Heat transfer surface of the economizer

$A_s\left[{\text{m}}^2\right]$

$\frac{Q_{Eco}}{U\ast F_c\ast \Delta T_{lm}}$

23.46

22.98

0.48

Total length of tubes of the economizer

$L\left[\text{m}\right]$

$\frac{A_s}{\pi \ast d}$

149.377

149.377

0

Heat of evaporator

$Q_{Eva}\left[\text{kW}\right]$

${\dot{m}}_{st}\ast h_{fg}$

8716.2764

8644.76

71.5164

Heat transfer surface of evaporator

$A_s\left[{\text{m}}^{\text{2}}\right]$

$\frac{N_{Tu}\ast C_{\min }}{h}$

33.281

30.678

2.603

Total length of evaporator

$L\left[\text{m}\right]$

$\frac{A_s}{\pi \ast d}$

211.87

211.87

0

Rate of steam

${\dot{m}}_{st}\left[\text{kg}/\text{s}\right]$

$\frac{{\dot{m}}_{FG}{C}_{pFG}\left(T_{FG1}-T_{FG2}\right)}{h_{fg}}$

0.7701

0.6302

0.1399

Heat rate of super

$Q_{SH}\left[\text{kW}\right]$

$\epsilon \ast C_{\min }\ast \left(T{F}_{G1}-T_S{}_{t2}\right)$

1179.4

1169.98

9.42

Transfer surface of superheater

142.04

139.86

2.18

Mass of dry cherry

${\dot{m}}_S\left[\text{kg}/\text{h}\right]$

${\dot{m}}_{Che}\left(100\%-X\%\right)$

1350

1290.87

59.13

Moisture in the wet cherry

$X_1\left[\%\right]$

$\frac{IM}{100-IM}$

2.3333

1.98

0.3533

Moisture in the dry cherry

$X_2\left[\%\right]$

$\frac{FM}{100\%FM}$

0.1111

0.08956

0.02154

Water evaporated

$m\left[\text{kg}\right]$

${\dot{m}}_S\left(X_1-X_2\right)$

3000

2909.89

90.11

Inlet gas thermal energy

$H_{G2}\left[\text{kJ}/\text{kg}\right]$

$C_S\left(T_{G2}-T_0\right)+Y_2{H}_L$

176.982

170.68

6.302

Rate of mass of gas

${\dot{m}}_G\left[\text{kg}/\text{h}\right]$

${\dot{m}}_G\left(Y_1-Y_2\right)={\dot{m}}_P\left(X_1-X_2\right)$

98,684.21

98,590.58

93.63

Heat transfer units in section-III

$N_{TU,III}$

$\frac{T_{G2}-T_{GB}}{\Delta T_{m,III}}$

0.022

0.002

0.020

heat transfer units in section-II

$N_{TU,II}$

$\frac{T_{GB}-T_{GA}}{\Delta T_{m,II}}$

0.2636

0.2333

0.0303

Total transfer units

$N_{TU}$

$N_{TU,I}+N_{TU,II}+N_{TU,III}$

1.84

1.09

0.75

Diameter of the dryer

$D\left[\text{m}\right]$

${\left(\frac{4\ast S}{\pi }\right)}^{0.5}$

1.54

1.54

0

Length of dryer

$L\left[\text{m}\right]$

$N_{TU}\ast L_{TU}$

9.46

9.46

0

Revolution per min

RPM

peripheral speed / diameter

4.44

4.44

0

Flue gas loss

$L_{FG}\left[\%\right]$

$L\left(c_{o2}+s_{o2}\right)+L_{H2O}+L\left(O_2+N_2\right)$

10.297

10.099

0.198

Other losses

$W_{Oth}\left[\%\right]$

By subtraction

26.9338

25.09778

1.83602

Total heat absorbed in boiler

$W_{in}\left[\text{kJ}/\text{kg}\right]$

$h_1-h_4$

3286.301

3198.898

87.403

Work of feed pump

$W_{FP}\left[\text{kJ}/\text{kg}\right]$

$V_3\left(P_5-P_3\right)$

0.9999

0.9999

0

Work of turbine

$W_{TU}\left[\text{kJ}/\text{kg}\right]$

$h_1-h_2$

1116.7421

1116.7421

0

Net work

$W_{net}\left[\text{kJ}/\text{kg}\right]$

$W_{TU}-W_{PU}$

1115.742

1110.987

4.7551

Net power output

$P_{Out}\left[\text{Mw}\right]$

$m_{ste}\ast w_{net}$

11.2

10.97

0.23

Overall CHP plant efficiency

${\eta }_{Overall}\left[\%\right]$

$\frac{W_{net}+Q_{pro}}{Q_{in}}$

84.15

83.957

0.193