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8/3/2019 Waste Heat Boiler Evaluation for Gas Fired Heater Furnace
1/35
Estimate Area & Heat Recovery for Flue Gas Heat Recovery for MED BFW Preheat
air Q=1.08CFM(dT) btuh 1 Estimate only based on simplistic HVAC Air Water-
water Q=500gpm(dT) btuh 2 Detailed to used actual Cp & Den's
Water lbs/hr=500gpm 3
fuel Q=(dH)SCFH(eff) btuh 4
flue gas (SCF /SCF )=(1+%XA/200)(15.8SG+1.8) FlueGz/ Fuel 5 Calc_F1
any SCFH/60=SCFM 6
Q=U(A)LMTD(F) BTUH 7
Input
Xair 10.0 % Excess Air from Furnace Design Sheet, Study to verify_basis: Furnace Design Sheet
Fuel Qual FlueGz SCF/SCF Fuel MW/29 General Statement for Gas Specific Gravity
0.73 14.0 Flue/Fuel Fuel SG amount of Flue Gas per Quantity of Fuel Used
Fuel/Furn 3.5 mmscfd Fuel Flow to Furnace from PI 5 year Trend, Design to perform sensitivity analysis see Fuel Analysis sheet
Fuel 1050.0 BTU/SCF Fuel Heat Content used in calculation to determine Fuel Gas Saving
dT water 175 F Water Temperature Increase inside Waste Heat Recovery Section *
H2O/Furn 70.0 gpm BFW Averaged Water Flow per Furnace-assume G80F10 servesG82 F7 & G80F11 serve G82F8_see G26E310A-C
T FlueGas in 490 F Flue Gas Temperature Average from PI Data Chart see FlueGas T summry
TH2O in 110 F Water Temperature from Boiler Feed Water prior to Heat Recovery
Uo 25 BTUH/SF/F Overall Heat Transfer Factor, assume finned tubes
OUTPUT Qwater=Qfluegas Calculation'
Flue Gas 2,041,768.8 SCFH Amount of Flue Gas, based on Fuel Flow from PI Fuel Flow & XA% & FuelSG Correlation
Fuel 145,833.3 scfh Convert PI Fuel Flow to SCFH from MMSCFD
Q water 6,186,250.0 BTUH Calc Water Heat duty Required by Eq#2
Flue Gas 34,029.5 SCFM Convert Flue Gas from SCFH to SCFM
dT FlueGas 154.1 F Flue Gas dT by eqn 1 & Heat Duty of Eq2
T FlueGas out 335.9 F Flue Gas T out by PI Flue Gas T & dT above
TH2O out 285.0 F Water T out by Assumed Inlet Water T & dTwater
LMTD 215.3 F LMTD by Text, (d1-d2)/ln(d1/d2)
Ax 1,352.1 Feet squared Recovery Exchanger Area by Eq.7 at F=0.85
8/3/2019 Waste Heat Boiler Evaluation for Gas Fired Heater Furnace
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Fuel Saved 7,364.6 SCFH
Fuel Cost 3.5 $/mSCF Calc_F1
Annual $ $206,208.3 $/year Fuel Saving in $/year
NPV $ at 7 $1,443,458.33 $
Pump HP 2.9 HP at 40 psi dP additional dP over what is used already
Pump elect 18,407.8 KWHR/YR to feed boilers
$/KWHR 0.035 e Cost unit
$ elec/yr 644.3 $ electri/yr use BFW Pump to Feed Heat Recovery
Job Scope
Add WHR unit to Stack on both Furnace, G80F10&11
Use Single 4" feed & Return Pipe, insulate Return to G82F10&11
Add Control Valve at G82 BFW Pumps and BL Isolation Valves
Relocate Stack TI to top of WHR HX
Use FBE Pipe as inplant Runs since T does not exceed FBE Limits.
