Boiler Thermal Calculation

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A B C D E F G H I J K L M N O P

6 DESIGN

8 N° JOB

10 BOILER TYPE

15

%

17 CAPACITY SH STEAM BOILER lb/h 189598 100

19 CAPACITY SAT. STEAM lb/h 189598 100 lb/h

21 CAPACITY SAT. STEAM lb/h 0 lb/h



27 psia 754.2

29 °F 761.0

TYPE

34 COMBUSTION

36 TYPE FURNACE MEMBRANE WALL

38 TYPE COMBUSTOR

40 MAIN CALCULATIONS 100 % 0 % 0 % 0 %

° F Kw ° F Kw ° F Kw ° F Kw

42 AIR & FLUE GAS CALCULATION

44 COMBUSTION CHAMBER YES

46 WATER WALL CHANNEL

48 SCREEN or EVAPORATOR I° YES

50 SUPERHEATER I° YES

52 SUPERHEATER II° YES

54 SUPERHEATER III°

56 EVAPORATORI° YES

58 EVAPORATOR II°

60 EVAPORATOR III°

62 EVAPORATOR IV°

64 ECONIMIZER I° YES

66 ECONIMIZER II°

68 AIR PREHEATER I°

70 AIR PREHEATER II°

72 kW

74 HEAT POWER RELEASED kW

DESIGN CONDITION

OPERATION PRESSURE

AUX. SAT. STEAM

AUX. SAT. STEAM

AUX. SAT. STEAM

AUX. SAT. STEAM

STEAM GENERATOR

THERMODINANIC CALCULATION

GTA

DATE 11/7/2006FBB

OPERATION TEMPERATURE

RDF

FLUIDIZED BED

FUEL OIL

by STEAM

POST-COMBUSTION

BURNER

0

0

TOTAL

189598

189598

0

0HEAT POWER EXCHANGED 0 0 0

COVER



A1 B C D E F G H I J K L M N

2 CALCULA

3 IMPORTE

4 FUEL KIN RDF INPUT

5 HHV AS FI Btu/lb 9897 HUMIDITY % 0.029

6 HHV ON D Btu/lb 7918 SPC HEAT Btu/lb°F 1.082 10.79

7 LHV ON D Btu/lb 7403 SPC.WEIG lb/cuft stp 0.081

8

9

10

11

12

13

1415 PM

16 ASH 0.000 SITE PRESSURE

17 C 12 0.000 11.53 509.626 psi a 14.68818 H2 2 0.000 8.94 36.654 34.34 140.794

19 O2 32 0.000 4.32 -67.824 V(O2) 8.169 8.923

20 S 32 0.000 4.29 2.660

21 N2 28 0.000 V(N2) 73.456 80.228

22 H2O 18 0.000 1.00 20.000 V(H2O) 8.441 -

23 CO 28

24 CO2 44 V(CO2) 9.882 10.793

25 H2S 34 V(SO2) 0.052 0.057

26 CH4 16 varia min 72.3022 cuft (npt)/lb

27 C2H4 28 varia nec 124.36 cuft (npt)/lb

28 C2H6 30 50.000 vgumido 133.82 100

29 C3H8 44 50.000 v anidro 122.5203 cuft (npt)/lb

30 C4H10 58 n 1.72 %

31 C5H12 72 AIR (n=1)= 7.32 lb/lb

32 NO2 46 0 AIR (n>1)= 12.58 lb/lb

33 Cl2 35 0.000 GAS (n=1)=

34 Char GAS (n>1)=

35 SO2 ARIA= 9.70 kg/kg

36 GAS= 10.77 kg/kg

37

38 TOTAL 0 99.92 56.65 585.26 100.000 100.000

39

40

41 0.72 7.3942

43

44

45

46 FUEL KIN FUEL OIL

47 HHV AS FI Btu/lb HUMIDITY %

48 HHV ON D Btu/lb SPC HEAT Btu/lb°F

49 LHV ON D Btu/lb SPC.WEIG lb/cuft stp

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

70

71

COMBUSTION SHEET CALCULATION

lb/10kB lb/10kB

THEORET

IC QTY. AIR

WATER

FROMFUEL

FUEL

ASH

lb/10kB

WATER THEORETICAL AIR

UID OR SOLIDS FUE GASEOUS, LIQUID OR SOLID FUELSGASEOUS FUELS

ULTIMATE ANALYSIS

lb/lb

OF

CONST.

lb/100 lb

OR

lb/100 cuft

lb/lb

OF

CONST.

lb/100 lb

OR

lb/100 cuft

ULT.

ANAL.%

BY VOL.

DENS. OF

GAS

Lb/100cuft

DENS. OF

CONST.

Lb/100cuft

ULT.

ANAL %

BY WT

FUEL

ASH

lb/10kB

ORSAT %

CO2 max

ORSAT %

CO2 max

AS FIRED

% DRY

GAS VOLUME

FORMULA

AS FIRED

% WET

AIR&FLUE GAS



Prodotti combustione per lb/lb su come br uciato

PM O2 Aria CO2 O2 N2 H2O SO2

44 32 28 18 64

ASH 0.000

C 12.01 0.000 0.000 0.000 0.000 0.000

H2 2.016 0.000 0.000 0.000 0.000 0.000

0.191885 O2 32 0.000 0.000

S 32.06 0.000 0.000 0.000 0.000 0.000

7.982684 N2 28.016 0.000 0.000

1.9062 H2O 18.016 0.000 0.000

CO 28.01 0.000 0.000 0.000 0.000 0.000

0.9664 CO2 44.01 0.000 0.0000 H2S 34.076 0.000 0.000 0.000 0.000 0.000 0.000

CH4 16.041 0.000 0.000 0.000 0.000 0.000 0.000

C2H4 28.051 0.000 0.000 0.000 0.000 0.000 0.000

11.04717 C2H6 30.067 50.000 53.214 229.373 0.000 176.158 0.000

C3H8 44.092 50.000 36.288 156.413 0.000 120.125 0.000

C4H10 58.118 0.000 0.000 0.000 0.000 0.000 0.000

C5H12 72.144 0.000 0.000 0.000 0.000 0.000 0.000

22.09434

nel combustibile

89.502 385.786 0.000 0.000 296.283 0.000 0.000

SO2 come CO2 89.502 385.786 0.000 0.000 296.283 0.000

72 40 60 80 100

CO2 0.000 0.000 0.000 0.000 0.000 0.000

O2 0.000 64.442 35.801 53.701 71.602 89.502

N2 296.283 509.607 414.797 474.053 533.310 592.567

H2O 0.000 0.000 0.000 0.000 0.000 0.000

Totale 296.283 574.049 450.598 527.755 604.912 682.069

72 40 60 80 100

CO2 0.000 0.000 0.000 0.000 0.000 0.000

O2 0.000 11.226 7.945 10.175 11.837 13.122

N2 100.000 88.774 92.055 89.825 88.163 86.878

H2O 0.000 0.000 0.000 0.000 0.000 0.000

Totale 100.000 100.000 100.000 100.000 100.000 100.000

72 40 60 80 100

CO2 0.000 0.000 0.000 0.000 0.000 0.000

O2 0.000 11.226 7.945 10.175 11.837 13.122N2 100.000 88.774 92.055 89.825 88.163 86.878

Totale 100.000 100.000 100.000 100.000 100.000 100.000

72 40 60 80 100

CO2 21.81 0.000 0.000 0.000 0.000 0.000 0.000

O2 15.89 0.000 9.966 7.025 9.022 10.517 11.678

N2 13.91 100.000 90.034 92.975 90.978 89.483 88.322

7.1890726 7.0885111 7.117899 7.0979204 7.0830384 7.0715234

Totale 100.000 100.000 100.000 100.000 100.000 100.000

Prodotti combustione % in peso sul secco

Prodotti combustione % in peso su come br uciato

Prodotti combustione per lb/lb sul secco

Peso lb/lb

Prodotti

Combustio Peso dei Prodotti Combustione al Variare Eccesso d'aria %

Peso lb/lb

Prodotti


Vol.

cuft/cuft

ProdottiDENSREL

Peso dei Prodotti Combustione al Variare Eccesso d'aria %

Analisi

Elementare

% in peso

Necessario in lb Prodotti della Combustione lb/lb

Prodotti combustione % in volume sul secco

Peso lb/lb

Prodotti


O2



A1 B C D E F G H I J K

2 CALCULATION

3 IMPORTED

4 KIND RDF MOIST INPUT

5 COUTRY VM

6 STATE FC

7 B OF M REF ASH

8 GRINDABILITY TOTAL

9 INITIAL DEF. VM+FC

10 SOFTENIG HHV AS FIRED Btu/lb 9897

11 LIQUID HHV ON DRY Btu/lb 7918

12 TYPE OF UNIT LHV ON DRY Btu/lb 7403

13 FIRING SYSTEM FLUIDIZED BE 0.716

14 SOURCE OF DATA15

16 1.082

17

18 NOTA:

19 1. APH "air pre-heater"

