Solid loading Rate SLR = (Qa+QRAS)*X/(24*1000*Acl) = kg/m2/hr

kg/m2/hr

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Tank dimensions

Length = 48.0 mWidth = 24.00 m

SWD = 1.5 mFB = 0.55 m

10 Sludge Holding TankSludge Wasted /d WAS = 18960 kg/d

Sludge Wasted /d WAS/(Sp Gr *Conc) = 2301.0 m3/d However handling rate based on 7day sludge handled in 5 d = 3221 m3/d

Hydraulic Retention Time, t = 1.5 days

= 4832 m3 Sludge concentration after before desludging = 1.2 % 12 kg/m3

Sludge volume to Dryings Beds = 1533.98 m3/d

Sludge Holding Tank decant = 766.99 m3/d SWD = 3 Length = 40.1 Width = 40.1 Area of Tank = 1610.68

Solids Loading rate = 16.48 kg/m2/d Depth based of HRT = 3.0 m Depth required for 1.2 % conc = 1.3

Available extra depth ( min. = 1.2 % conc depth) = 1.7 mFree Board = 0.5 m

Tank Dimensions Length = 40.1 m

Width = 40.1 mSWD = 3.0 mTotal Depth = 3.5 m

11 Sludge Drying Beds (SDB)

Sludge Volume = 1534.0 m3/d Approach -1 based on Solids loading

Solids loading rate SLR = 75 kg/m2/yr 50-100 kg/m2/yr

Area of SDB WAS*365/SLR = 92272.00 m2Depth of Sludge d = 0.225 m

Volume of beds = 20761 m3

Hyd.Retention Time t = 13.5 dCheckArea/person Area/Population = 0.317 m2/personDivide area into equal area + add 2 beds( 1 as under excavation+ I stand by)Length of each bed L = 21.85Width of each bed W = 14.16No of beds = 298.23Hence provide working no of beds = 6 noTotal no of Beds = 10Drying Period = = 0.27 days

Solids concentration after drying = 30 %Volume of solids after drying = 61.36 m3

Vwas

Sludge holding Tank Volume, Vsl

Vsl

Vwas-Vsl

Vsl

Asdb

Vbeds Asdb*d

Vbeds / Vsl

Filtrate considering no evaporation losses = 1472.62 m3/d

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12 Equipment sizing for Each aeration tank

AOR, 24381.6 kg/d

= AOR*Csw / α *(β*Fa*C'sw-C)(1.024)^(T-20) Where

α 0.60 0.4-0.8 range

Salinity surface tension factor β 0.95 0.7-0.98

Fa 1-(altitude/9450) 1.0Temp.correction factor at field cond. 1.024(T-20) 1.0Min.DO maintained in Aer.Tank C 2.0 mg/l

C'sw 9.1 mg/l O2 sol.in tap water at 20 deg C, Csw 9.08 mg/l SOR 56463.7 kg/d 0.43 (AOR/SOR) Side water depth in Aer Tank SWD 3.8 m Diffuser location from tank bottom d 0.25 m from vendor Diffuser submergence depth d1 SWD-d 3.55 m Air flow per diffuser 4.5 m3/hr from vendor Diffuser eff. per m submergence % 6.5 % from vendor Oxygen content in Air % 21% Diffuser effeciency % 23.1 %

Air density at filed conditions 1.206 kg/m3

Air required, filed conditions 966071.4 m3/d safety factor in order to get over all SF of 1.5 1.29

Air required , m3/hr 52092.8no of working blowers 1.0Air required ,m3/hr 52092.8

Air required, Nm3/hr 47722.6ChecksAir per m3 of tank volume blower capaity/ tank volume 1.15 0.6 -0.9 is the range

12 Power Required for Blowers Effeciency 0.85WRT1/eff = 6052.5529

Inlet pressure (absolute) = 1.01 atms Outlet pressure (absolute)= 1.39 atms

Power required 761.096451 HP Next available 25 HP

Margin = 0.03284735

13 Aeration Requirment for Sludge Holding TankVolume of sludge Holding Tank = 4832 m3Mixing power required = 30 kw/1000 m3 ( range 20-40)Required Kw = 144.96 KwAvailable next Kw = 4 Kw

14 Mixer for Chlorine MixingVolume = 168 m3Gt = 45000G = 500Watts = 42000

O2 under standard conditions of 20OC, SOR, kg/d

O2 Transfer correction factor

O2 Sol.Correc.factor,at field elev.

