Heat Balance Calculations
32
Heat in=out Heat Input = Heat Output Heat Input Combustion heat of Fuel. Sensible heat of Raw Meal. Sensible heat of Fuel. Sensible heat of Air. i. Primary air. ii. Secondary air. iii. Tertiary air. iv. ByPass Quench air. Sensible heat of Cooing Water. i. ByPass Cond. Tower. ii. Clinker Crusher. iii. Cooler. Heat Output Clinker heat of formation. Heat loss with preheater exit gas. i. Exit gas. ii. Evaporation of water. iii. Dust. iv. CO. Heat loss with bypass exit gas. i. Bypass gas. ii. Evaporation of water from cond. Tower. Heat loss with bypass dust. Heat loss with clinker crusher water. Heat loss with clinker. Heat loss with cooler exit gas. i. Cooler exit gas. ii. Evaporation of water. Heat loss due to radiation & convection. i. Radiation from kiln. ii. Radiation from cooler. Heat Balance Q 1 Q 2 Q 3 Q 4 Q 5 Q 6 Q 7 Q 8 Q 9 Q 10 Q 11 Q 12 Q 13 Q 14 Q 15 Q 16
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Heat Balance Calculations
Transcript of Heat Balance Calculations
Heat in=out
Heat Input = Heat Output
Heat Input
Combustion heat of Fuel.
Sensible heat of Raw Meal.
Sensible heat of Fuel.
Sensible heat of Air.i. Primary air.ii. Secondary air.iii. Tertiary air. iv. ByPass Quench air.
Sensible heat of Cooing Water.i. ByPass Cond. Tower.ii. Clinker Crusher. iii. Cooler.
Heat Output
Clinker heat of formation.
Heat loss with preheater exit gas.i. Exit gas.ii. Evaporation of water.iii. Dust.iv. CO.
Heat loss with bypass exit gas.
i. Bypass gas.
ii. Evaporation of water from cond. Tower.
Heat loss with bypass dust.
Heat loss with clinker crusher water.
Heat loss with clinker. Heat loss with cooler exit gas.
i. Cooler exit gas.
ii. Evaporation of water.Heat loss due to radiation & convection.
i. Radiation from kiln.
ii. Radiation from cooler.
Heat Balance
Q1
Q2
Q3
Q4
Q5
Q6
Q7
Q8
Q9
Q10
Q11
Q12
Q13
Q14
Q15
Q16
Heat in=out
iii. Radiation from preheater.Q17
1. Combustion Heat of Fuel
= F * Hc / P Where
Commbustion Heat
F Fuel Consumption (Main burner + Calciner)
Fuel Heat Content
P Clinker Production
Main burner 2240.45
Calciner burners 2810.29
F 5050.74 (Performance Test)
9500 (Fuel Analysis)P 38178.5 (Performance Test)
1256.8
Q1
Q1
Kcal / Kg ck
Kg f / hr
Hc
Kcal / Kg f
Kg ck
/ hr
Kg f / hr
Kg f / hr
Hc
Q1
Kcal / Kg ck
Q1
2. Sensible Heat of Raw Meal (Kiln Feed)
=Where
Sensible Heat of Raw Meal
M Kiln feed flow rate
Cp Specific Heat of Raw Meal
Kiln Feed Temperature
Ambient Temperature
P Clinker Production
M 67282.8 (Performance Test)Cp 0.22 (Table page )
83 (Thermometer)
30 (Assumption)P 38178.5 (Performance Test)
20.5
Q2
M * Cp * ( T2 - T
1 ) / P
Q2
Kcal / Kg ck
Kg raw
/ hr
Kcal / Kg raw
oC
T2
oCT
1oC
Kg ck
/ hr
T2
T1
Q2
Kcal / Kg ck
Q2
3. Sensible Heat of Fuel
=Where
Sensible Heat of Fuel
M Fuel flow rate (Main burner + Calciner )
Cp Specific Heat of Fuel
Fuel Temperature
Ambient Temperature
P Clinker Production
M 5050.7 (Performance Test)Cp 0.47 (Table page )
115 (Thermometer)
30 (Assumption)P 38178.5 (Performance Test)