20 2. Basato sulla formula di Verhoff/Banchero

21

22 R OPERATION CONDITION % 100

23 D16 FLUE GAS RECIRCULATING % 0

24 STM STEAM FLOW lb/h 189598

25 HEAT RELEASE Btu/h 206525847

26 P STEAM PRESSURE AT SH OUTLET psia 754.2

27 P1 STEAM PRESSURE IN DRUM psia 833.8

28 T4 TEMPERATURE AT SH OUTLET °F 76129 T9 TEMPERATURE SATURADE STEAM °F 523.0

30 T8 TEMPERATURE ECO OUTLET °F 455.0

31 T0 TEMPERATURE FEED WATER °F 320

32 I4 ENTHALPY OF STEAM AT SH OUTLET Btu/lb 1378.7

33 I3 ENTHALPY OF SATURADE STEAM Btu/lb 1198.4

34 I2 ENTHALPY SUPERHEATER WATER Btu/lb 515.6

35 I5 ENTHAPY OF ECO OUTLET Btu/lb 436.0

36 I1 ENTHALPY OF FEED WATER Btu/lb 291.7

37 HEAT ABSORBED BY STEAM Btu/lb 1087.0

38 N EXCCESS AIR LEAVING BOILER % 72

39 BD BLOW DOWN % 1.0

40 ACTUAL DRY AIR lb/10kB 12.58

41 WET GAS FROM FUEL AS FIRED lb/10kB 1.08

42 MOIST. IN AIR lb/10kB 0.1643 AD ADD. MOISTURE IN FUEL lb/10kB

44 WET GAS lb/10kB 13.82

45 WATER FROM FUEL lb/10kB 0.72

46 TOT. WATER IN WET GAS lb/10kB 0.88

47 DRY GAS lb/10kB 12.94

48 WATER IN GAS % BY WEIGHT % 6.36

49 T1 TEMPERATURE GAS INLET AIR HEATER °F

50 T2 TEMPERATURE GAS LEAVING UNIT °F 374.0

51 T3 TEMPERATURE INLET AIR APH °F Toutlet APH 95 68

52 GAS LVG - AIR ENT. °F 306

53 DRY GAS LOSS % % 9.50

54 WATER FROM FUEL AS FIRED LOSS % % 8.49

55 MOIST. IN AIR LOSS % % 0.24

56 L4 UNBURNED COMB. LOSS % % 1.0

57 RADIATION LOSS % % 0.55

58 L6 UNACC. FOR MFRS. MARGIN % % 1

59 TOTAL LOSS % % 20.78

60 EFFICIENCY ON HHV % % 79.22

61 EFFICIENCY ON LHV % % 84.73

62 Q INPUT IN FUEL Btu/h 260709970

63 GT WET GAS WEIGHT lb/h 360177

64 AT TOT. AIR TO BURNING lb/h 335774

65 FUEL lb/h 32928

66 HOTTEL FACTOR

67 V VOLUMN OF C. CHAMBER cuft

68 SF EPRS OF C. CHAMBER sqft

69SG GRATE AREA sqft 0

70 FURNACE SPC. LOAD Btu/cufth

71 EPRS SPC. LOAD Btu/sqfth

72 GRATE SPC. LOAD Btu/sqfth 0

PERFORMANCE SHEET CALCULATION

P

R O X I M A T E

A N A L Y S I S

A S

F I R E

FUEL

ASH lb/10kB

F U E L

H2O AS FIRED

lb/10kB

COMB



73

74

75 OPERATION CONDITION % 100

76 QC GAS HEAT CONVECTION QC Btu/h 6964056.283

77 STEAM FLOW Btu/h 189598

78 WET GAS WEIGHT lb/h 360177

79 WET GAS lb/10kB 13.82

80 WATER IN GAS % BY WEIGHT % 6.36

81 C 1 100

82 R & U 1.55 77.51 lb/10kB

83 H2O 0.72 744

84 AVAIL. HEAT FUEL/10kB

85 TEMP. GAS INLET AIR HEATER °F

86 TEMP. GAS LEAVING °F 37487 HEAT IN COMB. AIR lb/10kB 1099.1

88 HEAT AVAILABLE/10kB 10177.5

89 Qg = HEAT AVAILABLE/lb WET GAS 736.7

90 HEAT AVAILABLE Btu/h 265336703.5

91 HEAT AVAILABLE/EPRS Btu/sqfth

92 EM EMMISSIVITY % 0.75

93

94

95 Tgas = FURNACE EXIT TEMP °F

96 Tad =ADIABATIC COMBUSTION TEMPERATURE °F 2332

97 kW 77743.0

98 kW 60511.5

99 POWER REMAINING IN THE FURNACE kW

100

101

102

103 Qavailable BTU/h 243751836.1

104 MW

105 FLUE GAS HEAT SENSIBLE LOSS

106 OUTLET FLUE GAS ECO TEMPERATURE °F 374.0

107 Tflue gas ECO to Trif °F 338.0

108 FLUE GAS MOISTURE % by wgt 6.4

109 FLUE GAS ENTHALPY BTU/kg 78.0

110 Qpsf flue gas BTU/h 28077756.2

111 kW 8226.7

112 IRRADIATION HEAT LOSS

113 FURNACE SURFACE sqft

114 FURNACE WALL TEMPERATURE °F115 POST COMBUSTION SURFACE CHAMBER sqft

116 POST COMBUS. TEMPERATURE CHAMBER °F

117 EXTERNAL BOILER SURFACE sqft 22596.0

118 EXTENAL BOILER TEMPERATURE °F 131.0

119 Qp irr BTU/h 2333622.2

120 kW

121 ASH UNBURNING LOSS

122 PERCENT OF UNBURNING % 1.0

123 HEAT ASH UNBURNIG BTU/h 584301.4

124 Qp unb kW

125

126 CINDER HEAT SENSIBLE LOSS

127 ASH TEMPERATURE °C 752.0

128 ASH HEAT SPACIFIC SPC. (average) BTU/lb°F 0.24

129 Qsc BTU/h 849824.4

130 kW

131 Qu =Qa-Qp sf-Qp irr-Qp unb-Qp ash BTU/h 211906331.8

132 kW

133

134 EFFICIENCY CALCULATED (witout margin) % 84.7

135 MARGIN % 1.0

136 EFFICIENCY GUARANTY % 87.9

137

138

139 % H2O INTO FLUE GAS (by volumn) H20 8.441

140 % SO2 INTO FLUE GAS (by volumn) SO2 0.052

141 % MASS CONVERSION from SO2 to SO3 % 3.0142 OUTLET FLUE GAS PRESSURE in wc -3.937

143 FLUE GAS PRESSURE (absolute) pfa = pfr + 760 mmHG in Hg 29.579

144 PARCIAL H2O PRESSURE PH20 = H20 * pf in Hg 2.497

145 PARCIAL SO3 PRESSURE PSO3=k*SO2*pf*(PMSO2/PMSO3) 0.000369

146 DEW POINT TEMPERATURE °R 739.6

147

POWER INTO THE STEAM

POWER FUEL RELEASE

H E A

T I N

C O M B . A I R

FURNACE CALCULATION

H E A T

L O S S

922

9078

INDIRECT EFFICIENCY BOILER CALCULATION

CALCOLO DI DEW-POINT(see note 2.)