O2 sol.in tap water(field temp,)

SOR/(air density*O2 %*Diff Eff)

Kw = 42.00

System CurveDia Velocity Area

Suction Dia 0.15 m 1.5 0.017672Discharge Dia 0.1 m 2.4 0.007854Qs 0.026507Qd 0.01885

LossesÑH

Pd Atm 10Ps Atm 10hs suction head 5hd discharge head 15Friction losses

Flowratel/s Total Head

0 10.005 12.22

10 18.8715 29.9620 45.4825 65.4430 89.8335 118.6640 151.9245 189.6250 231.7555 278.3260 329.3365 384.7670 444.6475 508.9580 577.69

[(Pd-Ps)/rg]+(hd-hs)+[(Vd2-Vs2)/2g]+Friction lossed

l/s 0 5 10 15 20 25 30 350.00

20.00

40.00

60.00

80.00

100.00

120.00

140.00

160.00

Total Head

Total Head

Suction Qty K Length Head loss fBellmouth 1 0.05090deg Bend 1 0.400Straight Pipe 1.5Isolation valve 1 0.450Straight Pipe 190 Def bend 1 0.400

1.300 2.5DischargeStraight Pipe 1Isolation Valve 0.4590deg Bend 0.4Straight Pipe 290deg Bend 0.4Straight Pipe 1NRV 0.3Straight Pipe 100Gate valve Pipe exit 1

2.55 104

Vd Vs Term-1 Term-2 Term-3 Term-4 fittings0.00 0.00 0 10 0.00 0.00 ###0.64 0.28 0 10 0.02 2.20 ###1.27 0.57 0 10 0.07 8.80 ###1.91 0.85 0 10 0.15 19.81 ###2.55 1.13 0 10 0.27 35.22 ###3.18 1.41 0 10 0.41 55.02 ###3.82 1.70 0 10 0.60 79.23 ###4.46 1.98 0 10 0.81 107.85 ###5.09 2.26 0 10 1.06 140.86 ###5.73 2.55 0 10 1.34 178.28 ###6.37 2.83 0 10 1.66 220.10 ###7.00 3.11 0 10 2.01 266.32 ###7.64 3.40 0 10 2.39 316.94 ###8.28 3.68 0 10 2.80 371.96 ###8.91 3.96 0 10 3.25 431.39 ###9.55 4.24 0 10 3.73 495.22 ###

10.19 4.53 0 10 4.24 563.45 ###l/s 0 5 10 15 20 25 30 350.00

20.00

40.00

60.00

80.00

100.00

120.00

140.00

160.00

Total Head

Total Head

Nitrification

ConcentrationFrom to

Total N 20 85Organic 8 35Free Ammonia 12 50

Temp 20

NO3-N at outlet 5

inlet TKN 40

Outlet Ammonia,N 1

Kn 1

BODin So 400

BODout Se 10

MLSS 3500

Flow 1500

Inlet Solids 327

Outlet Solids 20

=

=

Safety factor (1.5 to 2.5) =

=

=

By Monod equn =

Organic removal rate

=

HRTn

DenitrificationNet yield of TSS, kg/ kg of BOD removed, 75 % VSSMlvss/MlssOrganic nitrogen content of cells (MLVSS)Soluble TKN,mg/lSoluble TKN,mg/lTKN to be nirtified mg/l

kg/d

μ N15 μ N10 + (20-t/20-10 *(μ N20-μ N10))

Minimum SRT θmc (KN+N/ μ NT *N)

Design SRT θmc

Design Nitrifier Growth rate,μ N

Design Nitrifier Growth rate,μ b 1/θdc =Yb*qb-Kd

Yb = Heterotrophic yield coefficient, Kg VSS sysnthesized /Kg BOD removed

Kb = Endogenous decay co eff.,d-1

μ b = Heterotrophic growth rate ,d-1

qb =rate of substrate BOD to Kg VSS removal, Kg BOD removed/Kg VSS.d

q DN

Mlvss required in the DN reactorMlvss in mg/litVolume of denitrifying reactor

Volume required for nitrification

=

t =f =

Qa*t*f/24 =R ((Ni-Ne/NO3e)-1)*Qa =

=

=capacity =

where

μ = 1.0087 at 20 Deg C

μdnT μdn20*1.09(T-20)*(1-C)