5.2
Q3
M * Cp * ( T2 - T
1 ) / P
Q3
Kcal / Kg ck
Kg f / hr
Kcal / Kg f
oC
T2
oCT
1oC
Kg ck
/ hr
T2
T1
Q3
Kcal / Kg ck
Q3
4. Sensible Heat Of Airi. Primary Air.
ii. Secondary Air.iii. Tertiary Air.iv. ByPass Quench Air.
=
=Where
Sensible Heat of Air
M Air Flow rate
Cp Specific Heat Of Air
Air Temperature
Ambient Temperature
P Clinker Production
Asuming
=Therefore
= 0
Q4
Qprim
+ Qsecond
+ Qterti
+ Qquench
Q4
M * Cp * ( T2 - T
1 ) / P
Q4
Kcal / Kg ck
m3 / h
Kcal / m3 oCT
2oC
T1
oCKg
ck / hr
T2
T1
Q4
Kcal / Kg ck
Q4
5. Sensible Heat of Cooling Wateri. ByPass Cond. Tower
ii. Clinker Crusheriii. Cooler
=
=Where
Sensible Heat of Water
M Water Flow rate
Cp Specific Heat Of Water
Water Temperature
Ambient Temperature
P Clinker Production
Asuming
=Therefore
= 0
Q5
Qc.t
. + Qcrusher
+ Qcooler
Q5
M * Cp * ( T2 - T
1 ) / P
Q5
Kcal / Kg ck
m3 / h
Kcal / m3 oCT
2oC
T1
oCKg
ck / hr
T2
T1
Q5
Kcal / Kg ck
Q5
1. Clinker Heat of Formation
Lab. Analysis Raw Mix Clinker
Moisture 0.25
Titration 80.2
80.1
0.24
15.46 25.02
3.13 4.85
0.12 0.25
CaO 44.56 68.18
MgO 0.11 0.27
0.06 0.09
0.04 0.06
S 0 0.61
0.06
L.O.I. 35.95 0.21
Sum 99.49 99.54
LSF
SM
AM
Raw Mix To Clinker Factor (Ck Factor)= 100 / (100 - L.O.I.)= 1.5613 Kg / Kg Clinker
as follows ,
CaO == 70.0328 Kg / Kg Clinker
MgO = MgCO3 * Ck Factor * 40.3 / 84.30.17913 Kg / Kg Clinker
=
+
= 418.835
CaCO3
MgCO3
SiO2
Al2O
3
Fe2O
3
K2O
Na2O
Combined H2O
CaO & MgO calculated from CaCO3 & MgCO
3 in Raw Mix
CaCO3 * Ck Factor * 56 / 100
Q6
(7.646 * CaO) + (6.48 * MgO) + (2.22 * Al2O
3)
(11.6 * Ck Factor * H2O) - (5.116 * SiO
2) - (0.59
* Fe2O
3) - (10 * {K2O + Na2O}) - (32 * Ck Factor * S)
Q6
Kcal / Kg ck
Q6
2. Heat Loss With Preheater Exit Gas
=Where
Heat Loss With Preheater Exit Gas
M Preheater Exit Gas Flow rate
Cp Specific Heat of Exit Gas
Preheater Exit Gas Temperature
Ambient Temperature
P Clinker Production
M 83008.4 (Calculation)Cp 0.31 (Table page )
440 (Thermometer)
30 (Assumption)P 38178.5 (Performance Test)
276.3N.B.