2 CALCULATION

3 INPUT DATA BUNDLE IMPORTED

4 INPUT

5 R OPERATION CONDITION %

6 STM STEAM CAPACITY lb/h

7 T9 SATURED STEAM TEMPERATURE °F

8 P1 STEAM PRESSURE DRUM psi 0.07677

9 P STEAM PRESSURE psi 5

10 I3 ENTALPHY SATURED STEAM Btu/lb

11 I2 ENTALPHY SUPERHEATER WATER

12 I1 ENTALPHY FEED WATER

13 GT GAS FLOW lb/h

14 TI INLET GAS TEMEPRATURE °F

15 K4 N° OF BUNDLES

16 B0 BUNDLE N°

17 D0

18 D2

19 D1

20 E0 SIDE INTERESTED BY GAS 1. OUTSIDE 2. INSIDE

21 I0 TUBE ARRANGEMENT 1. LINE 2. STAGERED PR 3. STAGERED DS

22 PT TRANSVERSAL PITCH in

23 PL LONGITUDINAL PITCH in

24 A1 GREATER SIDE ft

25 B LOWER SIDE ft

26 HI EFFECTIVE LENGHT TUBE ft

27 DE OUTSIDE TUBE DIAMETER in

28 ESP THICKNESS OF TUBE in

29 NR N° ROW

30 NS N° SECTION

31 NP N° PRINCIPLE

32 SF EFFECTIVE SURFACE sqft

33 RZ INSTALLED A ECO 1.YES 2.NO

34 EZ WATER WALL CHANNEL ACTIVE 1.YES 2.NO

35 L3 MISURA DELLA INTERCAPEDINE

36 HT BANDLE DEEP ft

37 FI INSIDE FOULING sqfth°F/Btu

38 FE OUTSIDE FOULING sqfth°F/Btu

39 TU TEMPERATURE GAS OUTLET ESTIMATED °F

40 PP PINCH POINT IN GAS OUTLET °F41 T8 TEMPERATURE WATER OUTLET ECO °F

42 I5 ENTALPHY WATER OUTLET ECO

43 T0 TEMPERATUR FEED W ATER INLET lb/cuft

44 L11 STRAIGHT LENGHT TUBE ft

45 L33 FRICTION FACTOR sqft/sqin

46 C1 BEND RADIUS ft

47 N1 N° BEND 45°

48 N2 N° BEND 90°

49 N3 N° BEND 180°

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

70

71

72

FINISH EVAPORATOR CALCULATION TEST

GAS FLOW TYPE 1. CROSS 2. PARALLEL

BUNDLE TYPE 1. BANK 2. COIL

FLOW GAS & STEAM 0 . EMPTY 1. EQUI 2. COUNTER

EVA-L1



73 B C D E F G H I J K

74

75 OUTPUT DATA 0 BANDLE

76


78 STM WATER FLOW lb/h

79 GAMA SPC. GAS WEIGHT lb/cuft

80 SG FREE GAS AREA sqft

81 VM GAS VELOCITY ft/s

82 ST FREE STEAM AREA sqft

83 VV STEAM VELOCITY ft/s

84 QV HEAT REALISE Btu/h

85 MGV MASS GAS VELOCITY lb/sqfth

86 MSV MASS STEAM VELOCITY lb/sqfth

87

88 KX FUEL FACTOR K2

89 FS SURFACE RATIO FS sqft

90 UR RADIATION COEFICIENT Btu/sqfth°F

91

92 TGM AVERAGE GAS TEMPERATURE °F

93 TF GAS FILM TEMPERATURE °F

94 CGP GAS HEAT SPECIFIC VALUE Btu/lb°F

95 LAMB GAS CONDUCTIVITY VALUE Btu/fth

96 NY GAS VISCOSITY VALUE lbft/h

97 LB BEAM LENGHT ft

98 FPP PHISICAL VALUE

99 REG REYNOLD GAS SIDE

100 FA GAS FORM FACTOR Fa

101 FD GAS ROW FACTOR Fd

102 UC1 CONVECTION COEFICIENT Btu/sqfth°F

103 UC GAS TRANSMISSION COEFICIENT Btu/sqfth°F

104

105 TSM AVERAGE STEAM TEMPERATURE °F

106 REA REYNOLD SUPERHEATER WATER SIDE

107 GV SPC. WEIGHT SUPERHEATER WATER lb/cuft

108 US STEAM TRANSMISSION COEFICIENT Btu/sqfth°F

109

110 J FACTOR f

111 LMTD LMTD °F

112 SF EFFECTIVE AREA sqft113 U TOTAL HEAT TRANSMISSION COEFICIENT Btu/sqfth°F

114

115 TI TEMPERATURE GAS INLET °F

116 TU TEMPERATURE GAS OUTLET °F

117

118 QG HEAT GAS REALISE Btu/h

119 KW HEAT POWER EXCHANGE Kw

120

121 FD COEF. ROW Fd

122 FB COEF. DISPOSITION Fb

123 PG PRESSURE LOSS GAS SIDE in wc

124

125 L33 FRICTION FACTOR sqft/sqin126 PV PRESSURE LOSS STEAM SIDE psi

127

128

129

130

131

132

133

134

135

136

137

138

139

140

141

142

143

144

SMOOTH EVAPORATOR CALCULATION TEST




2 CALCULATION

3 INPUT DATA I° BUNDLE IMPORTED

4 INPUT


6 STM STEAM FLOW lb/h

7 T9 INLET STEAM TEMPERATURE °F

8 T4 OUTLET STEAM TEMPERATURE °F 0.07677

9 P1 STEAM PRESSURE SH INLET psi

10 P STEAM PRESSURE SH OUTLET psi

11 GT GAS FLOW lb/h


13K4 N° OF BUNDLES

14 B0

15 D0

16 D1

17 D2

18 D3


20 K2 HOTTEL FACTOR




24 B LESSER SIDE ft


26 DE OUTSIDE TUBE DIAMETER in27 ESP THICKNESS OF TUBE in 340

28 NR N° ROW 360

29 NS N° SECTION 2.5

30 NP N° PRINCIPLE 40


32 T59/T5 IN & OUTLET STEAM TEMP. ASSUMED °F

33 TI/TU IN & OUTLET GAS TEMP. ASSUMED °F

34 RZ RADIATION FROM C. CHAMBER YES/NO

35 NRS N° ROW SCREEN

36 EZ WATER WALL CHANNEL ACTIVE YES/NO


38 HT BUNDLE DEEP ft

39 FI INSIDE FOULING sqfth°F/Btu40 FE OUTSIDE FOULING sqfth°F/Btu

41


43 I3 INLET STEAM ENTAPHY Btu/lb

44 T4 / T5 OUTLET STEAM TEMPERATURE °F

45 I4 / I5 OUTLET STEAM ENTALPHY Btu/lb



48 N1 N° BEND 45°

49 N2 N° BEND 90°

50 N3 N° BEND 180°

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

70

71

72

BUNDLES N° 1. I° 2. II°

PRIORITY SH BUNDLES 1. PRIMARY 2. SECONDARY

SUPERHEATER CALCULATION TEST


SH BUNDLES ARG. IN GAS FLOW 1. SERIE 2. PARALLEL


SUPER




74

75 OUTPUT DATA BUNDLE

76


78 GT GAS FLOW lb/h

79 GAMA SPC. GAS WIEGHT lb/cuft





84 QV HEAT IN STEAM Btu/h

85MGV MASS GAS VELOCITY lb/sqfth


87

88 KX FUEL FACTOR K2(B&W)



91







98 FPP PHISICAL VALUE99 REG REYNOLD's GAS SIDE Re





104


106 CVP STEAM HEAT SPECIFIC VALUE Btu/lb°F 0.607 0.585

107 NU STEAM VISCOSITY VALUE lb/fth 22.7 23.2

108 GV STEAM SPC. WEIGHT lb/cuft 0.06272 0.06409


110 RES REYMOLD's STEAM SIDE

111

112 I3 ENTHALPY STEAM INLET Btu/lb

113 I4 / I5 ENTHALPY STEAM OUTLET Btu/lb

114 L0MTD LMTD


116 U TOTAL HEAT TRANSMISSION COEFICIENT Btu/sqfth°F

117

118 J FACTOR f



121 T9 TEMPERTURE STEAM INLET °F

122 T4 / T5 TEMPERATURE STEAM OUTLET °F

123

124 QG HEAT GAS REALISE Btu/h125 KW HEAT POWER EXCHANGE kW

126

127 FD COEF. ROW Fd



130


132 PV PRESSURE LOSS STEAM SIDE psi

133

134 DSH DESUPERHEATER lb/h

135

136

137

138

139

140

141

142

143

144




A1 B C D E

2

3 INPUT DATA

4




8 T4 OUTLET STEAM TEMPERATURE °F

9 P1 STEAM PRESSURE SH INLET psi

10 P STEAM PRESSURE SH OUTLET psi

11 GT GAS FLOW lb/h

12 TI INLET GAS TEMEPRATURE °F13 K4 N° OF BUNDLES

14 B0

15 D0

16 D1

17 D2

18 D3


20 K2 HOTTEL FACTOR




24 B LESSER SIDE ft25 HI EFFECTIVE LENGHT TUBE ft



28 NR N° ROW

29 NS N° SECTION

30 NP N° PRINCIPLE


32 T59/T5 IN & OUTLET STEAM TEMP. ASSUMED °F

33 TI/TU IN & OUTLET GAS TEMP. ASSUMED °F

34 RZ RADIATION FROM C. CHAMBER YES/NO

35 NRS N° ROW SCREEN

36 EZ WATER WALL CHANNEL ACTIVE YES/NO


38 HT BUNDLE DEEP ft



41



44 T4 / T5 OUTLET STEAM TEMPERATURE °F

45 I4 / I5 OUTLET STEAM ENTALPHY Btu/lb



48 N1 N° BEND 45°

49 N2 N° BEND 90°

50 N3 N° BEND 180°

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

70

71

72

BUNDLES N° 1. I° 2. II°






SUPER

L M N O P

CALCULATION

BUNDLE IMPORTED

INPUT



73 B C D E

74

75 OUTPUT DATA

76


78 GT GAS FLOW lb/h

79 GAMA SPC. GAS WIEGHT lb/cuft





84 QV HEAT IN STEAM Btu/h85 MGV MASS GAS VELOCITY lb/sqfth


87

88 KX FUEL FACTOR K2(B&W)



91





96 NY GAS VISCOSITY VALUE lbft/h97 LB BEAM LENGHT ft


99 REG REYNOLD's GAS SIDE Re





104


106 CVP STEAM HEAT SPECIFIC VALUE Btu/lb°F

107 NU STEAM VISCOSITY VALUE lb/fth

108 GV STEAM SPC. WEIGHT lb/cuft109 US STEAM TRANSMISSION COEFICIENT Btu/sqfth°F

110 RES REYMOLD's STEAM SIDE

111

112 I3 ENTHALPY STEAM INLET Btu/lb

113 I4 / I5 ENTHALPY STEAM OUTLET Btu/lb

114 L0MTD LMTD



117

118 J FACTOR f



121 T9 TEMPERTURE STEAM INLET °F

122 T4 / T5 TEMPERATURE STEAM OUTLET °F

123


125 KW HEAT POWER EXCHANGE kW

126

127 FD COEF. ROW Fd



130

131L33 FRICTION FACTOR sqft/sqin


133

134 DSH DESUPERHEATER lb/h

135

136

137

138

139

140

141

142

143

144

SUPERHEATER CALCULA

L N O P

BUNDLE




2 CALCULATION


4 INPUT




8 P1 STEAM PRESSURE DRUM psi 0.07677

9 P STEAM PRESSURE psi 5




13 GT GAS FLOW lb/h14 TI INLET GAS TEMEPRATURE °F


16 B0 BUNDLE N°

17 D0

18 D2

19 D1






25 B LOWER SIDE ft

26 HI EFFECTIVE LENGHT TUBE ft27 DE OUTSIDE TUBE DIAMETER in


29 NR N° ROW

30 NS N° SECTION

31 NP N° PRINCIPLE





36 HT BANDLE DEEP ft



39 TU TEMPERATURE GAS OUTLET ESTIMATED °F40 PP PINCH POINT IN GAS OUTLET °F

41 T8 TEMPERATURE WATER OUTLET ECO °F

42 I5 ENTALPHY WATER OUTLET ECO Btu/lb

43 T0 TEMPERATUR FEED W ATER INLET °F




47 N1 N° BEND 45°

48 N2 N° BEND 90°

49 N3 N° BEND 180°

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

70

71

72





EVA-L




74

75 OUTPUT DATA I° BANDLE

76


78 STM WATER FLOW lb/h 110200

79 GAMA SPC. GAS WEIGHT lb/cuft 0.020

80 SG FREE GAS AREA sqft 149.6

81 VM GAS VELOCITY ft/s 24.9


83 VV STEAM VELOCITY ft/s 0

84 QV HEAT REALISE Btu/h 34919207

85 MGV MASS GAS VELOCITY lb/sqfth 178986 MSV MASS STEAM VELOCITY lb/sqfth

87

88 KX FUEL FACTOR K2 0.381

89 FS SURFACE RATIO FS sqft 0.966

90 UR RADIATION COEFICIENT Btu/sqfth°F 0.74

91

92 TGM AVERAGE GAS TEMPERATURE °F 1432.6

93 TF GAS FILM TEMPERATURE °F 914.5

94 CGP GAS HEAT SPECIFIC VALUE Btu/lb°F 0.267

95 LAMB GAS CONDUCTIVITY VALUE Btu/fth 0.031

96 NY GAS VISCOSITY VALUE lbft/h 0.080

97 LB BEAM LENGHT ft 0.181

98 FPP PHISICAL VALUE 0.12899 REG REYNOLD GAS SIDE 5498

100 FA GAS FORM FACTOR Fa 0.98

101 FD GAS ROW FACTOR Fd 1.00


103 UC GAS TRANSMISSION COEFICIENT Btu/sqfth°F 6.38

104

105 TSM AVERAGE STEAM TEMPERATURE °F 305.9

106 REA REYNOLD SUPERHEATER WATER SIDE 0

107 GV SPC. WEIGHT SUPERHEATER WATER lb/cuft 0.02

108 US STEAM TRANSMISSION COEFICIENT Btu/sqfth°F 1858.6

109

110 J FACTOR f 0.0

111 LMTD LMTD °F 995.6112 SF EFFECTIVE AREA sqft 4943

113 U TOTAL HEAT TRANSMISSION COEFICIENT Btu/sqfth°F 7.1

114

115 TI TEMPERATURE GAS INLET °F 1677.4

116 TU TEMPERATURE GAS OUTLET °F 1187.8

117

118 QG HEAT GAS REALISE Btu/h 34919207