(Ni-Ne)*24/(Xv * μdnT)

Vanx

QRAS

Qr (R- QRAS)

(P/Vanx)=0.00094*(μ)0.3*(X)0.298

P/Vanx kw/m3

Temp10 0.320 0.6530 1.2

0.3 at 20 Deg C

6.67 d

2

13.33 d

0.075 d

0.15 d

0.65

0.05

0.192307692

0.724285714 d

17.38285714 hr

0.65

0.7

0.07

27.5785

1.44

21.1385

31.70775

0.073002141

μ Nd-1

d-1

θc

434.3400002 kg

2450

177.2816327 m3

1086.428571

6.42

10000000000

1.425823E-120.0915378411

at 20 Deg C

Client: ABU DHABI MUNICIPALITY Ref/RFS:

Calc Sheet No.: / /Rev:

Drawings:Page: 1 of

Design: Hemant Kale Date:

Structure:Checked: Date:

Section: Head LossFile:

Design Criteria

Inlet Parameters1 Design Flow

Average Flow = 80000 3333.33333 0.925926 m3/s

= 160000 6666.66667 1.851852 m3/s =2 Chlorine Contact Tank water level = 63.3 63.3

3 Inlet chamber to CCT Weir width = 0.40 m

Qpeak = 1.851852 m3/s No of CCT = 2 Flow to each = 0.925926

Head over weir = 1.173 64.52279Top of weir level = 63.35 63.3Level in inlet chamber = 64.523

4 Filter outlet chamber To CCT inlet chamber

Manning's formula Depth of water in full pipe D at QavgDepth of water partially full pipe d d/D = 0.7 0.7

= 0.85 0.85Q = 1.851852 m3/s 0.925926Qf = 2.178649 m3/s 1.089325

Velocity in pipe when full = 0.75 m/s 0.75Dia of pipe at above velocity, D = 1.923 m 1.360Choose dia = 0.3 m 0.3Velocity at chossen dia = 30.837 m/s 15.419Manning's constant n = 0.0133 0.0133Wetted perimeter, R = 0.075 m 0.075Slope S = 5.410925 541.092 % 1.352731 135.273Fitting Factor Qty Elbow-90 34 2 = 20.4 20.4Elbow-45 14 0 0 0Radial T 22 0 0 0Tee 54 0 0 0Taper 22 0 0 0Straight pipe length = 40 32Toatl length of pipe = 60.4 52.4Drop in levels based on slope = 326.820 m 70.883Other losses Qty k factor

Exit 1 1 = 48.468 m 12.117Entry 1 0.5 = 24.234 m 6.058Valves 0 1 = 0.000 m 0.000

Total head loss = 399.521 m 463.171 89.058Level in filter outlet chamber = 463.171 m 64.523 89.210(as thumb rule pipe dia ODis added to 89.510

Project Name: Raising Capacity of Gayathi STP-Phase-II

Qa m3/d m3/hr

Peak Flow (1) Qp m3/d m3/hr

H=(0.55*Qa/W)^0.66

V=1/n*R2/3*S1/2

at above condition Q/Qf



Drawings:Page: 2 of



Section:Head LossFile:

Design Flow

Average Flow = 80000 3333.33333 0.925926 m3/s

Peak Flow = 160000 6666.66667 1.851852 m3/s

5 Filter to Filter outlet chamberWeir width = 2.16 m No of weirs = 2 mTotal weir width = 4.32Qpeak = 1.851852 m3/s

Head over weir = 0.385 msay = 0.05 m 463.321

Top of weir level = 463.171 463.171Free fall = 0.1

Level of water in Filter = 463.3216 Head Loss across the Filters


No of Cells) N = 4Total filtration area = 18.6624 m2Solids into Filter = 10 mg/lSolids out of Filter = 5 mg/lSolids captured = 400 kg/dSollid capture = 1.5 kg/m3/dHead Loss across the Filters = 14.29 mAdd = 0.15 m 477.761Total head loss = 14.44 m 463.321Level in Inlet chamber of the Filter = 477.76