Air Cp 0.31
ρ 1.293Sp.heat 0.237 Kcal / Kg
M
1.Process Flow Sheet 80985.2
2. Fuel Consumption 83008.4
3. Combustion Calculations 79353.803
Preheater Exit Gas CalculationProcess Update
I.D. Fan Flow Rate 65000 MKiln Feed 54 67.28 t / hFuel Consumption 3955 5050.74 Kg / h
i. Process Flow Sheet
M = 65000 * 67.28 / 54 = 80985.19
ii. Fuel Consumption
M = 65000*5050.7 / 3955 = 83008.37
iii. Combustion Calculations
M = 79353.8
Q7
M * Cp * ( T2 - T
1 ) / P
Q7
Kcal / Kg ck
m3 / h
Kcal / m3 oCT
2oC
T1 oC
Kg ck
/ h
T2
T1
Q7
Kcal / Kg ck
Q7
Kcal / m3 oC
Kg / m3
m3 / h
m3 / h
m3 / h
m3 / h
m3 / h
m3 / h
m3 / h
(See Mixing Chamber Balance)
AirPrimary Air = 3000Secondary Air 43600*67.28/54 = 54322Total 57322
Calculations Air = 0.26 * Hu
= 0.26 * 1256.7 * 38178.5 * 4.187 / 1000= 52230.8
Excess Air = 11 - 3.762 * CO 0.50%
2.50%
= 10% = 52230.8 * 0.1= 5223.1
Total Air = Min Air + Excess Air= 52230.8 + 5223.1= 57453.9
Comb. ProductsComb. Products = 0.29 * Hu
= 0.29 * 1256.7 * 38178.5 * 4.187 / 1000= 58257.445
= 22.26/100 * titration * Ck factor= 22.26/100 * 80.2/100 * 1.76= 0.32= 12217.12
Excess Air = 11 - 3.762 * CO 0.50%
2.50%
= 10% = 52230.8 * 0.1= 5223.1
Total Combustion Products== 75697.6
Nm3 / hNm3 / hNm3 / h
(Nm3 / MJ)
Nm3 / h
Cyclone 1 O
2 - 0.5 * CO
N2
O2
3.762*O2
Nm3 / h
Nm3 / h
(Nm3 / MJ)
Nm3 / h
CO2
Nm3 CO2 / Kg
ck
Nm3 CO2 / h
Cyclone 1 O
2 - 0.5 * CO
N2
O2
3.762*O2
Nm3 / h
Comb. Products + CO2 +
Excess Air
Nm3 / h
Exit gasPreheater Exit Gas + Dust
HeatDust Exchanger
Air Air
= + +
Q = M * Cp * T / P
= 79353.80 * 0.31 * 440 / 38178.47
= 283.50688
= 6391.8632 * 0.22 * 440 / 38178.47
= 16.206316
= 57453.893 * 0.31 * 30 / 38178
= 13.995354
= 313.709
= + +
= 79353.80 * 0.31 * 300 / 38178.47
= 193.30014
= 6391.8632 * 0.22 * 300 / 38178.47
= 11.049761
= 57453.893 * 0.31 * 210 / 38178.47
= 97.967478
= 302.317
N.B.M (dust) = 9.50% of Kiln Feed
Heat Exchanger Heat Balance
Q input
Q gas
Q dust
Q air
Q gas
Kcal / Kg ck
Q dust
Kcal / Kg ck
Q air
Kcal / Kg ck
Q input
Kcal / Kg ck
Q output
Q gas
Q dust
Q air
Q gas
Kcal / Kg ck
Q dust
Kcal / Kg ck
Q air
Kcal / Kg ck
Q output
Kcal / Kg ck
3.Heat Loss With ByPass Exit Gas
i. ByPass Exit Gas
=
Where
Heat Loss With ByPass Exit Gas
M ByPass Exit Gas Flow rate
Cp Specific Heat of Exit Gas
ByPass Exit Gas Temperature
Ambient Temperature
P Clinker Production
M 51770 (Pitot Measurements)Cp 0.31 (Table page )
134 (Thermometer)
30 (Assumption)P 38178.5 (Performance Test)
43.72
N.B.