119 KW HEAT POWER EXCHANGE Kw 10231

120

121 FD COEF. ROW Fd 1.00

122 FB COEF. DISPOSITION Fb 0.394

123 PG PRESSURE LOSS GAS SIDE in wc 1.09

124



127

128

129

130

131

132

133

134

135

136

137

138

139

140

141

142

143

144

SMOOTH EVAPORATOR CALCULATION TEST



A1 B C D E

2

3 INPUT DATA

4




8 P1 STEAM PRESSURE DRUM psi

9 P STEAM PRESSURE psi



12 I1 ENTALPHY FEED WATER13 GT GAS FLOW lb/h



16 B0 BUNDLE N°

17 D0

18 D2

19 D1






25 B LOWER SIDE ft




29 NR N° ROW

30 NS N° SECTION

31 NP N° PRINCIPLE




35 L3 MISURA DELLA INTERCAPEDINE36 HT BANDLE DEEP ft




40 PP PINCH POINT IN GAS OUTLET °F



43 T0 TEMPERATUR FEED WATER INLET °F




47 N1 N° BEND 45°48 N2 N° BEND 90°

49 N3 N° BEND 180°

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

70

71

72





EVA-L

L M N O P

II° BUNDLE



73 B C D E

74

75 OUTPUT DATA

76








84 QV HEAT REALISE Btu/h85 MGV MASS GAS VELOCITY lb/sqfth


87




91













104



107 GV SPC. WEIGHT SUPERHEATER WATER lb/cuft108 US STEAM TRANSMISSION COEFICIENT Btu/sqfth°F

109

110 J FACTOR f

111 LMTD LMTD °F

112 SF EFFECTIVE AREA sqft


114



117


119 KW HEAT POWER EXCHANGE Kw120

121 FD COEF. ROW Fd



124



127

128

129

130

131

132

133

134

135

136

137

138

139

140

141

142

143

144

SMOOTH EVAPORATOR CALCULATI

II° BUNDLE

100

110200

0.025

149.6

19.8

0

198952011789

0.381

0.966

0.53

1044.8

725.1

0.260

0.027

0.072

0.181

0.120

5693

0.98

1.00

6.01

305.9

0

0.021858.6

0.0

616.7

4943

6.5

1187.8

901.9

19895201

5829

1.00

0.392

0.86



A1 B C D E

2

3 INPUT DATA

4











16 B0 BUNDLE N°

17 D0

18 D2

19 D1




23PL LONGITUDINAL PITCH in


25 B LOWER SIDE ft




29 NR N° ROW

30 NS N° SECTION

31 NP N° PRINCIPLE














46 C1 BEND RADIUS ft47 N1 N° BEND 45°

48 N2 N° BEND 90°

49 N3 N° BEND 180°

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

6970

71

72





EVA-L

Q R S T U

III° BUNDLE



73 B C D E

74

75 OUTPUT DATA

76










87




91




95LAMB GAS CONDUCTIVITY VALUE Btu/fth









104




109

110 J FACTOR f

111 LMTD LMTD °F



114



117

118 QG HEAT GAS REALISE Btu/h119 KW HEAT POWER EXCHANGE Kw

120

121 FD COEF. ROW Fd



124



127

128

129

130

131

132

133

134

135

136

137

138

139

140

141142

143

144


III° BUNDLE

100

110200

0.030

149.6

16.8

0

119550931789

0.381

0.966

0.43

814.6

612.4

0.256

0.0250.068

0.181

0.115

5829

0.99

1.00

5.77

305.9

0

0.021858.6

0.0

391.3

4943

6.2

901.9

727.3

119550933503

1.00

0.390

0.73



A1 B C D E

2

3 INPUT DATA

4











16 B0 BUNDLE N°

17 D0

18 D2

19 D1




23PL LONGITUDINAL PITCH in


25 B LOWER SIDE ft




29 NR N° ROW

30 NS N° SECTION

31 NP N° PRINCIPLE














46 C1 BEND RADIUS ft47 N1 N° BEND 45°

48 N2 N° BEND 90°

49 N3 N° BEND 180°

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

6970

71

72





EVA-L

V W X Y Z

BUNDLE



73 B C D E

74

75 OUTPUT DATA

76










87




91




95LAMB GAS CONDUCTIVITY VALUE Btu/fth









104




109

110 J FACTOR f

111 LMTD LMTD °F



114



117

118 QG HEAT GAS REALISE Btu/h119 KW HEAT POWER EXCHANGE Kw

120

121 FD COEF. ROW Fd



124



127

128

129

130

131

132

133

134

135

136

137

138

139

140

141142

143

144


BUNDLE




2 CALCULATION

3 INPUT DATA BUNDLE IMPORTED

4 INPUT









13 GT GAS FLOW lb/h



16 B0 BUNDLES N°

17 D0





22 B LOWER SIDE ft




26 NR N° ROW

27 NS N° SECTION

28 NP N° PRINCIPLE


30 HA FIN HEIGHT in

31 EA FIN THICKNESS in

32 NA n°OF FIN BY INCH n°fin/in








40 T0 TEMPERATUR FEED W ATER INLET °F

41 CN CIRCULATION TYPE 1. NATURAL 2. ASSISTED

42 RC CIRCULATION RATE

43 LD STEEL CONDUCTIVITY Btu/fth°F

44 OM EFFICIENCY OF FIN %

45 PH TUBE ARRANGEMENT


47 L3 FRICTION FACTOR see (fg. 26 - STERN) sqft/sqin


49 N1 N° BEND 45°

50 N2 N° BEND 90°

51 N3 N° BEND 180°

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

70

71

72


FINNED EVAPORATOR CALCULATION TEST

EVA-A




74

75 OUTPUT DATA 0 BANDLE

76








84 QV HEAT EVAPORATOR REALISE Btu/h



87

88 KX FUEL FACTOR K2 (B&W)



91













104


106 REA REYNOLD's STEAM SIDE Re

107 GV SPC. WEIGHT SUPERHEATER WATER lb/cuft


109

110 J FACTOR

111 L0MTD LMTD °F



114

115 TI TEMPERATURE GAS INLET °F116 TU TEMPERATURE GAS OUTLET °F

117



120

121 FD COEF. ROW Fd



124



127

128

129

130

131

132

133

134

135

136

137

138

139

140

141

142

143

144

FINNED EVAPORATOR CALCULATION TEST




2 CALCULATION

3 INPUT DATA BANDLE IMPORTED

4 INPUT



7 T9/T0 INLET WATER TEMPERATURE °F

8 T4/T8 OUTLET WATER TEMPERATURE °F



11 GT GAS FLOW lb/h



14B0 N° OF BANDLES

15 D0

16 D1

17 D2


19 K2 HOTTEL FACTOR




23 B LOWER SIDE ft




27 NR N° ROW

28 NS N° SECTION29 NP N° PRINCIPLE


31 T5 OUTLET HOT WATER TEMP. ASSUMED °F

32 TU OUTLET GAS TEMP. ASSUMED °F





37 T4 OUTLET STEAM TEMPERATURE °F

38 I4 OUTLET STEAM ENTALPHY Btu/lb




42 N1 N° BEND 45°43 N2 N° BEND 90°

44 N3 N° BEND 180°

45

46

47

48

49

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

70

71

72

FINISH ECONOMIZER CALCULATION TEST



PRIORITY ECO BUNDLES 1. PRIMARY 2. SECONDARY

ECO-L




74

75 OUTPUT DATA BANDLE

76






82 ST FREE HOT WATER AREA sqft

83 W HOT WATER VELOCITY ft/s

84 QV HEAT NECESSARY RELEASE Btu/h



87


89 TF FILM TEMPERATURE °F









98 UG CONVECTION COEFICIENT Btu/sqfth°F


100


102 REA REYNOLD WATER SIDE

103 GV SPC. WEIGHT HOT WATER lb/cuft

104 US HOT WATER TRANSMISSION COEFICIENT Btu/sqfth°F

105

106 J FACTOR f

107 L0MTD LMTD °F



110



113 T9/T0 TEMPERTURE FEED WATER °F

114 T4/T8/TTEMPERATURE HOT WATER OUTLET °F

115

116 I1 ENTALPHY HOT WATER INLET Btu/lb

117 I4/I5 ENTALPHY HOT WATER OUTLET Btu/lb



120

121 FD COEF. ROW Fd



124



127

128

129

130

131

132

133

134

135

136

137

138

139

140

141

142

143144

SMOOTH ECONOMIZER CALCULATION TEST




2 CALCULATION

3 INPUT DATA BANDLE IMPORTED

4 INPUT



7 T0/T8 INLET WATER TEMPERATURE °F

8 T8 OUTLET WATER ECO TEMPERATURE °F 0.076225

9 P1/PoutSTEAM PRESSURE DRUM psi

10 Pin STEAM PRESSURE ECO INLET psi

11 GT GAS FLOW lb/h



14B0 BUNDLES N°

15 D0

16 D2





21 B LOWER SIDE ft




25 NR N° ROW

26 NS N° SECTION

27 NP N° PRINCIPLE

28 HA FIN HEIGHT in29 EA FIN THICKNESS in

30 NA N° FIN BY INCH fin/in

31 T84/T8 OUTLET WATER TEMP. ASSUMED °F





36 CN

37 RC CIRCULATION RATE

38 LD STEEL CONDUCTIVITY Btu/fth°F

39 OM EFFICIENCY OF FIN %

40 PH TUBE ARRANGEMENT


42 L3 FRICTION FACTOR see (fg. 26 - STERN) sqft/sqin43 C11 BEND RADIUS ft

44 N1 N° BEND 45°

45 N2 N° BEND 90°

46 N3 N° BEND 180°

47

48

49

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

70

71

72

73

FINNED ECONOMIZER CALCULATION TEST

FLOW GAS & STEAM 1 . EQUI 2. COUNTER

CIRCULATION TYPE 1. NATURAL 2. ASSISTED


ECO-A




75

76 OUTPUT DATA BANDLE

77






83 ST FREE HOT WATER AREA sqft

84 WA WATER VELOCITY ft/s

85 QV HEAT ECO RELEASE Btu/h


87 MSV MASS WATER VELOCITY lb/sqfth

88

89 TGM AVERAGE GAS TEMPERATURE







96 REG

97 FA

98 FD



101

102 TSM AVERAGE HOT WATER TEMPERATURE °F103 REA REYNOLD WATER SIDE

104 GV SPC. WATER WEIGHT lb/cuft

105 US WATER TRANSMISSION COEFICIENT Btu/sqfth°F

106

107 J FACTOR f

108 LMTD LMTD °F


110




114 T9/T0 TEMPERTURE FEED WATER °F

115 T4/T8 TEMPERATURE HOT WATER OUTLET °F

116


118 I1 ENTALPHY WATER INLET Btu/lb

119 I5 ENTALPHY HOT WATER OUTLET Btu/lb


121

122 FD COEF. ROW Fd

123 PH


125



128

129

130131

132

133

134

135

136

137

138

139

140

141

142

143

144

145

TUBE ARRANGEMENT Fb

GAS FORM FACTOR Fa

GAS ROW FACTOR Fd

REYNOLD GAS SIDE Re

FINNED ECONOMIZER CALCULATION TEST




2 CALCULATION


4 INPUT


6 EP EFFICIENCY OF AIR HEATER %

7 K4 N° OF BUNDLES

8 B0 BUNDLES N° 0.07677

9 AT AIR LOAD lb/h 5

10 GT FLUE GAS LOAD lb/h 6

11 TI INLET GAS TEMEPRATURE °F 7

12 T3 INLET AIR TEMPERATURE °F 9

13 T2 OUTLET FLUE GAS TEMP. ASSUMED °F 8

14 T4 OUTLET AIR TEMP. ASSUMED °F 10 95

15 DE OUTSIDE TUBE DIAMETER in 14

16 ESP THICKNESS OF TUBE in 14

17 ED DIAGONAL PITCH in 17

18 AL FREE AREA BY FEET sqft/ft 18

19 PL TRASVERSAL PITCH in 17

20 NP N° ROW 19

21 NL N° SECTION 20

22 LZ EFFECTIVE LENGHT TUBE ft 22

23 PAS N° OF AIR CROSSES 24

24 AZ FLOWING TYPE I° II° III° 34

25 RA FACTOR Ra graf. (H-546) 30

26 RG FACTOR Rg graf. (H-546) 31

27 ST STRATIFICATION FOR VALUE OF item 25 33

28 F1 FACTOR F1 graf. (H-546) 37


30 FA AIR SIDE FRICTION FACTOR in wc

31 FG GAS SIDE FRICTION FACTOR in wc

32

33

34

35

36

37

38

39

40

41

42

43

44

45

46

47

48

49

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

70

71

72

AIR PREHEATER CALCULATION

AIR PREHEATER




74

75 OUTPUT DATA

76


78 CAP SPC. HEAT OF AIR Btu/lb°F 13

79 CGP SPC. HEAT OF FLUE GAS Btu/lb°F 13

80 SA SPC. EFFECTIVE SURFACE sqft/ft 15

81 AI INTERNAL TUBE AREA sqft 16

82 NT TOTAL N° OF TUBES 21

83 SEFF EFFECTIVE SURFACE sqft 23

84 AP HEIGHT OF AIR CROSSES ft 25

85 AAR