Used Finned Tubes in Coiled Arrangement approx 32ft L x 5ftOD-400SF extended area
8/3/2019 Waste Heat Boiler Evaluation for Gas Fired Heater Furnace
3/35
Boiler feed water average 70 gpm/boiler G26E310A-C sheet Calc_F1
Summary Apr.28/09 T, F, five yr look back Fuel gpm BFW pH gpm T, F
MEAN Range L R Hi mmscfd water Steam Inlet W
stack F1 G26AH 490 385 580 3.5 70 25 110
stack F2G26AH 515 440 625 3.5 70 25 110
stack F211G57AH 450 365 545 3.5 70 25 110
stack F212AM 486 310 255 380
oil F212 OinAM 48 195 155 235
oil F212 OoutAM 265 255 380
Based on Heat Recovered and Fuel Heat Value at 83% Boiler Effiency, study to confirm Boiler Effiency Orsat
Fuel Ax The Fuel & Ax are input at each dT
dT H2O m$/yr Ft2 dT H2O Fuel at 3yr CapX guess Fuel at 5yr
75 88 403 75 265 177 88 442 177 265
100 118 582 100 353 319 35 589 319 270
125 147 792 125 442 522 -80 737 522 214
150 177 1045 150 530 813 -282 884 813 71
175 206 1352 175 619 1228 -609 1032 1228 -197
dT H2O PV CRF=3 PV CRF=5
75 88 265
100 35 270
125 -80 214
150 -282 71
175 -609 -197
Calc_F1
-700
-600
-500
-400
-300
-200
-100
0100
200
300
400
50 75 100 125 150 175 200
PV CRF=3
PV CRF=5
8/3/2019 Waste Heat Boiler Evaluation for Gas Fired Heater Furnace
4/35
Estimate Area & Heat Recovery for Flue Gas Heat Recovery for MED BFW Preheat '- Detailed to used actual Cp & Den's
air Q=1.08CFM(dT) btuh 1
H2O Q=500gpm(dT) btuh 2
H2O lbs/hr=500gpm 3
fuel Q=(dH)SCFH(eff) btuh 4
fluegas (SCF /SCF )=(1+%XA/2 Flue/ Fuel 5 '(SCF /SCF )=(1+%XA/200)(15.8SG+1.8)any SCFH/60=SCFM 6
Q=U(A)LMTD(F) BTUH 7
Input
Xair 10.0 % Excess Air from Furnace Design Sheet, Study to verify
Fuel Qual FlueGz SCF/SCFFuel MW/29 General Statement for Gas Specific Gravity
0.73 14.0 Flue/Fuel Fuel SG amount of Flue Gas per Quantity of Fuel Used
Fuel/Furn 3.5 mmscfd Fuel Flow to Furnace from PI 5 year Trend, Design to perform sensitivity analysis
Fuel 1050.0 BTU/SCF Fuel Heat Content used in calculation to determine Fuel Gas Saving
dTH2O 254 F Water Temperature Increase inside Waste Heat Recovery Section *
H2O/Furn 11.0 gpm BFW Averaged Water Flow per Furnace-assume G80F10 servesG82 F7 & G80F11 serve G82F8T Flue in 490 F Flue Gas Temperature Average from PI Data Chart
TH2O in 110 F Water Temperature from Boiler Feed Water prior to Heat Recovery
Uo 25 BTUH/SF/F Overall Heat Transfer Factor, assume finned tubes
OUTPUT Qwater=Qfluegas Calc.' Amount of Flue Gas, based on Fuel Flow from PI Fuel Flow & XA% & FuelSG Correlation
Flue Gas 2,041,768.8 SCFH
Fuel 145,833.3 scfh Convert PI Fuel Flow to SCFH from MMSCFD
Q water 1,410,970.0 BTUH Calc Water Heat duty Required by Eq#2
Flue Gas 34,029.5 SCFM Convert Flue Gas from SCFH to SCFM
dT.FlueGz 35.1 F Flue Gas dT by eqn 1 & Heat Duty of Eq2
T Flue out 336.1 F Flue Gas T out by PI Flue Gas T & dT aboveTH2O out 364.0 F Water T out by Assumed Inlet Water T & dTwater
LMTD 63.6 F LMTD by Text, (d1-d2)/ln(d1/d2)
Ax 1,043.8 Feet2
Recovery Exchanger Area by Eq.7 at F=0.85
Fuel Saved 7,356.5 SCFH
Fuel Cost 3.5 $/mSCF
Annual $ $205,982.3 $/year Fuel Saving in $/year
NPV $ at $1,441,876.33 $
Pump HP 0.5 HP at 40 psi dP additional dP over what is used already
Pump ele2,892.7 KWHR/YR to feed boilers
$/KWHR 0.035 e Cost unit
$ elec/yr 101.2 $ electri/yr use BFW Pump to Feed Heat Recovery
Calc_F1-BOIL
8/3/2019 Waste Heat Boiler Evaluation for Gas Fired Heater Furnace
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If steam is produced use above to calc Sensible Heat Calc_F1-BOIL
Then Carry the value to cal. Latent Heat Requirements
H liq at T 337 Btu/# Tsat= 364 F use stm table for H
H vap at T 1204 Btu/# Psat= 160 psia use stm table for H
dH stm at T 867 Btu/# net Latent Heat Required
flow H2O 5500 #/hr frm B16 Convert gpm500=#/hrLatent Q 4768500 BTUH (BTU/#)(#/HR)
dT flue gas 119 F by ratio of above 224
T flue out 371 F 254
LMTD 67 F 84
Ax 3.9 SQ Ft.