7 Head loss from Outlet chamber of Secondary Clarifier to Inlet Chamber of Filtera Individual S/Clarifiers to Commom headerNo of clarifiers = 2 2

Manning's formula Depth of water in full pipe D AT QavgDepth of water partially full pipe d d/D = 0.7 0.7

= 0.85 0.85Q = 0.925926 m3/s 0.462963Qf = 1.089325 m3/s 0.544662

Velocity in pipe when full = 0.75 m/s 0.75Dia of pipe at above velocity, D = 1.360 m 0.962Choose dia = 0.2 m 0.2Velocity at chossen dia = 34.692 m/s 17.346Manning's constant n = 0.0133 0.0133Wetted perimeter, R = 0.05 m 0.05Slope S = 11.79068 1179.068 % 2.94767


Qa m3/d m3/hr

Qp m3/d m3/hr

H=(0.55*Qa/W)^0.66

V=1/n*R2/3*S1/2




Drawings:Page: 3 of




Fittings Factor Qty Elbow-90 34 2 = 13.6Elbow-45 14 1 2.8

Radial T 22 0 0Tee 54 1 10.8Taper 22 0 0Straight pipe length = 22Toatl length of pipe = 49.2Drop in levels based on slope = 580.101 mOther losses Qty k factor

Exit 0 1 = 0.000 mEntry 1 0.5 = 30.671 mValves 0 1 = 0.000 m

Total head loss = 610.772 m

b Head loss through Common Pipe

Manning's formula Depth of water in full pipe D Depth of water partially full pipe d d/D = 0.7 0.7

= 0.85 0.85 Q = 1.851852 m3/s 0.925926 m3/sQf = 2.178649 m3/s 1.089325 m3/s

Velocity in pipe when full = 0.75 m/s 0.75 m/sDia of pipe at above velocity, D = 1.923 m 1.360 mChoose dia = 0.3 m 0.3 m

Velocity at chossen dia = 30.837 m/s 15.419 m/sManning's constant n = 0.0133 0.0133Wetted perimeter, R = 0.075 m 0.075 mSlope S = 5.410925 541.092 % 1.352731 135.273Fitting Factor Qty Elbow-90 34 2 = 20.40 20.40Elbow-45 14 1 4.20 4.20Radial T 22 1 6.60 6.60Tee 54 1 16.20 16.20Taper 22 0 0.00 0.00Straight pipe length = 50 50Toatl length of pipe = 97.4 97.4Drop in levels based on slope = 527.024 m 131.756 mOther losses Qty k factor

Exit 1 1 = 48.468 m 12.117 mEntry 0 0.5 = 0.000 m 0.000 mValves 1 1 = 48.468 m 12.117 m

Head loss thro'common header = 623.959 m 155.990 mHead loss- S/C outlet chamber to filter inlet = 1234.732 155.990

say = 1234.700 m 0.5 mLevel in Inlet chamber of the Filter = 477.76 1712.461 0.00 0.500Level in Outlet chamber of the clarifer = 1712.46 477.761 0.50


V=1/n*R2/3*S1/2




Drawings:Page: 4 of




Design Flow

Average Flow = 80000 3333.33333 0.925926 m3/s

Peak Flow = 160000 6666.66667 1.851852 m3/s

Qras Qras = 80000 3333.33333 0.925926 m3/s8 Outlet Chamber of the S/Clarifier 1713.06 Launder Top level Head loss D/S = 1234.7 m

Pipe dia = 0.2 m 1712.461 1712.461 Water LevelInvert level of chamber = 477.56 IL of IL of chamberS/C launder invert level = 1712.46 S/C laund 477.56

Launder Depth = 0.6 m ChamberTop of concrete of launder = 1713.06

9 Head over the V notch Q= 8/15*Cd*tanθ/2*√2*9.81*H5/2 Launder width = 0.4 m Circumference of the each clarifier = 27.33 m C/C distance of V notch = 0.15 m No of notches = 182 n 1713.11 Weir plate Level Qpeak /per V notch Q = 0.005088 m3/s Angle of V notch θ = 90.00 deg 1713.17 water Level in V notch

Coefficient of discharge Cd = 0.61 Head over the V notch = 0.10 m 104 mm Water Level in V notch = 1713.166