TOTAL AIR FREE AREA sqft 2686 AGAS TOTAL FLUE GAS AREA sqft 27

87 MAV AIR MASS VELOCITY lb/sqfth 28

88 MGV FLUE GAS MASS VELOCITY lb/sqfth 29

89 TSM AVERAGE AIR TEMPERATURE °F

90 TGM AVERAGE FLUE GAS TEMPERATURE °F

91 R0 FACTOR R0 32

92 C1 T(air)/T(in gas)-T(in air) 35

93 C2 At*.248/(GT*cpg) 36

94 F1 FATTORE F1 graf. (H-546) 37

95 RCOEF COEFICENTE Rcoef 38

96 C3 R*Seff/(At*.248) 40

97 F2 FATTORE F2 graf.(H-545) 41

98 TU OUTLET FLUE GAS TEMPERATURE °F

99 T4 OUTLET AIR TEMPERATURE °F 42

100

101 PAIR AIR PRESSURE LOSS in wc 43

102 PGAS FLUE GAS PRESSURE LOSS in wc 44

103

104

105

106

107

108

109

110

111

112

113

114

115

116

117

118

119

120

121

122

123

124

125

126

127

128

129

130

131

132

133

134

135

136

137

138

139

140

141

142

143

144




A1 B C D E F G

2

3 INPUT DATA

4


6 EP EFFICIENCY OF AIR HEATER %

7 K4 N° OF BUNDLES

8 B0 BUNDLES N° 0.07677

9 AT AIR LOAD lb/h 5

10 GT FLUE GAS LOAD lb/h 6

11 TI INLET GAS TEMEPRATURE °F 7

12 T3 INLET AIR TEMPERATURE °F 9

13 T2 OUTLET FLUE GAS TEMP. ASSUMED °F 8

14T4 OUTLET AIR TEMP. ASSUMED °F 10

15 DE OUTSIDE TUBE DIAMETER in 14

16 ESP THICKNESS OF TUBE in 14

17 ED DIAGONAL PITCH in 17

18 AL FREE AREA BY FEET sqft/ft 18

19 PL TRASVERSAL PITCH in 17

20 NP N° ROW 19

21 NL N° SECTION 20

22 LZ EFFECTIVE LENGHT TUBE ft 22

23 PAS N° OF AIR CROSSES 24

24 AZ FLOWING TYPE I° II° III° 34

25 RA FACTOR Ra graf. (H-546) 30

26 RG FACTOR Rg graf. (H-546) 31

27 ST STRATIFICATION FOR VALUE OF item 25 33

28F1 FACTOR F1 graf. (H-546) 37


30 FA AIR SIDE FRICTION FACTOR in wc

31 FG GAS SIDE FRICTION FACTOR in wc

32

33

34

35

36

37

38

39

40

41

42

43

44

45

46

47

48

49

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

7071

72


AIR PREHEATER

CALCULATION

II° BUNDLE IMPORTED

INPUT



73 B C D E F G

74

75 OUTPUT DATA

76


78 CAP SPC. HEAT OF AIR Btu/lb°F 13

79 CGP SPC. HEAT OF FLUE GAS Btu/lb°F 13

80 SA SPC. EFFECTIVE SURFACE sqft/ft 15

81 AI INTERNAL TUBE AREA sqft 16

82 NT TOTAL N° OF TUBES 21

83 SEFF EFFECTIVE SURFACE sqft 23

84 AP HEIGHT OF AIR CROSSES ft 25

85 AAR TOTAL AIR FREE AREA sqft 26

86 AGAS TOTAL FLUE GAS AREA sqft 27

87 MAV AIR MASS VELOCITY lb/sqfth 28

88 MGV FLUE GAS MASS VELOCITY lb/sqfth 29

89 TSM AVERAGE AIR TEMPERATURE °F


91 R0 FACTOR R0 32

92 C1 T(air)/T(in gas)-T(in air) 35

93 C2 At*.248/(GT*cpg) 36

94 F1 FATTORE F1 graf. (H-546) 37

95 RCOEF COEFICENTE Rcoef 38

96 C3 R*Seff/(At*.248) 40

97 F2 FATTORE F2 graf.(H-545) 41

98 TU OUTLET FLUE GAS TEMPERATURE °F

99 T4 OUTLET AIR TEMPERATURE °F 42

100

101 PAIR AIR PRESSURE LOSS in wc 43

102 PGAS FLUE GAS PRESSURE LOSS in wc 44

103

104

105

106

107

108

109

110

111

112

113

114

115

116

117

118

119

120

121

122

123

124

125

126

127

128129

130

131

132

133

134

135

136

137

138

139

140

141

142143

144


L M N O P




2 CALCULATION

3 INPUT DATA CHANNEL IMPORTED

4 INPUT

5 B0 N° OF CHANNELS TO ANALYSIS


7 QZ1 FLUE GAS TYPE INCOMMING


9 P1 PRESSURE DRUM psig

10 P1 OPERATION PRESSURE psig

11 T5 OPERATION TEMPERATURE °F


13 T0 FEED WATER TEMPERATURE °F

14 T3 AMBIENT TEMPERATURE °F

15 I4 ENTHALPY OUTLET OF BOILER Btu/lb

16 I2 ENTHALPY SUPERHEATER WATER Btu/lb

17 I5 ENTHALPY OUTLET ECONOMISER Btu/lb

18 I1 ENTHALPY FEED W ATER (Btu/lb) Btu/lb

19 GT FLOW FLUE GAS CAPACITY (lb/h) lb/h

20 UMI HUMIDITY FLUE GAS %

21 GAMA SPC. WEIGHT FLUE GAS lb/cuft

22 VP1 PARCIAL PRESSURE OF CO2 %

23 VP2 PARCIAL PRESSURE OF H2O %


25 T1 INLET TEMPERATURE OF FLUE GAS °F

26 FI INSIDE FOULING FACTOR sqfth°F/Btu

27 FE OUTSIDE FOULING FACTOR sqfth°F/Btu28 LZ WIDHT OF ROOF ft

29 LP DEEP OF ROOF ft

30 HT HOTTEL FACTOR %

31 LZ WIDHT OF CHANNEL ft

32 LP DEEP OF CHANNEL ft

33 AL HEIGHT OF CHANNEL ft


35 DE TUBE DIAMETR OF WALLS in


37 PT PITCH OF TUBE in

38

39

40

41

42

43

44

45

46

47

48

49

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

70

71

72

CHANNEL AND CAVITY CALCULATION

CHANNEL




74

75 OUTPUT DATA CHANNEL

76


78 Q HEAT RELEASE Btu/h

79 T2 OUTLET CHANNEL TEMPERATURE °F

80 TP TUBE WALL TEMPERATURE °F

81 L0MTD LMTD °F

82

83 LZ WIDHT SIZE OF CHANNEL ft

84 LP DEEP SIZE OF CHANNEL ft

85 AL HEIGHT SIZE OF CHANNEL ft

86 HT HOTTEL FACTOR

87 V VOLUMN OF CHANNEL cuft

88 SF EPRS PROJCTED CHANNEL AREA sqft

89 ST TOTAL TUBE INSIDE AREA sqft

90


92 MGV FLUE GAS MASS VELOCITY lb/sqfth

93 GM SPC. FLUE GAS WEIGHT lb/cuft

94 DI HYDRAULIC DIAMETER ft

95 VL FLUE GAS VELOCITY ft/s

96

97 LB BEAM LEIGHT ft

98 UR RADIANT HEAT COEFICIENT Btu/sqfth°F

99

100 UMI HUMIDITY %

101 CGP SPC. HEAT OF FLUE GAS Btu/lb°F

102 NY VISCOSITY COEFICIENT lbft/h

103 LAMB CONDUCTIVITY COEFICIENT Btu/fth

104 FPP PHISICAL FACTOR


106 UL LONGITUDINAL HEAT COEFICIENT Btu/sqfth°F

107 UE SUM UL+UR Btu/sqfth°F

108

109 UI MOISTURE HEAT COEFICIENT Btu/sqfth°F

110 NYW VISCOSITY OF MOISTURE lbft/h

111 GAMA SPC. WEIGHT OF MOISTURE

112 WA MOISTURE VELOCITY ft/s113

114

115 TSM AVERAGE MOISTURE TEMPERATURE °F

116 UA MOISTURE HEAT COEFICIENT Btu/sqfth°F

117

118

119 U TOTAL HEAT COEFICIENT Btu/sqfth°F

120 T1 INLET CHANNEL TEMPERATURE °F

121 TU OUTLET CHANNEL TEMPERATURE °F

122

123 F3 SPC. HEAT BY EPRS Btu/sqft

124 F2 SPC. HEAT BY VOLUMN Btu/sqft

125

126

127

128

129

130

131

132

133

134

135

136

137

138

139

140

141

142

143

144




A1 B C D E

2

3 INPUT DATA

4








12 T9 SATURED STEAM TEMPERATURE °F13 T0 FEED WATER TEMPERATURE °F





18 I1 ENTHALPY FEED WATER (Btu/lb) Btu/lb





23 VP2 PARCIAL PRESSURE OF H2O %24 I4 ENTHALPY OUTLET OF BOILER Btu/lb



27 FE OUTSIDE FOULING FACTOR sqfth°F/Btu

28 LZ WIDHT OF ROOF ft










38

39

40

41

42

43

44

45

46

47

48

49

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

70

71

72


CHANNELCHANNEL



73 B C D E

74

75 OUTPUT DATA

76





81 L0MTD LMTD °F

82




86 HT HOTTEL FACTOR




90





95VL FLUE GAS VELOCITY ft/s

96



99

100 UMI HUMIDITY %








108




112 WA MOISTURE VELOCITY ft/s

113

114



117

118




122



125

126

127

128

129

130

131

132

133

134

135

136

137

138

139

140

141

142

143

144

CHANNEL AND CAVITY C CHANNEL



A1 B C D E

2

3 INPUT DATA

4
































38

39

40

41

42

43

44

45

46

47

48

49

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

70

71

72


CHANNELCHANNEL



73 B C D E

74

75 OUTPUT DATA

76





81 L0MTD LMTD °F

82




86 HT HOTTEL FACTOR




90






96



99

100 UMI HUMIDITY %








108





113

114



117

118




122



125

126

127

128

129

130

131

132

133

134

135

136

137

138

139

140

141

142

143

144




A1 B C D E

2

3 INPUT DATA

4
































38

39

40

41

42

43

44

45

46

47

48

49

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

68

69

70

71

72


CHANNELCHANNEL



73 B C D E

74

75 OUTPUT DATA

76





81 L0MTD LMTD °F

82




86 HT HOTTEL FACTOR




90






96



99

100 UMI HUMIDITY %








108





113

114



117

118




122



125

126

127

128

129

130

131

132

133

134

135

136

137

138

139

140

141

142

143

144




COVER PAGE DATI DI INPUT

n° POS VAR DESCRIZIONE UNITY MAIN COMBUSTION POST-COMBUSTION

GENERAL

E6 DESIGN

E8 n° JOB

E10 BOILER TYPE

K10 DATE 8/7/2006

DESIGN CONDITION

F17 CAPACITY SH STEAM BOILER lb/h 189598

F27 OPERATION PRESSURE ( ABSOLUTE) psia 754.2

F29 OPERATION TEMPERATURE ( AT RELATIVE PRESSURE ) °F 761

K19 AUX. SAT. STEAM lb/h

G19 CARICO OPERATIVO PARZIALE % 100

G21 CARICO OPERATIVO PARZIALE %G23 CARICO OPERATIVO PARZIALE %

G25 CARICO OPERATIVO PARZIALE %

TYPE

I34 TYPE OF FUEL RDF FUEL OIL

I36 TYPE OF FURNAE MEMBRANE WALL

I38 TYPE OF COMBUSTION EQUIPMENT FLUIDIZED BED BURNER

MAIN COMPONENTS

I42 AIR & FLUE GAS CALCULATION YES / NO

I44 COMBUSTION YES / NO YES

I46 WATER WALL CHAMBER YES / NO

I48 SCREEN OR EVAPORATOR I° YES / NO YES

I50 SUPERHEATER I° YES / NO YES

I52 SUPERHEATER II° YES / NO YES

I54 SUPERHEATER III° YES / NO

I56 EVAPORATOR I° YES / NO YES

I58 EVAPORATOR II° YES / NO

I60 EVAPORATOR III° YES / NO

I62 EVAPORATOR IV° YES / NOI64 ECONOMISER I° YES / NO YES

I66 ECONOMISER II° YES / NO

I68 AIR PREHEATER FLUE GAS TYPE I° YES / NO

I69 AIR PREHEATER FLUE GAS TYPE II° YES / NO

(Psh1 I° II° III° IV°

(Psh1 (ammesso) psig 79.55

(Psh2 (ammesso) psig

(Psh3 (ammesso) psig

(Peva (ammesso) psig

(Peco1 (ammesso) psig

(Peco2 (ammesso) psig

BIO-05

FBB



AIR & FLUE GAS DATI DI INPUT

n° POS VAR DESCRIZIONE UNITY MAIN CONBUSTION POST COMBUSTION

E4 COMB FUEL TYPE RDF FUEL OIL

F5HHV

ON DRY HIGHER HEATING VALUE HHV Btu/lb 9897 10325 kcal/kg PCI

% BY VOLUMN (as fired)

D16 ASH %

D17 C CARBON %

D18 H2 HYGROGEN %

D19 O2 OXIGEN %

D20 S SULFUR %

D21 N2 NITROGEN %

D22 H2O WATER %

D23 CO CARBON MONOXID %

D24 CO2 CARBON DIOXID %

D25 H2S HYDROGRN SILFIDE %

D26 CH4 METHANE %

D27 C2H4 ETHILENE %

D28 C2H6 ETHANE %

D29 C3H8 PROPENE %

D30 C4H10 n-BUTANE %

D31 C5H12 n-PENTANE %

0 0

% BY WEIGHT (as fired)