Job Scope
Add WHR unit to Stack on both Furnace, G80F10&11
Use Single 4" feed & Return Pipe, insulate Return to G82F10&11
Add Control Valve at G82 BFW Pumps and BL Isolation Valves
Relocate Stack TI to top of WHR HX
Use FBE Pipe as inplant Runs since T does not exceed FBE Limits.
Used Finned Tubes in Coiled Arrangement approx 32ft L x 5ftOD-400SF extended area
8/3/2019 Waste Heat Boiler Evaluation for Gas Fired Heater Furnace
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basis: Vendor Proposal Summary Apr.28/09 mmscfd gpm
Recv./furn 4.2 MW/Furnace T, F, five yr look back Fuel gpm BFW pH T, F
Recv in BTUH 14.3 mmbtuh/fur MEAN Range L R Hi water Steam Inlet W
net dHs 1116 btu/# Stm F1 G26AH 490 385 580 3.5 70 25 110
H2O mass 12833 #S/hr/furn F2G26AH 515 440 625 3.5 70 25 110
H2O volume 25.7 gpm/furn F211G57AH 450 365 545 3.5 70 25 110numb Furn 4.0 number F212AM 486 310 255 380
max H2O 102.7 gpm avail 4.2MW/Furnace F212 OinAM 486 195 155 235
required H2O 210.0 gpm req'd 70*3boilers F212 OoutAM 486 265 255 380
Boiler feed water average 70 gpm/boiler G26E310A-C sheet
Based on Heat Recovered and Fuel Heat Value at 83% Boiler Effiency, study to confirm Boiler Effiency Orsat
Fuel Ax
gpm H2O m$/yr Ft2 gpm H2O Fuel at 3yrPOT CapX guess Fuel at 5yr
4 75 138 4 225 32 193 375 32 343
6 112 245 6 337 80 257 562 80 4828 150 406 8 449 179 269 748 179 568
10 187 707 10 562 435 127 937 435 501
11 206 1048 11 618 817 -199 1030 817 213
1,048 gpm H2OPV CRF=3 PC CRF=5
4 193 343
6 257 482
Calc_F1-BOIL 8 269 568
10 127 501
11 -199 213
Calc_F1-BOIL
-300
-200
-100
0
100
200
300
400
500
600
700
0 2 4 6 8 10 12
PV CRF=3
PC CRF=5
8/3/2019 Waste Heat Boiler Evaluation for Gas Fired Heater Furnace
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Estimate Area & Heat Recovery for Flue Gas Heat Recovery for MED BFW Preheat
Estimate only based on simplistic HVAC Air Water- Detailed to used actual Cp & Den's
air Q=1.08CFM(dT) btuh 1
water Q=500gpm(dT) btuh 2 Calc_F2
Water lbs/hr=500gpm 3
fuel Q=(dH)SCFH(eff) btuh 4
flue gas (SCF /SCF )=(1+%XA/200)(15FlueGz/NG 5 '(SCF /SCF )=(1+%XA/200)(15.8SG+1.8)any SCFH/60=SCFM 6
Q=U(A)LMTD(F) BTUH 7
Input
Xair 10.0 % Excess Air from Furnace Design Sheet, Study to verify
Fuel Qual FlueGz SCF/SCF Fuel MW/29 General Statement for Gas Specific Gravity
0.73 14.0 Flue/Fuel Fuel SG amount of Flue Gas per Quantity of Fuel Used
Fuel/Furn 3.5 mmscfd Fuel Flow to Furnace from PI 5 year Trend, Design to perform sensitivity analysis
Fuel 1050.0 BTU/SCF Fuel Heat Content used in calculation to determine Fuel Gas Saving
dT water 250 F Water Temperature Increase inside Waste Heat Recovery Section *
H2O/Furn 70.0 gpm BFW Avg H2O Flow per Furnace-assume G80F10 servesG82 F7 & G80F11 serve G82F8
Flue in T 515 F Flue Gas Temperature Average from PI Data Chart
T H2O in 110 F Water Temperature from Boiler Feed Water prior to Heat Recovery
Uo 25 BTUH/SF/F Overall Heat Transfer Factor, assume finned tubes
OUTPUT Qwater=Qfluegas Calc.'