10 Side water depth of clarifier SWD = 3.5 m Hopper top level = 1709.67

11 Aeration Tank outlet to each S/Clarifier

Manning's formula Depth of water in full pipe D

Depth of water partially full pipe d d/D = 0.7 0.7

= 0.85 0.85Q = 1.389 m3/s 0.926

Qf = 1.634 m3/s 1.089

Velocity in pipe when full = 0.750 m/s 0.750Dia of pipe at above velocity, D = 1.666 m 1.360Choose dia = 0.3 m 0.3 Velocity at chossen dia = 23.128 m/s 15.419Manning's constant n = 0.0133 0.0133Wetted perimeter, R = 0.075 m 0.075Slope S = 3.043645 304.365 % 1.352731Fitting Factor Qty Elbow-90 34 3 = 30.60 30.60Elbow-45 14 1 4.20 4.20Radial T 22 0 0.00 0.00Tee 54 0 0.00 0.00Taper 22 0 0.00 0.00Straight pipe length = 35 35Total length of pipe = 69.80 69.80Drop in levels based on slope = 212.446 m 0.944


Qa m3/d m3/hr

Qp m3/d m3/hr

m3/hr

V=1/n*R2/3*S1/2




Drawings:Page: 5 of




Average Flow = 80000 3333.33333 0.925926 m3/s

Peak Flow = 160000 6666.66667 1.851852 m3/s

Qras Qras = 80000 3333.33333 0.925926 m3/s

Other losses Qty k factorExit 1 1 = 27.263 mEntry 1 0.5 = 13.632 mValves 1 1 = 27.263 m

Head loss thro'common header = 280.604 m Head loss- AT outlet to S/Clarifier = 280.604 m say = 280.604 m 1993.770 Level in S/clarifier = 1713.17 1713.166 Level in Outlet of AT = 1993.77

12 Level in Aeration Tank Weir width = 0.60 m Q(Qpeak+Qras) = 2.778 m3/s

No of AT = 2.000 nos Flow to each = 1.389 m3/s

Head over weir = 1.173 m 1994.992Allow for free Fall = 0.05 m 1993.77Top of weir level = 1993.770Water Level in Aeration tank = 1994.992Bottom Level of AT at center of tank = 1991.192 1994.905 1991.192 1987.480

Bottom Level of AT at OUTLET = 1987.480 U/stream centre d/s stream Bottom level of AT c/wall with Anoxic Tank = 1994.905

13 Anoxic Tank to Aeration TankProvide opening bewteen An Tk and Ae Tank

Width = 400 mmHeight = 400 mmArea = 0.16 m2

Q(Qavg+Qras+Qir) per tank = 195000 m3/d 8125.00 2.26 m3/s

Q(Qpeak+Qras+Qir) per tank = 235000 m3/d 9791.67 2.72 m3/sVelocity at (Qavg+Qras+Qir) per tank = 14.106 m/s m3/sVelocity at (Qpeak+Qras+Qir) per tank = 16.999 m/sVelocity head at max velocity = 14.729 m ### mmLevel in Aeration Tank = 1994.992 2009.72 1994.99Level in Anoxic Tank = 2009.721

1994.905 1994.905Anoxic Aeartion


Qa m3/d m3/hr

Qp m3/d m3/hr

m3/hr

H=(0.55*Qa/W)^0.66

m3/hr

m3/hr



Drawings:Page: 6 of




Average Flow = 80000 3333.33333 0.925926 m3/s

Peak Flow = 160000 6666.66667 1.851852 m3/s

14 Distribution Box to Anoxic Tank Tank

Manning's formula Depth of water in full pipe D Depth of water partially full pipe d d/D = 0.7

= 0.85 Q = 1.389 m3/sQf = 1.634 m3/s

Velocity in pipe when full = 0.750 m/s Dia of pipe at above velocity, D = 1.666 m Choose dia = 0.25 m Velocity at chossen dia = 33.304 m/s Manning's constant n = 0.0133 Wetted perimeter, R = 0.0625 m Slope S = 8.0579 805.790 % Fitting Factor Qty

Elbow-90 34 2 = 0.00Elbow-45 14 0 0.00

Radial T 22 0 0.00Tee 54 0 0.00Taper 22 0 0.00Straight pipe length = 0Total length of pipe = 0.00