G16 ASH + ASFALTENE % 14.3

G17 C CARBON % 44.2

G18 H2 HYGROGEN % 4.1

G19 O2 OXIGEN % 15.7

G20 S SULFUR % 0.62

G21 N2 NITROGEN % 0.4

G22 H2O WATER % 20

G33 Cl CLORO % 0.6

G32 NO2 NITRGEN DIOXID %

G34 CHAR CHAR %G35 CO CARBON MONOXID %

G36 CO2 CARBON DIOXID %

G37 SO2 SULFUR DIOXID %

99.92 0

N ECESS AIR % 72

SITE PRESSURE psia 14.688

ecess air raccomanded

range use

FUEL OIL 10 a 20% 15%

NATURAL GAS 10 a 15% 10%

BIOMASS 25 a 60% 30% grate

50% furnace

CDR 50 à 75% 70% fluidized bed



COMBUSTION DATI DI INPUT FOR COMBUSTION

n° POS VAR DESCRIZIONE UNITY I° II° III° IV°

H23 R OPERATION CONDITION %

H24 STM STEAM FLOW lb/h

H25 Q1 HEAT REALISE Btu/h

H26 P STEAM PRESSURE AT SH OUTLET psig

H27 P1 STEAM PRESSURE IN DRUM psig

H28 T4 TEMPERATURE AT SH OUTLET °F

H29 T9 TEMPERATURE SATURADE STEAM °F

H30 T8 TEMPERATURE ECO OUTLET ASSUMED °F 374

H31 T0 TEMPERATURE FEED WATER °F 320

H32 I4 ENTHALPY OF STEAM AT SH OUTLET Btu/lb

H33 I3 ENTHALPY OF SATURADE STEAM Btu/lb

H34 I2 ENTHALPY SUPERHEATER WATER Btu/lb

H35 I5 ENTHAPY OF ECO OUTLET Btu/lb

H36 I1 ENTHALPY OF FEED WATER Btu/lb

H38 N EXCCESS AIR LEAVING BOILER % 72

H39 BD BLOWN DOWN % 1

H43 AD ADD. MOISTURE IN FUEL lb/10kB

H49 T1 TEMPERATURE GAS INLET AIR HEATER °F

H50 T2 TEMPERATURE GAS LEAVING UNIT °F 374

H51 T3 TEMPERATURE AIR °F 68

H56 L4 UNBURNED COMB. LOSS % % 1

H58 L6 UNACC. FOR MFRS. MARGIN % % 1

H66 HOTTEL FACTOR

H67 V VOLUMN OF C. CHAMBER cuft

H68 SF EPRS OF C. CHAMBER sqft

H69 SG GRATE AREA sqft

EFICIENCY OF EXCHANGER % 1

G51 Tah TEMPERATURE OUTLET AIR PRE-HEATER °F 95

DATI DI INPUT FOR FBB

H113 FURNACE SURFACE sqft

H114 FURNACE WALL TEMEPRATURE °F

H115 POST-COMBUSTION CHAMBER SURFACE sqft

H116 POST-COMB. CHAMBER WALL TEMEPRATURE °F

H117 EXTERNALBOILER SURFACE sqft 22596

H118 EXTERNAL BOILER TEMPERATURE °F 131

H127 ASH TEMPERATURE °F 752

H128 ASH HEAT SPECIFIC BTU/lb°F 0.24

H135 EFFICIENCY MARGIN % 1

DATI DI INPUT FOR DEW-POINT

H141 MASS CONVERSIONFROM SO2 to SO3 % 3

H142 BOILER OUTLET FLUE GAS PRESSURE in wc -3.937

FLUE GAS RECIRCULATED

E16 % FLUE GAS RECIRCULATED % 0

% PRIMARY & SECONDARY AIR MIXING % 100

% FLUE GAS RECIRCULATED MIXING % 100



A B C D E F G H I° J K

EVAPORATOR FINISH-L1 DATI DI INPUT I° BUNDLE



H6 STM STEAM CAPACITY lb/h

H7 T9 SATURED STEAM TEMPERATURE °F

H8 P1 STEAM PRESSURE DRUM psi

H9 P STEAM PRESSURE psi

H10 I3 ENTALPHY SATURED STEAM Btu/lb

H11 I2 ENTALPHY SUPERHEATER WATER

H12 I1 ENTALPHY FEED WATERH13 GT GAS FLOW lb/h

H14 TI INLET GAS TEMEPRATURE °F

H15 K4 N° OF BUNDLES

H16 B0 N° OF BUNDLES

H17 D0 BUNDLE TYPE 1. BANK 2. COIL

H18 D2

H19 D1 GAS FLOW TYPE 1. CROSS 2. PARALLEL

H20 E0 SIDE INTERESTED BY GAS 1. OUTSIDE 2. INSIDE

H21 I0 TUBE ARRANGEMENT 1. LINE 2. STAGERED PR 3. STAGERED DS

H22 PT TRANSVERSAL PITCH in

H23 PL LONGITUDINAL PITCH in

H24 A1 GREATER SIDE ftH25 B LESSER SIDE ft

H26 HI EFFECTIVE LENGHT TUBE ft

H27 DE OUTSIDE TUBE DIAMETER in

H28 ESP THICKNESS OF TUBE in

H29 NR N° ROW

H30 NS N° SECTION

H31 NP N° PRINCIPLE

H32 SF EFFECTIVE SURFACE sqft

H33 RZ INSTALLED A ECO 1.YES 2.NO

H34 EZ WATER WALL CHANNEL ACTIVE 1.YES 2.NO

H35 L3 MISURA DELLA INTERCAPEDINE ft

H36 HT BUNDLE DEEP ftH37 FI INSIDE FOULING sqfth°F/Btu

H38 FE OUTSIDE FOULING sqfth°F/Btu

H39 TU TEMPERATURE GAS OUTLET ASSUMED °F

H40 PP PINCH POINT IN GAS OUTLET °F

H41 T8 TEMPERATURE WATER OUTLET ECO °F

H42 I5 ENTALPHY WATER OUTLET ECO

H43 T0 TEMPERATUR FEED WATER INLET lb/cuft

H44 L11 STRAIGHT LENGHT TUB ft

H45 L33 FRICTION FACTOR sqft/sqin

H46 C1 BEND RADIUS ft

H47 N1 N° BEND 45°

H48 N2 N° BEND 90°

H49 N3 N° BEND 180°

H50 EFICIENCY OF EXCHARGER decimal

H51 SMOOTH

H52 (Peva EVA PRESSURE LOSS psi

FI 0.00005 sqfth°F/Btu

FE

NAT GAS 0.002 sqfth°F/Btu

LIGHT OIL 0.004 sqfth°F/Btu

HEAVY OIL 0.01 sqfth°F/Btu


FOULING FACTOR:

SURFACE TUBE TYPE



A B C D E F G H I° J K L

SUPERHEATER DATI DI INPUT I° BUNDLE




H7 T9 INLET STEAM TEMPERATURE °F

H8 T4 OUTLET STEAM TEMPERATURE °F

H9 P1 STEAM PRESSURE SH INLET psi

H10 P STEAM PRESSURE SH OUTLET psi

H11 GT GAS FLOW lb/h



H14 B0

H15 D0

H16 D1

H17 D2

H18 D3


H20 K2 HOTTEL FACTOR



H23 A1 GREATER SIDE ft

H24 B LOWER SIDE ft




H28 NR N° ROW

H29 NS N° SECTION


H31 SF EFFECTIVE SURFACE TOTALE sqft

H32 T5 OUTLET STEAM TEMP. ASSUMED °F

H33 TU OUTLET GAS TEMP. ASSUMED °F

H34 RZ RADIATION FROM C. CHAMBER YES/NO

H35 NRS N° ROW SCREEN

H36 EZ WATER WALL CHANNEL ACTIVE YES/NO

H37 L3 MISURA DELLA INTERCAPEDINE

H38 HT BANDLE DEEP ft

H39 FI INSIDE FOULING sqfth°F/Btu


%

H42 T9 INLET STEAM TEMPERATURE °F

H43 I3 INLET STEAM ENTAPHY Btu/lb

H44 T4 / T5 OUTLET STEAM TEMPERATURE °F

H45 I4 / I5 OUTLET STEAM ENTALPHY Btu/lb

H46 L11 STRAIGHT LENGHT TUBE ft

H47 C11 BEND RADIUS ftH48 N1 N° BEND 45°

H49 N2 N° BEND 90°

H50 N3 N° BEND 180°

H51 (Psh psi

FINISH

CALCOLO % AREA DI PASSAGGIO FUMI

EFICIENCY OF EXCHANGER

SH PRESSURE LOSS

SURFACE TUBE TYPE


BUNDLES N°






NOTA IMPORTANTE: inserire i dati dei "BANDLES" seguendo il flusso dei fumi

NOTA RIGA:

16 IF D3=2 "parallel bundle" introdurre in L18 la % in cui è diviso l'area di passaggio dei fumi attraverso il SH I° & SH II°

23 Considerare l'altezza totale dei banchi surriscaldatore fino al refrattario FI

28 Indicare il numero di raw di ogno banco FE

29Indicare il numero di section di ogno banco NAT G

LIGHT

31 Considerare l'area totale del SH HEAVY



A B C D E F G H I J K L M

EVAPORATOR FINISH DATI DI INPUT I° BUNDLE









H12 I1 ENTALPHY FEED WATER




H16 B0 N° OF BUNDLES


H18 D2


H20 E0 SIDE INTERESTED BY GAS 1. OUTSIDE 2. INSIDE




H24 A1 GREATER SIDE ftH25 B LESSER SIDE ft




H29 NR N° ROW

H30 NS N° SECTION



H33 RZ INSTALLED A ECO 1.YES 2.NO

H34 EZ WATER WALL CHANNEL ACTIVE 1.YES 2.NO

H35 L3 MISURA DELLA INTERCAPEDINE ft

H36 HT BUNDLE DEEP ftH37 FI INSIDE FOULING sqfth°F/Btu




H41 T8 TEMPERATURE WATER OUTLET ECO °F

H42 I5 ENTALPHY WATER OUTLET ECO

H43 T0 TEMPERATUR FEED WATER INLET lb/cuft


H45 L33 FRICTION FACTOR sqft/sqin


H47 N1 N° BEND 45°

H48 N2 N° BEND 90°H49 N3 N° BEND 180°

H50 EFICIENCY OF EXCHANGER decimal

H51 FINISH

H52 (TIZE psi

1 1 1 2 2

1 1 1 2 3

1 2 2 1 1

1 1 2 1 1A B C D E


B0= il numero dal bundle che si sta calcolando

U=45° fattore di riduzione del coef. U trasmissione

SURFACE TUBE TYPE

SH PRESSURE LOSS

con relazione all'asse del tubo = 0,75



T U V W X Y Z

BUNDLE IV° BUNDLE

III° IV° I° II° III° IV°



A B C D E F G H I° J K L M

EVAPORATOR FINNED DATI DI INPUT









H12 I1 ENTALPHY FEED WATER




H16 B0 BUNDLES N°






H22 B LOWER SIDE ft




H26 NR N° ROW

H27 NS N° SECTION



H30 HA FIN HEIGHT in

H31 EA FIN THICKNESS in

H32 NA n°OF FIN BY INCH n°fin/in

H33 RZ




H37 PINCH POINT IN GAS OUTLET °F

H41 CN

H42 RC CIRCULATION RATE

H43 LD STEEL CONDUCTIVITY Btu/fth°F

H44 OM EFFICIENCY OF FIN %

H45 PH TUBE ARRANGEMENT


H47 L3 FRICTION FACTOR see (fg. 26 - STERN) sqft/sqin


H49 N1 N° BEND 45°

H50 N2 N° BEND 90°

H51 N3 N° BEND 180°

H52 decimalH53 FINNED

H54 (Peva psi


FE

NAT GAS 0.002 sqfth°F/Btu

LIGHT OIL 0.004 sqfth°F/Btu


PH IN LINE 4

PH IN STAGER 3

INSTALLED A ECO 1.YES 2.NO


FOULING FACTOR:

EFFICIENCY OF EXCHANGER

SURFACE TUBE TYPE

EVA PRESSURE LOSS




ECONOMIZER FINISH DATI DI INPUT

n° POS VAR UNITY I° II° III° IV°


H6 STM WATER FLOW lb/h

H7 T9/T0 INLET WATER TEMPERATURE °F

H8 T4/T8 OUTLET WATER TEMPERATURE °F




H12 TI INLET GAS TEMEPRATURE °FH13 K4 N° OF BUNDLES

H14 B0 N° OF BANDLES

H15 D0


H17 D2


H19 K2 K2 (from B&W book)




H23 B LOWER SIDE ft

H24 HI EFFECTIVE LENGHT TUBE ftH25 DE OUTSIDE TUBE DIAMETER in


H27 NR N° ROW

H28 NS N° SECTION



H31 T5 OUTLET HOT WATER TEMP. ASSUMED °F





H40 L33 COEF. ATTRITO INTERNH41 C11 BEND RADIUS ft

H42 N1 N° BEND 45°

H43 N2 N° BEND 90°

H44 N3 N° BEND 180°

H45 decimal

H46 FINISH

H47 (Peco psi


FE

NAT GAS 0.002 sqfth°F/BtuLIGHT OIL 0.004 sqfth°F/Btu


DESCRIZIONE



FOULING FACTOR:


SURFACE TUBE TYPE

ECO PRESSURE LOSS




ECONOMIZER FINNED DATI DI INPUT I° BUNDLE

n° POS VAR UNITY I° III° IV°


H6 STM WATER FLOW lb/h

H7 T9/T0 INLET WATER TEMPERATURE °F

H8 T4 OUTLET WATER TEMPERATURE °F

H9 P1 STEAM PRESSURE IN DRUM psi

H10 Pineco STEAM PRESSURE ECO INLET psi




H14 B0 BUNDLES N°

H15 D0

H16 D2

H17 I0 TUBE ARRANGEMENT 1. LINE 2. STAGERED PR3. STAGERED DS




H21 B LOWER SIDE ft




H25 NR N° ROW

H26 NS N° SECTION


H28 HA FIN HEIGHT in

H29 EA FIN THICKNESS in

H30 NA N° FIN BY INCH fin/in

H31 T5 OUTLET WATER TEMP. ASSUMED °F





H36 CN

H37 RC CIRCULATION RATE

H38 LD STEEL CONDUCTIVITY Btu/fth°F

H39 OM EFFICIENCY OF FIN %

H40 PH TUBE ARRANGEMENT see (i.e. - STERN)