Flue Gas 2,041,768.8 SCFH Flue Gas, basis: Fuel Flow from PI Fuel Flow & XA% & FuelSG Correlation
Fuel 145,833.3 scfh Convert PI Fuel Flow to SCFH from MMSCFD
Q water 8,837,500.0 BTUH Calc Water Heat duty Required by Eq#2
Flue Gas 34,029.5 SCFM Convert Flue Gas from SCFH to SCFM
dT FlueGas 220.1 F Flue Gas dT by eqn 1 & Heat Duty of Eq2
Flue out T 294.9 F Flue Gas T out by PI Flue Gas T & dT above
TH2O out 360.0 F Water T out by Assumed Inlet Water T & dTwater
LMTD 169.5 F LMTD by Text, (d1-d2)/ln(d1/d2)
Ax 2,453.3 Feet2
Recovery Exchanger Area by Eq.7 at F=0.85
Fuel Saved 10,520.8 SCFH Calc_F2
Fuel Cost 3.5 $/mSCF
Annual $ $294,583 $/year Fuel Saving in $/year
NPV $ at 7 $2,062,083 $
Pump HP 2.9 HP at 40 psi dP additional dP over what is used already
Pump elect 18,407.8 KWHR/YR to feed boilers
$/KWHR 0.035 e Cost unit
$ elec/yr 644.3 $ electri/yr use BFW Pump to Feed Heat RecoveryJob Scope
Add WHR unit to Stack on both Furnace, G80F10&11
Use Single 4" feed & Return Pipe, insulate Return to G82F10&11
Add Control Valve at G82 BFW Pumps and BL Isolation Valves
Relocate Stack TI to top of WHR HX
Use FBE Pipe as inplant Runs since T does not exceed FBE Limits.
Used Finned Tubes in Coiled Arrangement approx 32ft L x 5ftOD-400SF extended area
8/3/2019 Waste Heat Boiler Evaluation for Gas Fired Heater Furnace
8/35
Boiler feed water average 70 gpm/boiler G26E310A-C sheet Calc_F2
Summary Apr.28/09 T, F, five yr look back Fuel gpm BFW pH gpm T, F
MEAN Range L R Hi mmscfd water Steam Inlet W
F1 G26AH 490 385 580 3.5 70 25 110
F2G26AH 515 440 625 3.5 70 25 110
F211G57AH 450 365 545 3.5 70 25 110
F212AM 486 310 255 380F212 OinAM 486 195 155 235
F212 OoutAM 486 265 255 380
Based on Heat Recovered and Fuel Heat Value at 83% Boiler Effiency, study to confirm Boiler Effiency Orsat
Fuel Ax
dT H2O m$/yr Ft2 dT H2O Fuel at 3y CapX guess Fuel at 5yr
75 88 373 75 265 156 109 442 156 285.6
100 118 535 100 353 279 75 589 279 310.4
125 147 724 125 442 452 -10 737 452 285.0
150 177 946 150 530 693 -163 884 693 191.0
175 206 1211 175 619 1030 -411 1031 1030 1.0
dT1 dT2 dT H2O PV CRF=3 PV CRF=5
185 155 75 108.8 285.6
170 100 74.8 310.4
125 -9.6 285.0
150 -162.6 191.0
175 -411.4 1.0
Calc_F2
-500.0
-400.0
-300.0
-200.0
-100.0
0.0
100.0
200.0
300.0
400.0
50 75 100 125 150 175 200
PV
CRF=3
8/3/2019 Waste Heat Boiler Evaluation for Gas Fired Heater Furnace
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Estimate Area & Heat Recovery for Flue Gas Heat Recovery for MED BFW PreheatCalc_F2-BOIL
air Q=1.08CFM(dT) btuh 1 'Estimate only based on simplistic HVAC Air Water- Detailed to used actual Cp & Den's
water Q=500gpm(dT) btuh 2
Water lbs/hr=500gpm 3
fuel Q=(dH)SCFH(eff) btuh 4
flue gas (SCF /SCF )=(1+%XA/200)(15.8FlueGz/ Fuel 5 (SCF /SCF )=(1+%XA/200)(15.8SG+1.8) Calc_F2-BOIL
any SCFH/60=SCFM 6
Q=U(A)LMTD(F) BTUH 7
Input THIS SHEET BASIS IS STEAM GENERATION BY COUNTERCURRENT FLOW
Xair 10.0 % Excess Air from Furnace Design Sheet, Study to verify
Fuel Qual FlueGz SCF/SCF Fuel MW/29 General Statement for Gas Specific Gravity
0.73 14.0 Flue/Fuel Fuel SG amount of Flue Gas per Quantity of Fuel Used
Fuel/Furn 3.5 mmscfd Fuel Flow to Furnace from PI 5 year Trend, Design to perform sensitivity analysis
Fuel 1050.0 BTU/SCF Fuel Heat Content used in calculation to determine Fuel Gas Saving