Air Cp 0.31
ρ 1.293Sp.heat 0.237 Kcal / Kg
ii. Evaporation of Water from ByPass Cond. Tower
= M λ / Pwhere
Heat Loss With Evap. of Water
M Water Flow rate
λ Heat of Vaporization
P Clinker Production
M 3700 (Process Flow Sheet)
λ 539 (Table page )P 38178.5 (Performance Test)
52.24
N.B.
Water λ 539 Kcal / Kg
ρ 1000
Q8
M * Cp * ( T2 - T
1 ) / P
Q8
Kcal / Kg ck
m3 / h
Kcal / m3 oCT
2oC
T1 oC
Kg ck
/ h
T2
T1
Q8
Kcal / Kg ck
Q8
Kcal / m3 / oC
Kg / m3
Q9
Q9
Kcal / Kg ck
Kg water
/ h
Kcal / Kg water
Kg ck
/ h
Q9
Kcal / Kg ck
Q9
Kg / m3
ByPass Exit Gas Calculation
Process Update
ByPass Fan Flow Rate 28720 M
Kiln Feed 54 67.28 t / h
Fuel Consumption 3955 5050.74 Kg / h
i. Process Flow Sheet
M = 28720*67.28 / 54 = 35783
ii. Fuel Consumption
M = 28720*5050.7 / 3955 = 36676.93
iv. Pitot Measurment
M = 51770
M
Process Flow Sheet 35783
Fuel Consumption 36677
Pitot Measurments 51770
m3 / h
m3 / h
m3 / h
m3 / h
m3 / h
m3 / h
m3 / h
Mixing Chamber Balance
Gas Mixing Gas + Quench Air
Dust Chamber
Quench Air Dust
=
? 1875 Kg / h 8300
0.31 0.22 0.31
1100 1100 30
450 450 450
= 4032.43
Kiln Combustion Products= 0.29 * 0.45 * Hu= 0.29 * 0.45 * 1256.7 * 38178.5 * 4.187 / 1000
= 26215.85
= 12217.12 * 0.04
= 488.6848
Excess Air= 1 Smoke Chamber
1 - 3.762 * CO 0.50%
1.75%
= 7%= 52230.8 * 0.07
= 3656.16
Total = 30360.69
ByPass %
= %
= 13.28
Qg
+ Qd + Q
a = Q
g + Q
d + Q
a
Mg C
pg T
i + M
d Cp
d T
i + M
a Cp
a T
i = M
g C
pg T
o + M
d Cp
d T
o + M
a Cp
a T
o
Mg C
pg (T
i - T
o) M
d Cp
d (T
o -
T
i) + M
a Cp
a (T
o - T
i)
Mg Nm3 / h M
dM
a Nm3 / hCp
g Kcal/m3 oC Cpd Kcal/KgoC Cp
a Kcal/m3 oCT
ioC T
ioC T
ioC
To
oC To
oC To
oC
Mg Nm3 / h
(Nm3 / MJ)
Nm3 / h
CO 2
Nm3 CO2 / h
O2 - 0.5 * CO
N2
O2
3.762*O2
Nm3 / h
Nm3 / h
Mg
/ Total
Calciner Combustion Products
= 0.29 * 0.55 * Hu
= 0.29 * 0.55 * 1256.7 * 38178.5 * 4.187 / 1000
= 32041.59
= 12217.12 * 0.96
= 11728.44
Excess Air
= 1 Cyclone 1
1 - 3.762 * CO 0.50%
2.50%
= 10%= 52230.8 * 0.1
= 5223.08
Total = 48993.11
Total Combustion Products
= Kiln Combustion Products + Calciner Combustion Products
= 30360.69 + 48993.11
= 79353.80
(Nm3 / MJ)
Nm3 / h
CO 2
Nm3 CO2 / h
O2 - 0.5 * CO
N2
O2
3.762*O2
Nm3 / h
Nm3 / h
Nm3 / h
4. Heat Loss with ByPass Dust
=
whereHeat Loss with ByPass Dust
M ByPass DustCp Specific Heat of Dust
ByPass Dust TemperatureAmbient Temperature
P Clinker Production
M 1980 (ByPass Weighing Test)Cp 0.22 (Table page )
60 (Thermometer)30 (Assumption)
P 38178.5 (Performance Test)
0.34
Q10