H41 L11 STRAIGHT LENGHT TUBE ft

H42 L33 FRICTION FACTOR see (fg. 26 - STERN) sqft/sqin


H44 N1 N° BEND 45°

H45 N2 N° BEND 90°

H46 N3 N° BEND 180°

H47 EFICIENCY OF EXCHARGER decimal

H48 FINNED

H49 (Peco ECO PRESSURE LOSS psi


DESCRIZIONE

FLOW GAS & STEAM 1. EQUI 2. COUNTER


SURFACE TUBE TYPE



A B C D E F G H I° J K

AIR PREHEATER DATI DI INPUT I° BUNDLE



H6 EP EFFICIENCY OF AIR HEATER %


H8 B0 BUNDLES N°


H10 T3 INLET AIR TEMPERATURE °F

H11 T2 OUTLET FLUE GAS TEMP. ASSUMED °F

H14 T4 OUTLET AIR TEMP. ASSUMED °F



H17 ED DIAGONAL PITCH in

H18 AL FREE AREA BY FEET sqft/ft

H19 PL TRASVERSAL PITCH in

H20 NP N° ROW

H21 NL N° SECTION

H22 LZ EFFECTIVE LENGHT TUBE ft

H23 PAS N° OF AIR CROSSES

H24 AZ FLOWING TYPE I° II° III°

H25 RA FACTOR Ra graf. (H-541-2)

H26 RG FACTOR Rg graf. (H-541-2)H27 ST STRATIFICATION FOR VALUE OF graf. (H-541-2) item 25

H28 F1 FACTOR graf. (H-546)

H29 F2 FACTOR graf. (H-545)

H30 FA AIR SIDE FRICTION FACTOR graf. (H-542) in wc

H31 FG GAS SIDE FRICTION FACTOR graf. (H-545) in wc

DESCRIZIONE



CHANNELS & CAVITY DATI DI INPUT


H5 B0 N° OF CHANNELS TO ANALYSIS


H7 QZ1 FLUE GAS TYPE INCOMMING


H9 P1 PRESSURE DRUM psig

H10 P1 OPERATION PRESSURE psig

H11 T5 OPERATION TEMPERATURE °FH12 T9 SATURED STEAM TEMPERATURE °F

H13 T0 FEED WATER TEMPERATURE °F

H14 T3 AMBIENT TEMPERATURE °F

H15 I4 ENTHALPY OUTLET OF BOILER Btu/lb

H16 I2 ENTHALPY SUPERHEATER WATER Btu/lb

H17 I5 ENTHALPY OUTLET ECONOMISER Btu/lb

H18 I1 ENTHALPY FEED WATER (Btu/lb) Btu/lb

H19 GT FLOW FLUE GAS CAPACITY (lb/h) lb/h

H20 UMI HUMIDITY FLUE GAS %

H21 GAMA SPC. WEIGHT FLUE GAS lb/cuft

H22 VP1 PARCIAL PRESSURE OF CO2 %H23 VP2 PARCIAL PRESSURE OF H2O %

H24 I4 ENTHALPY OUTLET OF BOILER Btu/lb

H25 T1 INLET TEMPERATURE OF FLUE GAS °F

H26 FI INSIDE FOULING FACTOR sqfth°F/Btu

H27 FE OUTSIDE FOULING FACTOR sqfth°F/Btu

H28 LZ WIDHT OF ROOF ft

H29 LP DEEP OF ROOF ft

H30 HT HOTTEL FACTOR %

H31 LZ WIDHT OF CHANNEL ft

H32 LP DEEP OF CHANNEL ft

H33 AL HEIGHT OF CHANNEL ftH34 HT HOTTEL FACTOR %

H35 DE TUBE DIAMETR OF WALLS in


H37 PT PITCH OF TUBE in

DESCRIZIONE



CHANNELS & CAVITY

OUTPUT DATA


H78 Q HEAT RELEASE Btu/h

H79 T2 OUTLET CHANNEL TEMPERATURE °F

H80 TP TUBE WALL TEMPERATURE °F

H81 L0MTD LMTD °F

H83 LZ WIDHT SIZE OF CHANNEL ft

H84 LP DEEP SIZE OF CHANNEL ft

H85 AL HEIGHT SIZE OF CHANNEL ft

H86 HT HOTTEL FACTOR

H87 V VOLUMN OF CHANNEL cuft

H88 SF EPRS PROJCTED CHANNEL AREA sqft

H89 ST TOTAL TUBE INSIDE AREA sqft

H91 TGM AVERAGE FLUE GAS TEMPERATURE °F

H92 MGV FLUE GAS MASS VELOCITY lb/sqfth

H93 GM SPC. FLUE GAS WEIGHT lb/cuft

H94 DI HYDRAULIC DIAMETER ft

H95 VL FLUE GAS VELOCITY ft/s

H97 LB BEAM LEIGHT ft

H98 UR RADIANT HEAT COEFICIENT Btu/sqfth°F

H100 UMI HUMIDITY %

H101 CGP SPC. HEAT OF FLUE GAS Btu/lb°F

H102 NY VISCOSITY COEFICIENT lbft/h

H103 LAMB CONDUCTIVITY COEFICIENT Btu/fth

H104 FPP PHISICAL FACTOR

H105 TF FILM TEMPERATURE °F

H106 UL LONGITUDINAL HEAT COEFICIENT Btu/sqfth°F

H107 UE SUM UL+UR Btu/sqfth°F

H109 UI MOISTURE HEAT COEFICIENT Btu/sqfth°F

H110 NYW VISCOSITY OF MOISTURE lbft/h

H111 GAMA SPC. WEIGHT OF MOISTURE

H112 WA MOISTURE VELOCITY ft/s

H114 TSM AVERAGE MOISTURE TEMPERATURE °F

H115 UAMOISTURE HEAT COEFICIENT Btu/sqfth°F

H117 U TOTAL HEAT COEFICIENT Btu/sqfth°F

H118 T1 INLET CHANNEL TEMPERATURE °F

H119 TU OUTLET CHANNEL TEMPERATURE °F

H121 F3 SPC. HEAT BY EPRS Btu/sqft

H122 F2 SPC. HEAT BY VOLUMN Btu/sqft



CALCOLO DELLA SEZIONE LATO VAPORE CALCOLO DELLA SEZIONE LATO FUMI

portata vapore lb/h 217800 portata fumi lb/h 352330

peso specifico cuft/lb 1.12 peso specifico cuft/lb 0.078

velocita vapore ft/s 65 temp. fumi in °F 919

diametro tubi in 2.375 temp. fumi out °F 750

spessore in 0.157 velocita fumi ft/s 32

velocita di massa lb/sqfth 262080 velocita di massa lb/sqfth 7333.188248

area tubo sqft 0.023167705 correzione in temp. cuft/h 5534893.504

area necessaria sqft 0.831043956 area necessaria sqft 48.04595056

n° principii - 35.87079395 sezione libera aletta sqft 0.153

lunghezza libera ft 314.0258206

n° sezioni previste 18

lunghezza tubi ft 16.52767477



CALCOLO DELLA SUPERFICIE DEL BANCO EVAPORATORE STOP cancellare

TUTTE LE MISURE IN METRI 1 2 3 4

1 numero di tubi sulla sezione 1 1 1 1

2 numero di sezione 1

3 distanza tra centri c.cilindrici 3.2 3.2 3.2 3.2

interasse tubi 0.1

A1 distanza tra l'asse c. cilindrico sup 1 0.9 0.8 0.7

e l'ultimo tubo del fascio

B distanza tra gli assi c. cilindrici 0.1

A2 distanza tra l'asse c. cilindrico inf 1.1 1 0.9 0.8

e l'ultimo tubo del fascio

rt raggio dic curvatura dei tubi 0.22 0.22 0.22 0.22passo angolare c. superiore 10

E angolo a partire asse orrizontale 30 40 50 60

c. cilindrico superiore

60 50 40 30

passo angolare c. inferiore 8

E angolo a partire asse orrizontale 20 28 36 44

c. cilindrico inferiore

70 62 54 46

Ris raggio interno c. cilindrico superiore 0.5 0.5 0.5 0.5

Rii raggio interno c. cilindrico inferiore 0.4 0.4 0.4 0.4

NOTA: a 0.11002 0.078601 0.05148 0.02948 0 0

b 0.88998 0.821399 0.74852 0.67052 0 0

1. Per un nuovo calcolo, cancellare il calcolo 1 0.527691 0.572322 0.664609 0.841278 0 0le colonne in "verde" c 0.513891 0.689331 0.892206 1.161649 0 0

g 0.704428 0.857873 1.033631 1.271659 0 0

2. Per il calcolo trascinare verso destra con

il Mouse la colonna "D" tra le righe "4 a 26" d 0.14478 0.116737 0.090704 0.067188 0 0

e 0.95522 0.883263 0.809296 0.732812 0 0

2 0.616536 0.600383 0.60039 0.618803 0 0

f 0.347708 0.469694 0.588064 0.707775 0 0

h 0.55445 0.663953 0.76606 0.866042 0 0

3 1.941122 1.678174 1.400309 1.062299 0 0

4+5 0.499164 0.430049 0.360934 0.291819 0 0

tot 3.584513 3.280927 3.026242 2.814199 0 0

Lunghezza Totale = 12.7059 m 41.686 ft

Superficie Totale = 91.4651 m2 984.164 sqft



0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0



BANDLE I° II° III° LE

NS 52 54 NS

NR (totali) 12 12 NR

NR(B) 2 2 NR

DE

DE in 2 2 A

A ft 8.2 8.2 r

r ft 0.164 0.164 B

B ft 10 10 PT

PT in 2.51 PL

PL in 3.94 LA

AL

SF(totale) sqft 2684.815 2787.86 PR

L tubo ft 107.6674 107.6674

CALCOLO DEL CANALE DOVE E' ALLOGIATO L' SH

LA ft 205.2133 NO

AL ft 128.3433

PR ft 10.414

BX = "11" & "12"

Pout

FUMI

SH 1 SH 2

Pin1=Pout + (sh2 + (sh1= Pcc Pin2=Pout + (sh2

Psh1m=Pout + (sh2 + (sh1/2 Psh2m=Pout + (sh2/2

BX = "21" & "22"

Pout

FUMI

SH 2 SH 1

Pin2=Pout + (sh2 Pin1=Pout + (sh2 + (sh1= Pcc

Psh2m=Pout + (sh2/2 Psh1m=Pout + (sh2 + (sh1/2

(sh2

Psh2m

CALCOLO DELLA SUPERFICIE DEL SURRISCALDATORE

Pout1=Pin2

Psh2m

(sh1

Psh1m

(sh2

Pout1=Pin2

DEFINIZIONE DEL CALCOLO DELLA CADUTA DI PRESSIONE NEL SURRISCALDATORE

Psh1m

(sh1



Pout + (Psh1 + (Psh2

Pout + (Psh1/2

Pout + (Psh1 + (Psh2/2

Pout + (Psh1 + (Psh2

Pout + (Psh2/2

Pout + (Psh2 +(Psh1/2



VOLUMI PARZIALI, ARIA & GAS DA 1 KG DI COMBUSTIBILE

SUL SECCO TAL QUALE

PM ELEMENTO ANALISI

12 C 45.6 31.92 31.92

2 H2 6.4 4.48 4.48

32 S 0 0 0

32 O2 46 32.2 32.2

28 N2 0 0 018 H2O 0 30 30

CZ 2 1.4 1.4

n= 1 1.3 1.3

Varia min= 2.9586667 m3N/kg 47.41792 cuft/lb npt

Varia=n x Varia min Varia= 3.8462667 m3N/kg 61.64329 cuft/lb npt

Vgas secco=

Vgas umido= 4.69588 m3N/kg 75.25986 cuft/lb npt

Vanidro= 3.8207867 m3N/kg 74.38477 cuft/lb npt

V(CO2)= 0.1268857 % 0.126886 %

V()H2O)= 0.1863534 % 0.186353 %

V(S2)= 0 % 0 %

V(O2)= 0.0396935 % 0.039694 %

V(N2)= 0.6470674 % 0.647067 %

1 1

sul SECCO

UM = (8,936*H2/(11,48*n+1+0,2272*n*H2))