dT water 254 F Water Temperature Increase inside Waste Heat Recovery Section *
H2O/Furn 12.0 gpm BFW Averaged Water Flow per Furnace-assume G80F10 servesG82 F7 & G80F11 serve G82F8
T FlueGas in 515 F Flue Gas Temperature Average from PI Data Chart
TH2O in 110 F Water Temperature from Boiler Feed Water prior to Heat Recovery
Uo 25 BTUH/SF/F Overall Heat Transfer Factor, assume finned tubes
OUTPUT Qwater=Qfluegas Calculation'
Flue Gas 2,041,768.8 SCFH Amount of Flue Gas, based on Fuel Flow from PI Fuel Flow & XA% & FuelSG Correlation
Fuel 145,833.3 scfh Convert PI Fuel Flow to SCFH from MMSCFD
Q water 1,539,240.0 BTUH Calc Water Heat duty Required by Eq#2
Flue Gas 34,029.5 SCFM Convert Flue Gas from SCFH to SCFM
dT FlueGas 38.3 F Flue Gas dT by eqn 1 & Heat Duty of Eq2
T FlueGas out 347.1 F Flue Gas T out by PI Flue Gas T & dT above
TH2O out 364.0 F Water T out by Assumed Inlet Water T & dTwater
LMTD 89.8 F LMTD by Text, (d1-d2)/ln(d1/d2)
Ax 807.0 Feet squared Recovery Exchanger Area by Eq.7 at F=0.85
Fuel Saved 8,025.3 SCFH Based on Heat Recovered and Fuel Heat Value at 83% Boiler Effiency,
Fuel Cost 3.5 $/mSCF study to confirm Boiler Effiency Orsat
Annual $ $224,708.0 $/year Fuel Saving in $/year
NPV $ at 7 $1,572,956.00 $
8/3/2019 Waste Heat Boiler Evaluation for Gas Fired Heater Furnace
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Pump HP 0.5 HP at 40 psi dP additional dP over what is used already Calc_F2-BOIL
Pump elect 3,155.6 KWHR/YR to feed boilers
$/KWHR 0.035 e Cost unit
$ elec/yr 110.4 $ electri/yr use BFW Pump to Feed Heat Recovery
If steam is produced use above to calc Sensible Heat dT1 dT2 At
Then Carry the value to cal. Latent Heat Requirements 237.1 21.5 810.3
H.liq @T 337.0 Btu/# Tsat= 364 F use stm table for HH.vap @T 1204.0 Btu/# Psat= 160 psia use stm table for H
dH stm @T 867.0 Btu/# net Latent Heat Required
flow H2O 6000.0 #/hr frm B16 Convert gpm500=#/hr
Latent Q 5202000.0 BTUH (BTU/#)(#/HR)
dT flue gas 129.5 F by ratio of above 224
T flue out 385.5 F
LMTD 86.2 F
Ax 3.3 SQ Ft.
91.2
Recv./furn 4.2 MW/Furnace Job Scope
Recv in BTUH 14.3 mmbtuh/fur Add WHR unit to Stack on both Furnace, G80F10&11
net dHs 1116.0 btu/# Stm Use Single 4" feed & Return Pipe, insulate Return to G82F10&11
H2O mass 12833.3 #S/hr/furn Add Control Valve at G82 BFW Pumps and BL Isolation ValvesH2O volume 25.7 gpm/furn Relocate Stack TI to top of WHR HX
numb Furn 4.0 number Use FBE Pipe as inplant Runs since T does not exceed FBE Limits.
max H2O 102.7 gpm avail 4.2MW/Furnace Used Finned Tubes in Coiled Arrangement
required H2O 210.0 gpm req'd 70*3boilers approx 32ft L x 5ftOD-400SF extended area
clc rec 6.74 mm btuh
clc rec 1.98 MW/Furn
8/3/2019 Waste Heat Boiler Evaluation for Gas Fired Heater Furnace
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Calc_F2-BOIL Boiler feed water average 70 gpm/boiler G26E310A-C sheet
Summary Apr.28/09 T, F, five yr look back Fuel gpm BFW pH gpm T, F gpm H2O PV CRF=3 PC CRF=5
MEAN Range L R Hi mmscfd water Steam Inlet W 4 200 350
stack F1 G26AH 490 385 580 3.5 70 25 110 6 278 502
stack F2G26AH 515 440 625 3.5 70 25 110 8 326 626
stack F211G57AH 450 365 545 3.5 70 25 110 10 314 689
stack F212AM 48 310 255 380 12 133 583
oil F212 OinAM195 155 235
oil F212 OoutA 265 255 380
Calc_F2-BOIL
Fuel Ax
gpm H2O m$/yr Ft2 gpm H2O Fuel at 3yr CapX guess Fuel at 5yr