M * Cp * ( T2 - T
1 ) / P
Q10
Kcal / Kg ck
Kg dust
/ h
Kcal / Kg dust
oCT
2oC
T1 oC
Kg ck
/ h
T2
T1
Q10
Kcal / Kg ck
Q10
5. Heat Loss with Clinker Crusher Water
=
whereHeat Loss with Ck Crusher Water
M Water Flow rate
Cp Specific Heat of Water
Water outlet TemperatureWater inlet Temperature
P Clinker Production
M 36000 (Site Flowmeter)Cp 0.48 (Table page )
40 (Thermometer)30 (Thermometer)
P 38178.5 (Performance Test)4.53
N.B.Water 0.48
ρ 1000
Q11
M * Cp * ( T2 - T
1 ) / P
Q11
Kcal / Kg ck
Kg water
/ h
Kcal / Kg water
oC
T2
oCT
1 oC
Kg ck
/ h
T2
T1
Q11
Kcal / Kg ck
Q11
Cp Kcal / Kg oC Kg / m3
6. Heat Loss with Clinker
=
whereHeat Loss with Clinker
Cp Specific Heat of Clinker Clinker outlet TemperatureAmbient Temperature
Cp 0.24 (Table page )285 (Hand Thermocouple)30 (Performance Test)
61.2
Q12
Cp * ( T ck
- T1 )
Q12
Kcal / Kg ck
Kcal / Kg ck
oCT
cli oC
T oC
Tcli
T Q
12 Kcal / Kg
ckQ
12
7.Heat Loss With Cooler Exit Gasi. Cooler Exit Gas
=where
Heat Loss with Cooler Exit GasM Exit Gas Flow rateCp Specific Heat of Exit Gas
Exit Gas outlet TemperatureAmbient Temperature
P Clinker Production
M 35514 (Pitot Measurements)Cp 0.31 (Table page )
244 (Thermometer)
30 (Assumption)P 38178.5 (Performance Test)
61.71
MProcess Flow Sheet 27100Fuel Consumption 28733Performance CurvePitot Measurments 35514
ii. Evaporation of Water= M λ / P
whereHeat Loss With Evap. of Water
M Water Flow rateλ Heat of VaporizationP Clinker Production
M 17500 (Site Flowmeter)λ 539 (Table page )P 38178.5 (Performance Test)
247.06
N.B.Water λ 539 Kcal / Kg
ρ 1000
Q13
M * Cp * ( T2 - T
1 ) / P
Q13
Kcal / Kg ck
m3 / h Kcal / m3 oC
T2
oCT
1 oC
Kg ck
/ h
T2
T1
Q13
Kcal / Kg ck
Q13
m3 / hm3 / hm3 / hm3 / h
Q14
Q14
Kcal / Kg ck
m3 / h Kcal / Kg
water
Kg ck
/ h
Q14
Kcal / Kg ck
Q14
Kg / m3
Cooler Exit Gas Calculation
Process Update
Cooler Fan Flow Rate 22500 M
Kiln Feed 54 67.28 t / h
Heat Consumption 1300 1256.7
Fuel Consumption 3955 5050.7 Kg / h
i. Process Flow Sheet
M = 22500*67.28*1256.7 / 54*1300 = 27099.6077
ii. Fuel Consumption
M = 22500*5050.7 / 3955 = 28733.4387
iii. Performance Curve
M =
iv. Pitot Measurment
M = 35514
m3 / h
Kcal / Kg ck
m3 / h
m3 / h
m3 / h
m3 / h
Cooler Heat BalanceWater Vapour
Exit GasHot Clinker from Kiln
Cooler
Cooling Water Clinker
RadiationHeat Input
i. Heat received with clinker
=Where
Heat received with clinker
Specific Heat of Clinker Clinker Temperature
T Ambient Temperature
0.241130
T 30264
ii. Cooling Water
= M CpWhere