Drop in levels based on slope = 0.000Other losses Qty k factor


Toatl Head loss = 0.000 Head loss- D/Box to Anoxic Tank = 0.000 m

say = 0.000 m 1994.992Level in Anoxic Tank = 2009.72 2009.721Level in Distribution Box = 1994.992

15 Distrbution BoxWeir width = 1.00 m Qpeak = 1.389 m3/s

Head over weir = 0.837 m Allow for free Fall = 0.1 mWorst case when flow is full and I stream closed 1995.930Head over weir = 1.012 1994.992 Top of weir level = 1995.092 Level of water over weir = 1995.930Depth of flow in Box = 0.500 1994.592 Bottom Level of Box = 1994.592


Qa m3/d m3/hr

Qp m3/d m3/hr

V=1/n*R2/3*S1/2


H=(0.55*Qa/W)^0.66



Drawings:Page: 7 of




Average Flow = 80000 3333.33333 0.925926 m3/s

Peak Flow = 160000 6666.66667 1.851852 m3/s

16 Grit Chammber To Distribution Box


= 0.85 Q = 1.852 m3/sQf = 2.179 m3/s


Elbow-90 34 2 = 20.40Elbow-45 14 0 0.00


Drop in levels based on slope = 245.656 Other losses Qty k factor

Exit 1 1 = 48.468 mEntry 1 0.5 = 24.234 mValves 0 1 = 0.000 m 2314.287

Toatl Head loss = 318.357 say = 318.357 m Grit 1995.930

Level in Grit Channel = 2314.29 Channel


Qa m3/d m3/hr

Qp m3/d m3/hr

V=1/n*R2/3*S1/2




Drawings:Page: 1 of




Design Criteria

Inlet Parameters1 Design Flow

Average Flow = 80000 3333.33333 0.925926 m3/s

= 160000 6666.66667 1.851852 m3/s

RAS flow = 80000 3333.33333 0.925926 m3/s

IR flow = 230000 9583.33333 2.662037 m3/sNo of streams = 2

Anoxic Mixer


Qa m3/d m3/hr

Peak Flow (1) Qp m3/d m3/hr

m3/d m3/hr

m3/d m3/hr



Drawings:Page: 2 of




Design Flow

Average Flow = 80000 3333.33333 0.925926 m3/s

Peak Flow = 160000 6666.66667 1.851852 m3/s

5 Filter to Filter outlet chamberWeir width = 2.16 m No of weirs = 2 mTotal weir width = 4.32Qpeak = 1.851852 m3/s

Head over weir = 0.385 msay = 0.05 m 0.100

Top of weir level = 0.000 0.000Free fall = 0.05

Level of water in Filter = 0.1006 Head Loss across the Filters


No of Cells) N = 4Total filtration area = 18.6624 m2Solids into Filter = 10 mg/lSolids out of Filter = 5 mg/lSolids captured = 400 kg/dSollid capture = 1.5 kg/m3/dHead Loss across the Filters = 14.29 mAdd = 0.2 m 14.600Total head loss = 14.50 m 0.100Level in Inlet chamber of the Filter = 14.60

7 Head loss from Outlet chamber of Secondary Clarifier to Inlet Chamber of Filtera Individual S/Clarifiers to Commom headerNo of clarifiers = 2


= 0.85 Q = 0.925926 m3/sQf = 1.089325 m3/s

Velocity in pipe when full = 0.75 m/sDia of pipe at above velocity, D = 1.360 mChoose dia = 0.2 mVelocity at chossen dia = 34.692 m/sManning's constant n = 0.0133Wetted perimeter, R = 0.05 mSlope S = 11.79068 1179.068 %


Qa m3/d m3/hr

Qp m3/d m3/hr

H=(0.55*Qa/W)^0.66

V=1/n*R2/3*S1/2




Drawings:Page: 3 of




Fittings Factor Qty Elbow-90 34 0 = 0Elbow-45 14 0 0

Radial T 22 0 0Tee 54 0 0Taper 22 0 0Straight pipe length = 20Toatl length of pipe = 20Drop in levels based on slope = 235.814 mOther losses Qty k factor


Total head loss = 266.484 m =

b Head loss through Common Pipe


= 0.85 Q = 1.851852 m3/sQf = 2.178649 m3/s

Velocity in pipe when full = 0.75 m/sDia of pipe at above velocity, D = 1.923 mChoose dia = 0.3 m