4 75 118 4 225 25 200 375 25 350
6 112 204 6 337 60 278 562 60 502
8 150 321 8 449 123 326 749 123 626
10 187 497 10 562 248 314 937 248 689
12 225 810 12 674 541 133 1124 541 583
0
100
200
300
400
500
600
700
800
0 2 4 6 8 10 12 14
PV CRF=3
PC CRF=5
8/3/2019 Waste Heat Boiler Evaluation for Gas Fired Heater Furnace
12/35
Estimate Area & Heat Recovery for Flue Gas Heat Recovery for MED BFW Preheat
air Q=1.08CFM(dT) btuh 1 'Estimate only based on simplistic HVAC Air Water-
water Q=500gpm(dT) btuh 2 Detailed to used actual Cp & Den's
Water lbs/hr=500gpm 3 'Boiler feed water average 70 gpm/boiler G26E310A-C sheet
fuel Q=(dH)SCFH(eff) btuh 4
flue gas (SCF /SCF )=(1+%XA/200)(1 FlueGz/ Fuel 5 '(SCF /SCF )=(1+%XA/200)(15.8SG+1.8)
any SCFH/60=SCFM 6Q=U(A)LMTD(F) BTUH 7 Calc_F2-BOIL50#
Input THIS SHEET BASIS IS STEAM GENERATION BY COUNTERCURRENT FLOW
Xair 10.0 % Excess Air from Furnace Design Sheet, Study to verify
Fuel Qual FlueGz SCF/SCF Fuel MW/29 General Statement for Gas Specific Gravity
0.73 14.0 Flue/Fuel Fuel SG amount of F lue Gas per Quantity of Fuel Used
Fuel/Furn 3.5 mmscfd Fuel Flow to Furnace: PI 5 year Trend, Design to make sensitivity analysis
Fuel 1050.0 BTU/SCF Fuel Heat Content used in calculation to determine Fuel Gas Saving
dT water 149.3 F Water Temperature Increase inside Waste Heat Recovery Section *
H2O/Furn 18.0 gpm BFW Avg. H2O Flow/Furnace-assume G80F10->G82 F7 & G80F11->G82F8
T FlueGas in 515 F Flue Gas Temperature Average from PI Data ChartTH2O in 110 F Water Temperature from Boiler Feed Water prior to Heat Recovery
Uo 25 BTUH/SF/F Overal l Heat Transfer Factor, assume finned tubes
OUTPUT Qwater=Qfluegas Calculation
Flue Gas 2,041,768.8 SCFH Flue Gas, basis: Fuel Flow from PI Fuel Flow & XA% & FuelSG Correlation
Fuel 145,833.3 scfh Convert PI Fuel Flow to SCFH from MMSCFD
Q water 1,357,137.0 BTUH Calc Water Heat duty Required by Eq#2
Flue Gas 34,029.5 SCFM Convert Flue Gas from SCFH to SCFM
dT FlueGas 33.8 F Flue Gas dT by eqn 1 & Heat Duty of Eq2
T FlueGas out 270.7 F Flue Gas T out by PI Flue Gas T & dT above
TH2O out 259.3 F Water T out by Assumed Inlet Water T & dTwater
LMTD 91.1 F LMTD by Text, (d1-d2)/ln(d1/d2)
Ax 701.0 FeetSquared Recovery Exchanger Area by Eq.7 at F=0.85
Fuel Saved 11,676.4 SCFH Based on Heat Recovered and Fuel Heat Value
Fuel Cost 3.5 $/mSCF at 83% Boiler Effiency, study to confirm Boiler Effiency Orsat
Annual $ $326,937.9 $/year Fuel Saving in $/year
NPV $ at 7 $2,288,565.30 $
Pump HP 0.7 HP at 40 psi dP additional dP over what is used already
Pump elect 4,733.4 KWHR/YR to feed boilers
$/KWHR 0.035 e Cost unit$ elec/yr 165.7 $ electri/yr use BFW Pump to Feed Heat Recovery
Calc_F2-BOIL50#
8/3/2019 Waste Heat Boiler Evaluation for Gas Fired Heater Furnace
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If steam is produced use above to calc Sensible Heat Calc_F2-BOIL50#
Then Carry the value to cal. Latent Heat Requirements At
H liq at T 703.8
H vap at T
dH stm at T
flow H2O dT1 dT2
Latent Q 160.7 45.2dT flue gas 228 Btu/# Tsat= 259 F use stm table for H
T flue out 1167 Btu/# Psat= 35 psia use stm table for H
LMTD 939 Btu/# net Latent Heat Required
Ax 9000 #/hr frm B16 Convert gpm500=#/hr
8451000 BTUH (BTU/#)(#/HR)
210 F by ratio of above 224
Recv./furn 305 F
Recv in BTUH 150 F
net dHs 2.8 SQ Ft.