UM = 0.0457723 %

cpm =

T7 = 1053 cpm = 0.2939412 kcal/kg°C

sul TAL QUALE

UM = (8,936*H2/(11,48*n+1+0,2272*n*H2))

UM = 0.0251193 %

cpm = ((972,7+10,76*UM)+((332,62-6,5*UM)*T7/1000)-((83,93-7,33*UM)*(T7/1000)^2))/418

T7 = 1053 cpm = 0.2938818 kcal/kg°C

UMIDITA & CALORE SPACIFICO FUMI



CALCOLO DEL FATTORE Fb CALCOLO PERDITA DI CARICO LATO FU

IN LINE

Re sl/d

st/d 1.5 2.0 2.5 3.0 1.5 2.0 2.5 3.0 1.5 2.0 2.5

asse X

2000 0.32 0.154 0.095 0.079 0.42 0.228 0.158 0.137 0.528 0.334 0.254

8000 0.32 0.16 0.115 0.097 0.4 0.228 0.162 0.141 0.528 0.334 0.24

14000 0.32 0.162 0.12 0.1 0.385 0.223 0.162 0.14 0.52 0.32 0.226

20000 0.32 0.163 0.12 0.1 0.38 0.22 0.161 0.14 0.484 0.294 0.218

IN STAGERED

Re sl/d

st/d 1.5 2.0 2.5 3.0 1.5 2.0 2.5 3.0 1.5 2.0 2.5

asse X

2000 0.6 0.5 0.48 0.46 0.62 0.48 0.4 0.375 0.64 0.442 0.362

8000 0.492 0.394 0.36 0.355 0.505 0.38 0.339 0.32 0.52 0.37 0.318

14000 0.425 0.34 0.313 0.3 0.46 0.358 0.3 0.282 0.49 0.338 0.284

20000 0.383 0.32 0.296 0.28 0.44 0.32 0.278 0.26 0.48 0.32 0.263

1.5 2.0 3.0

asse Y asse Y asse Y

1.5 2.0 3.0

asse Y asse Y asse Y



INFORMAZIONI PER UTILIZZARE IL PROGRAMMA STEAM CALCULATOR

LEGGENDA: X DATO DI INPUT X FUNZIONI NON CARICATE

O DATO DI OUTPUT O FUNZIONI NON CARICATE

pressione temperatura decimale entalpia volume spc. calore spc. viscosità conduttività

psia ° F Btu/lb cuft/lb Btu/lf°F lb/fth Btu/hft°F

P T Q H V C M K

P T x o

T P o x

P QV x x o

P QH x x o

P QS x x

P QC x x o

P QW x x

P QG x x

P QM x x o

P QK x x o

T QV x x o

T QH x x o

T QS x x

T QC x x o

T QW x x

T QG x x

T QM x x o

T QK x x o

P TV x x o

P TH x x o

P TS x x

P TC x x o

P TW x x

P TG x x

P TM x x o

P TK x x o

P HT x o x

P HV x x oP HS x x

P HQ x o x

P HC x x o

P HW x x

P HG x x



0.00043 J / kg Btu / lb 2325.6

3.9682 kcal Btu 0.252

3087.46 kcal ft * lb 0.00032389

4186.85 kcal J 0.0002389

POR X P/ OBTER

P/ OBTER X POR

0.0011627 kcal kW * h 860.01

427 kcal kg * m 0.002343

0.0015593 kcal HP * h 641.3

0.1123 kcal / m3 Btu / cu ft 8.899

0.0011628 kcal / h kW 860

0.6719 kcal / m * h * °C Btu / ft * h * °F 1.4882

0.3687 kcal / m2 * h Btu / sq ft * h 2.712

0.2049 kcal / m2 * h * °C Btu / sq ft * h * °F 4.88

0.08064 kcal / m2 * h * °C / cm Btu / sq ft * h * °F / in 12.4

0.6719 kcal / m2 * h * °C / m Btu / sq ft * h * °F / ft 1.4882

1.8 kcal / kg Btu / lb 0.5556

1 kcal / kg °C Btu / lb * °F 1

3.9682 kcal / kW Btu / kW * h 0.252

2.2046 kg lb 0.45359

0.0092972 kg * m Btu 107.559

7.23 kg * m lb * ft 0.1383



SCREEN DATI DI INPUT I° BUNDLE


H5 R %

H6 GT lb/h

H7 TI °F


H9 A0 TYPE OF FUEL 1.WOOD 2.BAGASSE 3.FUEL OIL 4.COAL 5.NAT.GAS

H10 K2 HOTTEL FACTOR

H11 PT TRANSVERSAL PITCH inH12 PL LONGITUDINAL PITCH in


H14 B LESSER SIDE ft



H17 ESP THICKNESS in

H18 NRS N° ROW

H19 NS N° SECTION

H20 TU °F

H21 decimal

H22 FINISHH23 (Psceen psi

OPERATION CONDITION

FLOW GAS

INLET GAS TEMEPRATURE

OUTLET GAS TEMP. ASSUMED


SURFACE TUBE TYPESCEEN PRESSURE LOSS




2 CALCULATION

3 INPUT DATA IMPORTED

4 INPUT


6 GT FLOW GAS lb/h



9 A0 TYPE OF FUEL 1.WOOD 2.BAGASSE 3.FUEL OIL 4.COAL 5.GAS

10 K2 HOTTEL FACTOR




14 B LESSER SIDE ft



17 ESP THICKNESS in

18 NRS N° ROW

19 NS N° SECTION


21

22

23

24

25

26

27

28

29

30

31

32

33

34

35

36

37

38

39

40

41

42

43

44

45

46

47

48

49

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

6768

69

70

71

72

SCREEN CALCULATION TEST

SCREEN




74

75 OUTPUT DATA

76


78



81 SCR FREE GAS AREA sqft


83 K1


85

86 (T RIFERIMENTO °F87 TI TEMPERATURE GAS INLET °F


89

90 CGP HEAT SPC. GAS Btu/lb/°F



93


95

96

97

98

99

100

101

102

103

104

105

106

107

108

109

110

111

112

113114

115

116

117

118

119

120

121

122

123

124

125

126

127

128

129

130

131

132

133

134

135

136

137

138

139

140

141

142

143

144

SCREEN CALCULATION TEST

FACTOR ST/DE



123456 35

DATI VENDITE

6 7 8 9 10 11 12 13 14 15 16 1

I0 2 2 2 2 2 2 2 2 2 2 2

NR 5 6 7 8 9 10 11 12 13 14 15 1

FD 1.06 1.05 1.04 1.02 1.01 1.00 1.02 1.09 1.25 1.53 1.99 2.6

SL/D 2 2 2 2 2 2 2 2 2 2 2

ST/D 1.5 1.5 1.5 1.5 2 2 2 2 2.5 2.5 2.5 2

REG 2000 8000 14000 20000 2000 8000 14000 20000 2000 8000 14000 2000

FB 0.6200 0.5050 0.4600 0.4400 0.4788 0.3608 0.2792 0.2000 0.4000 0.3390 0.2990 0.279

0.6200 0.5050 0.4600 0.4400 0.4788 0.3608 0.2792 0.2000 0.4000 0.3390 0.2990 0.279

arrotonda 0.6000 0.5000 0.5000 0.4000 0.5000 0.4000 0.3000 0.2000 0.4000 0.3000 0.3000 0.300

arr diff 0 0 0 0 0 0 0 0 0 0 0

arr ecc 2 1 1 1 1 1 1 1 1 1 1

arr 0.6200 0.5000 0.4000 0.4000 0.4000 0.3000 0.2000 0.1000 0.4000 0.3000 0.2000 0.200

0.7000 0.6000 0.5000 0.5000 0.5000 0.4000 0.3000 0.2000 0.5000 0.4000 0.3000 0.300

LMTD = ((TI - TD) - (TU - TE)) / (2.303 * Log((TI - TD) / (TU - TE)))

L0MTD = LMTD / 1.8

ti 753 t9 221

tu 289 t51 350

LMTD= 188.2627

P = Sheets(14).Cells(8, 8).Value

Psh1m = P + Sheets(1).Cells(50, 22).Value

Psh2m = P + Sheets(1).Cells(50, 21).Value + Sheets(1).Cells(52, 22).Value

Psh3m = P + Sheets(1).Cells(50, 21).Value + Sheets(1).Cells(52, 21).Value + Sheets(1).Cells(54, 22).Value

T9 = 519.5: T4 = 797: TSM1 = (T9 + T54) / 2: TSM2 = (T59 + T4) / 2: TEM1 = (T0 + T84) / 2: TEM2 = (T89 + T8) / 2

Rem"1"

P = Sheets(14).Cells(8, 8).Value

T4 = Sheets(14).Cells(10, 8).Value

Rem"sh out"

H41 = MyStmPTH(P, T4)

V41 = MyStmPTV(P, T4)

C41 = MyStmPTC(P, T4)

M41 = MyStmPTM(P, T4)

K41 = MyStmPTK(P, T4)



Rem"sh1 middle"

H41m = MyStmPTH(Psh1m, TSM1)

V41m = MyStmPTV(Psh1m, TSM1)

C41m = MyStmPTC(Psh1m, TSM1)M41m = MyStmPTM(Psh1m, TSM1)

K41m = MyStmPTK(Psh1m, TSM1)

Rem"sh2 middle"H42m = MyStmPTH(Psh2m, TSM2)

V42m = MyStmPTV(Psh2m, TSM2)

C42m = MyStmPTC(Psh2m, TSM2)M42m = MyStmPTM(Psh2m, TSM2)

K42m = MyStmPTK(Psh2m, TSM2)

Rem"sh in"P1 = Sheets(1).Cells(70, 21).Valu

T9 = MyStmPT(P1)

H31 = MyStmPQH(P1, 1)

V31 = MyStmPQV(P1, 1)

C31 = MyStmPQC(P1, 1)

M31 = MyStmPQM(P1, 1)K31 = MyStmPQK(P1, 1)

Rem"2"

P1 = Sheets(1).Cells(70, 21).Valu

T9 = MyStmPT(P1)

Q = 1

H31 = MyStmPQH(P1, 1)V31 = MyStmPQV(P1, 1)

C31 = MyStmPQC(P1, 1)

M31 = MyStmPQM(P1, 1)

K31 = MyStmPQK(P1, 1)

Rem"3"

P1 = Sheets(1).Cells(70, 21).ValuT2 = T9

Q = 0

H21 = MyStmPQH(P1, 0)

V21 = MyStmPQV(P1, 0)C21 = MyStmPQC(P1, 0)

M21 = MyStmPQM(P1, 0)

K21 = MyStmPQK(P1, 0)

Rem"eco out"

Pouteco = Sheets(1).Cells(72, 21).Value

T8 = T9 - 68H5 = MyStmPTH(Pout, T8)

V5 = MyStmPTV(Pout, T8)

C5 = MyStmPTC(Pout, T8)

M5 = MyStmPTM(Pout, T8)

K5 = MyStmPTK(Pout, T8)

Rem"eco1 middle"H81m = MyStmPTH(Peco1m, TEM1)

V81m = MyStmPTV(Peco1m, TEM1)

C81m = MyStmPTC(Peco1m, TEM1)

M81m = MyStmPTM(Peco1m, TEM1)

K81m = MyStmPTK(Peco1m, TEM1)

Rem"eco2 middle"H82m = MyStmPTH(Peco2m, TEM2)

V82m = MyStmPTV(Peco2m, TEM2)

C82m = MyStmPTC(Peco2m, TEM2)

M82m = MyStmPTM(Peco2m, TEM2)K42m = MyStmPTK(Peco2m, TEM2)

Rem"eco in"Pineco = Sheets(1).Cells(70, 19).Value

T0 = 266

H0 = MyStmPTH(Pin, T0)

V0 = MyStmPTV(Pin, T0)C0 = MyStmPTC(Pin, T0)

Boiler Thermal Calculation

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