Velocity at chossen dia = 30.837 m/sManning's constant n = 0.0133Wetted perimeter, R = 0.075 mSlope S = 5.410925 541.092 %Fitting Factor Qty Elbow-90 34 1 = 10.20Elbow-45 14 0 0.00Radial T 22 1 6.60Tee 54 0 0.00Taper 22 0 0.00Straight pipe length = 20Toatl length of pipe = 36.8Drop in levels based on slope = 199.122 mOther losses Qty k factor


Head loss thro'common header = 296.057 m Head loss- S/C outlet chamber to filter inlet = 562.542

say = 0.5 m 15.100Level in Inlet chamber of the Filter = 14.60 14.600Level in Outlet chamber of the clarifer = 15.10


V=1/n*R2/3*S1/2




Drawings:Page: 4 of




Design Flow

Average Flow = 80000 3333.33333 0.925926 m3/s

Peak Flow = 160000 6666.66667 1.851852 m3/s

Qras Qras = 80000 3333.33333 0.925926 m3/s8 Outlet Chamber of the S/Clarifier 15.70 Launder Top level Head loss D/S = 0.5 m

Pipe dia = 0.3 m 15.100 15.100 Water LevelInvert level of chamber = 14.30 IL of IL of chamberS/C launder invert level = 15.10 S/C laund 14.30

Launder Depth = 0.6 m ChamberTop of concrete of launder = 15.70

9 Head over the V notch Q= 8/15*Cd*tanθ/2*√2*9.81*H5/2 Launder width = 0.4 m Circumference of the each clarifier = 27.33 m C/C distance of V notch = 0.15 m No of notches = 182 n 15.75 Weir plate Level Qpeak /per V notch Q = 0.005088 m3/s Angle of V notch θ = 90.00 deg 15.80 water Level in V notch

Coefficient of discharge Cd = 0.61 Head over the V notch = 0.10 m 104 mm Water Level in V notch = 15.804

10 Side water depth of clarifier SWD = 3.5 m Hopper top level = 12.30

11 Aeration Tank outlet to each S/Clarifier

Manning's formula Depth of water in full pipe D

Depth of water partially full pipe d d/D = 0.7

= 0.85 Q = 1.389 m3/s

Qf = 1.634 m3/s

Velocity in pipe when full = 0.750 m/sDia of pipe at above velocity, D = 1.666 mChoose dia = 0.25 mVelocity at chossen dia = 33.304 m/sManning's constant n = 0.0133Wetted perimeter, R = 0.0625 mSlope S = 8.0579 805.790 %Fitting Factor Qty Elbow-90 34 3 = 25.50Elbow-45 14 0 0.00Radial T 22 0 0.00Tee 54 0 0.00Taper 22 0 0.00Straight pipe length = 20Total length of pipe = 45.50Drop in levels based on slope = 366.634 m


Qa m3/d m3/hr

Qp m3/d m3/hr

m3/hr

V=1/n*R2/3*S1/2




Drawings:Page: 5 of




Average Flow = 80000 3333.33333 0.925926 m3/s

Peak Flow = 160000 6666.66667 1.851852 m3/s

Qras Qras = 80000 3333.33333 0.925926 m3/s

Other losses Qty k factorExit 1 1 = 56.533 mEntry 1 0.5 = 28.266 mValves 0 1 = 0.000 m

Head loss thro'common header = 451.433 m Head loss- AT outlet to S/Clarifier = 451.433 m say = 0.3 m 16.104 Level in S/clarifier = 15.80 15.804 Level in Outlet of AT = 16.10

12 Level in Aeration Tank Weir width = 0.60 m Q(Qpeak+Qras) = 2.778 m3/s

No of AT = 2.000 nos Flow to each = 1.389 m3/s

Head over weir = 1.173 m 17.327Allow for free Fall = 0.05 m 16.10Top of weir level = 16.104Water Level in Aeration tank = 17.327Bottom Level of AT at center of tank = 13.527 17.240 13.527 9.815

Bottom Level of AT at OUTLET = 9.815 U/stream centre d/s stream Bottom level of AT c/wall with Anoxic Tank = 17.240