H2O mass Calc_F2-BOIL50#
H2O volume 177
numb Furn 4.2 MW/Furnace
max H2O 14.3 mmbtuh/fur
required H2O 1116 btu/# Stm
12833 #S/hr/furn
25.7 gpm/furn
4.0 number
102.7 gpm avail 4.2MW/Furnace
210.0 gpm req'd 70*3boilers
8/3/2019 Waste Heat Boiler Evaluation for Gas Fired Heater Furnace
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Summary Apr.28/09 T, F, five yr look bac Fuel gpm BFW pH gpm T, F
MEAN Range L R Hi mmscfd water Steam Inlet W
stack F1 G26AH 490 385 580 3.5 70 25 110
stack F2G26AH 515 440 625 3.5 70 25 110
stack F211G57AH 450 365 545 3.5 70 25 110
stack F212AM 486 310 255 380
oil F212 OinAM 486 195 155 235oil F212 OoutAM 486 265 255 380
Calc_F2-BOIL50#
Fuel Ax gpm H2O CapX guess
gpm H2O m$/yr Ft2 Fuel at 3yrPOT Fuel at 5yr
10 182 181 10 545 49 495 908 49 859
12 218 250 12 654 82 572 1090 82 1008
15 273 406 15 819 179 640 1365 179 1186
18 327 703 18 981 431 550 1635 431 1204
21 381 1678 21 1144 1735 -591 1907 1735 172
gpm H2O PV CRF=3PC CRF=5
10 495 859
12 572 1008
15 640 1186
18 550 1204
21 -591 172
Calc_F2-BOIL50#
Job Scope
Add WHR unit to Stack on both Furnace, G80F10&11
Use Single 4" feed & Return Pipe, insulate Return to G82F10&11
Add Control Valve at G82 BFW Pumps and BL Isolation ValvesRelocate Stack TI to top of WHR HX
Use FBE Pipe as inplant Runs since T does not exceed FBE Limits.
Used Finned Tubes in Coiled Arrangement approx 32ft L x 5ftOD-400SF extended area
Calc_F2-BOIL50#
-1000
-500
0
500
1000
1500
10 15 20 25
PV
CRF=3
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Estimate Area & Heat Recovery for Flue Gas Heat Recovery for MED BFW Preheat
air Q=1.08CFM(dT) btuh 1 Estimate only based on simplistic HVAC Air Water- Detailed to used actual Cp & Den's
water Q=500gpm(dT) btuh 2
Water lbs/hr=500gpm 3 Calc_F211
fuel Q=(dH)SCFH(eff) btuh 4
flue gas (SCF /SCF )=(1+%XA/200)(15.8SG+1.8) FlueGz/ Fuel 5 '(SCF /SCF )=(1+%XA/200)(15.8SG+1.8)
any SCFH/60=SCFM 6
Q=U(A)LMTD(F) BTUH 7
Input
Xair 10.0 % Excess Air from Furnace Design Sheet, Study to verifyFuel Qual FlueGz SCF/SCF Fuel MW/29 General Statement for Gas Specific Gravity
0.73 14.0 Flue/Fuel Fuel SG amount of Flue Gas per Quantity of Fuel Used
Fuel/Furn 3.5 mmscfd Fuel Flow to Furnace from PI 5 year Trend, Design to perform sensitivity analysis
Fuel 1050.0 BTU/SCF Fuel Heat Content used in calculation to determine Fuel Gas Saving
dT water 75 F Water Temperature Increase inside Waste Heat Recovery Section *
H2O/Furn 70.0 gpm BFW Averaged Water Flow per Furnace-assume G80F10 servesG82 F7 & G80F11 serve G82F8
T FlueGas in 450 F Flue Gas Temperature Average from PI Data Chart
TH2O in 110 F Water Temperature from Boiler Feed Water prior to Heat Recovery
Uo 25 BTUH/SF/F Overall Heat Transfer Factor, assume finned tubes
OUTPUT Qwater=Qfluegas Calculation'
Flue Gas 2,041,768.8 SCFH FlueGas, basis: Fuel by PI Fuel & XA% & FuelSG Corr.