Sensible Heat of WaterM Water Flow rateCp Specific Heat Of Water
Water TemperatureAmbient Temperature
P Clinker Production
As=
Therefore= 0
Q ck
Cp ck
( T ck
- T )
Q ck
Kcal / Kg ck
Cp ck
Kcal / Kg ck
oCT
ckoCoC
Cp ck
T ck
Q ck
Kcal / Kg ck
Qwater
( T2 - T
1 ) / P
Qwater
Kcal / Kg ck
m3 / hKcal / m3 oC
T2
oCT
1oC
Kg ck
/ hr
T2
T1
Qwater
Kcal / Kg ck
Heat Outputi. Heat Loss with Clinker
Q = 61.2
ii. Radiation
Q = 10.49
iii. Exit Gas
Q = 61.71
iv. Water Vapour
Q = 247.06
Kcal / Kg ck
Kcal / Kg ck
Kcal / Kg ck
Kcal / Kg ck
8. Heat Loss due to Radiation & Convection
Kiln Diam. 3.2 Length 56 m Production P 916.3 t / d
Total Surface Area F 562.688 Specific Surface 0.61409
Surface Area 10.048 Ambient Temp. 30
From Surface Radiation From Surface Radiation Outlet Temp Loss Outlet Temp Loss
m Mcal/h m Mcal/h
1 280 4973 49.97 29 275 4805 48.282 281 5007 50.31 30 242 3776 37.943 320 6466 64.97 31 200 2671 26.844 358 8121 81.60 32 201 2695 27.085 325 6671 67.03 33 212 2962 29.766 344 7484 75.20 34 215 3041 30.567 348 7662 76.99 35 208 2863 28.778 339 7264 72.99 36 214 3016 30.309 320 6466 64.97 37 207 2839 28.53
10 331 6922 69.55 38 207 2839 28.5311 316 6306 63.36 39 208 2863 28.7712 321 6507 65.38 40 205 2791 28.0413 313 6190 62.20 41 208 2863 28.7714 343 7440 74.76 42 206 2815 28.2915 337 7172 72.06 43 200 2671 26.8416 336 7132 71.66 44 193 2510 25.2217 332 6962 69.95 45 201 2695 27.0818 312 6150 61.80 46 201 2695 27.0819 312 6150 61.80 47 195 2554 25.6620 322 6546 65.77 48 194 2533 25.4521 321 6507 65.38 49 201 2695 27.0822 305 5875 59.03 50 200 2671 26.8423 286 5190 52.15 51 193 2510 25.2224 303 5809 58.37 52 182 2260 22.7125 297 5577 56.04 53 182 2260 22.7126 306 5918 59.46 54 178 2176 21.8627 284 5108 51.33 55 206 2815 28.2928 292 5396 54.22 56 200 2671 26.84
1798.3 789.321Total 2587.62 Mcal/h
Radiation : Mcal / h * 24 * 1.05 / P = 71.16 Kcal / Kg
Sp.Radiation : Mcal / h *1.05*1000 / F= 4828.61
i. Radiation from kiln
m2 m2/t/d
m2 oC
oC Kcal / m2 / * h oC Kcal / m2 / * h
Q15
Kcal / h * m2
Cooler Diam. 3.18 Length 8.5 m Production P 916.3 t / d
Total Surface Area F 84.8742 Specific Surface 0.093
From Surface Ambient Surface Radiation WindOutlet Area Temp. Temp. Loss Speed
m Mcal / h m / s< 3 m/s
1 9.99 30 319 6030 60.212 9.99 335 7092 70.853 9.99 283 5077 50.724 9.99 279 4938 49.335 9.99 275 4805 48.006 9.99 278 4905 49.007 9.99 205 2791 27.888 9.99 195 2554 25.51
381.509
Radiation : Mcal / h * 24 * 1.05 / P = 10.49