13 Anoxic Tank to Aeration TankProvide opening bewteen An Tk and Ae Tank

Width = 400 mmHeight = 400 mmArea = 0.16 m2

Q(Qavg+Qras+Qir) per tank = 195000 m3/d 8125.00 2.26 m3/s

Q(Qpeak+Qras+Qir) per tank = 235000 m3/d 9791.67 2.72 m3/sVelocity at (Qavg+Qras+Qir) per tank = 14.106 m/s m3/sVelocity at (Qpeak+Qras+Qir) per tank = 16.999 m/sVelocity head at max velocity = 14.729 m ### mmLevel in Aeration Tank = 17.327 32.06 17.33Level in Anoxic Tank = 32.056

17.240 17.240Anoxic Aeartion


Qa m3/d m3/hr

Qp m3/d m3/hr

m3/hr

H=(0.55*Qa/W)^0.66

m3/hr

m3/hr



Drawings:Page: 6 of




Average Flow = 80000 3333.33333 0.925926 m3/s

Peak Flow = 160000 6666.66667 1.851852 m3/s

14 Distribution Box to Anoxic Tank Tank


= 0.85 Q = 0.926 m3/sQf = 1.089 m3/s


Elbow-90 34 2 = 13.60Elbow-45 14 0 0.00


Drop in levels based on slope = 396.167Other losses Qty k factor


Toatl Head loss = 488.179 Head loss- D/Box to Anoxic Tank = 488.179 m

say = 0.4 m 32.856Level in Anoxic Tank = 32.46 32.456Level in Distribution Box = 32.86

15 Distrbution BoxWeir width = 1.00 m Qpeak = 0.926 m3/s

Head over weir = 0.641 m Allow for free Fall = 0.05 mWorst case when flow is full and I stream closed 33.547Head over weir = 1.012 32.856 Top of weir level = 32.906 Level of water over weir = 33.547Depth of flow in Box = 0.500 32.406 Bottom Level of Box = 32.406


Qa m3/d m3/hr

Qp m3/d m3/hr

V=1/n*R2/3*S1/2


H=(0.55*Qa/W)^0.66

Head loss Calculation Raw sewage Pumping ABV ROCK SITE -5

BY HRK

hf=6.82*(V/C)^1.85*L/D^1.167PIPE LENGTH 160.00 160.00FLOW , m3/d 4500 4500m3/hr 187.50 187.50m3/s 0.05 0.05PIPE DIAMETER, mm 300 300PIPE DIAMETER, m 0.30 0.30AREA 0.07 0.07VELOCITY , m/s 0.74 0.74C 100.00 140.00V/C^1.85 0.0 0.0L/D^1.167 652.11 652.11HEAD LOSS, hf m 0.50 0.27HEAD LOSS PIPE FITTINGS

Quantity K values K * V^2/2gVALVES 1.00 0.19 0.0052629Check Valves 1.00 0.6 0.0166198ELBOWS 3.00 0.28 0.0232677TEES 0.00 0.7 0ENTRANCE 1.00 1 0.0276996EXIT 1.00 0.75 0.0207747Head loss through fittings 0.0936248Head Loss in meters thr pipe and fittings 0.60add 10 % extra 0.66Static Head 0Total Head Loss 0.66

Qa 4148.6 m3/dPeak factor 3.41Peak flow 14146.73 m3/d

0.163735 m3/s

1 Mechanical Bar ScreenFlow 4148.60 m3/dClear spacing 25.00 mmScreening Removed 20.00 m3/mldQuantity of Screenings 0.08 m3/dScreenings bin with storage of 7.00 daysVolume of Bin 0.58 m3

2 Approach & flow through velocitiesMax. Vel. At feed channel 1.00 m/sMax. Vel. at screen face 1.00 m/s

Approach velocityClear spacing 25.00 mmThickness of bars 6.00 mmFlow through screen Velcoity Vsc 0.90 m/sAproach velocity V1 0.73 m/sHead loss Vsc^2-V1^2/2*g*Cd^2 0.02 mH1 20.46 mm

Downstream depth of flow 262 mmDepth U/S of screen Yc 282.46

0.28 mClear width of Screen Wsc 0.64 mRequired Screen width 0.80 mFree Board at Qpeak 0.35 mTotal depth 0.63 m

For Screens 50 % blockedFlow area =

SPREADSHEET FOR ACTIVATED SLUDGE PROCESS

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