Spec. Radiation : Mcal / h * 1.05 * 1000 / F = 4719.75
ii.Radiation from cooler
m2 m2/t/d
m2 oC oC Kcal / m2 * h
Kcal / Kg ck
Q16
Kcal / h * m2
iii. Radiation from Preheater
Ambient Temp.P 916.3 t / d
DATASurface Surface Radiation Loss
Cyclones Temp. Mcal / hCyc. 1 A cyc 3 6.45 60.76 85 574 34.88
cone 0.7 3.185 18.50 90 641 11.86Cyc. 1 B cyc 3 6.45 60.76 90 641 38.95
cone 0.7 3.185 18.50 92 670 12.40Cyc. 2 cyc 4 4.07 51.12 95 709 36.24
cone 0.7 3.56 26.27 109 925 24.30Cyc. 3 cyc 4 4.07 51.12 95 709 36.24
cone 0.7 4.148 30.61 100 778 23.81Cyc. 4 cyc 4.2 4.27 56.31 115 1003 56.48
cone 0.7 4.33 33.31 118 1051 35.01Calciner cyc 4.44 4.18 58.28 110 925 53.91
cone 1.97 4.64 46.70 115 1003 46.84
Material Pipes Length Diam. ACyc. 1 A 7.08 0.7 15.56 105 850 13.23Cyc. 1 B 6.63 0.7 14.57 105 850 12.39Cyc. 2 10.12 0.7 22.24 110 925 20.58Cyc. 3 to P.C. 9.91 0.7 21.78 135 1338 29.14
to Riser 16.13 0.7 35.45 140 1427 50.59Cyc. 4 11.5 0.7 25.28 140 1427 36.07
Ducts Length Diam. AC1-C2 9.29 2.53 73.80 110 925 68.27C2-C3 9.56 2.53 75.95 100 778 59.09C3-C4 11.07 2.67 92.81 120 1083 100.51Riser 3.97 1.52 24.14 135 1338 32.30
S.Ch d A1 43.36 135 1338 58.01
L A2 8.88 140 1427 12.66966.04 Total 903.74
wD h
D d h L w3.95 1 3.92 1.72 1.58
Radiation : Mcal / h * 24 * 1.05 / P = 24.8544
Spec. Radiation : Mcal / h * 1.05 * 1000 / F = 982.276
30 oCD
cL
c
L o
do
Dc
L c
do
L o Area m2 Kcal / m2 * h
Kcal / Kg ck
Q17
Kcal / h * m2
Heat BalanceResults
Heat Input = Heat Output
Heat Input
Combustion heat of Fuel. 1256.78
Sensible heat of Raw Meal. 20.55
Sensible heat of Fuel. 5.23
Sensible heat of Air. 0.00i. Primary air.
ii. Secondary air.iii. Tertiary air. iv. ByPass Quench air.
Sensible heat of Cooing Water. 0.00i. ByPass Cond. Tower.
ii. Clinker Crusher. iii. Cooler.
Total 1282.56Heat Output
Clinker heat of formation. 418.84
Heat loss with preheater exit gas. 276.34i. Exit gas.ii. Evaporation of water.iii. Dust.iv. CO.
Heat loss with bypass exit gas.
i. Bypass gas. 43.72
ii. Evaporation of water from cond. Tower. 52.24
Heat loss with bypass dust. 0.34
Heat loss with clinker crusher water. 4.53
Heat loss with clinker. 61.20Heat loss with cooler exit gas.
i. Cooler exit gas. 61.71
ii. Evaporation of water. 247.06Heat loss due to radiation & convection.
i. Radiation from kiln. 71.16
ii. Radiation from cooler. 10.49
iii. Radiation from preheater. 24.85Total 1272.49
% Diff. 0.79
Kcal / Kg ck
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E:E\Heat balance\In=Out