Fuel 145,833.3 scfh Convert PI Fuel Flow to SCFH from MMSCFD
Q water 2,651,250.0 BTUH Calc Water Heat duty Required by Eq#2Flue Gas 34,029.5 SCFM Convert Flue Gas from SCFH to SCFM
dT FlueGas 66.0 F Flue Gas dT by eqn 1 & Heat Duty of Eq2
T FlueGas out 384.0 F Flue Gas T out by PI Flue Gas T & dT above
TH2O out 185.0 F Water T out by Assumed Inlet Water T & dTwater
LMTD 269.5 F LMTD by Text, (d1-d2)/ln(d1/d2)
Ax 463.0 Feet squared Recovery Exchanger Area by Eq.7 at F=0.85
Calc_F211
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Fuel Saved 3,156.3 SCFH Calc_F211
Fuel Cost 3.5 $/mSCF
Annual $ $88,375.0 $/year Fuel Saving in $/year
NPV $ at 7 $618,625.00 $
Pump HP 2.9 HP at 40 psi dP additional dP over what is used already
Pump elect 18,407.8 KWHR/YR to feed boilers
$/KWHR 0.035 e Cost unit
$ elec/yr 644.3 $ electri/yr use BFW Pump to Feed Heat Recovery
If steam is produced use above to calc Sensible Heat
Then Carry the value to cal. Latent Heat Requirements
H liq at T 337 Btu/# Tsat= 364 F use stm table for H
H vap at T 1204 Btu/# Psat= 160 psia use stm table for H
dH stm at T 867 Btu/# net Latent Heat Required
flow H2O 35000 #/hr frm B16 Convert gpm500=#/hr
Latent Q 30345000 BTUH (BTU/#)(#/HR)
dT flue gas 755.7007138 F by ratio of above 224
T flue out -371.7
Job Scope Calc_F211
Add WHR unit to Stack on both Furnace, G80F10&11
Use Single 4" feed & Return Pipe, insulate Return to G82F10&11
Add Control Valve at G82 BFW Pumps and BL Isolation Valves
Relocate Stack TI to top of WHR HX
Use FBE Pipe as inplant Runs since T does not exceed FBE Limits.
Used Finned Tubes in Coiled Arrangement approx 32ft L x 5ftOD-400SF extended area
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Calc_F211 Boiler feed water average 70 gpm/boiler G26E310A-C sheet
Summary Apr.28/09 T, F, five yr look back Fuel gpm BFW pH gpm T, F
MEAN Range L R Hi mmscfd water Steam Inlet W dT H2O PV CRF=3 PC CRF=5
F1 G26AH 490 385 580 3.5 70 25 110 75 44 221
F2G26AH 515 440 625 3.5 70 25 110 100 255 490
F211G57AH 450 365 545 3.5 70 25 110 125 -239 56
F212AM 486 310 255 380 150 -560 -206
F212 OinAM 486 195 155 235 175 -1088 -676
F212 OoutAM 486 265 255 380Based on Heat Recovered and Fuel Heat Value at 83% Boiler Effiency, study to confirm Boiler Effiency Orsat
Fuel Ax CapX guess
dT H2O m$/yr Ft2 dT H2O Fuel at 3yrPOT Fuel at 5yr
75 88 463 75 265 221 44 442 221 221
100 118 280 100 353 99 255 589 99 490
125 147 935 125 442 681 -239 737 681 56
150 177 1255 150 530 1090 -560 884 1090 -206
175 206 1661 175 619 1707 -1088 1031 1707 -676
-1200
-1000
-800
-600
-400
-2000
200
400
600
50 75 100 125 150 175 200PV CRF=3
PC CRF=5
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Estimate Area & Heat Recovery for Flue Gas Heat Recovery for MED BFW Preheat
air Q=1.08CFM(dT) btuh 1 'Estimate only based on simplistic HVAC Air Water- Detailed to used actual Cp & Den's
water Q=500gpm(dT) btuh 2
Water lbs/hr=500gpm 3 Calc_F211_BOIL
fuel Q=(dH)SCFH(eff) btuh 4
flue gas (SCF /SCF )=(1+%XA/200)(15.8SG+1.8) FlueGz/ Fuel 5 Boiler feed water average 70 gpm/boiler G26E310A-C sheet
any SCFH/60=SCFM 6
Q=U(A)LMTD(F) BTUH 7
Input
Xair 10.0 % Excess Air from Furnace Design Sheet, Study to verifyFuel Qual FlueGz SCF/SCF Fuel MW/29 General Statement for Gas Specific Gravity
0.73 14.0 Flue/Fuel Fuel SG amount of Flue Gas per Quantity of Fuel Used
Fuel/Furn 3.5 mmscfd Fuel Flow to Furnace from PI 5 year Trend, Design to perform sensitivity analysis
Fuel 1050.0 BTU/SCF Fuel Heat Content used in calculation to determine Fuel Gas Saving
dT water 254 F Water Temperature Increase inside Waste Heat Recovery Section *
H2O/Furn 7.0 gpm BFW Averaged Water Flow per Furnace-assume G80F10 servesG82 F7 & G80F11 serve G82F8
T FlueGas in 450 F Flue Gas Temperature Average from PI Data Chart
TH2O in 110 F Water Temperature from Boiler Feed Water prior to Heat Recovery
Uo 25 BTUH/SF/F Overall Heat Transfer Factor, assume finned tubes
OUTPUT Qwater=Qfluegas Calculation'
Flue Gas 2,041,768.8 SCFH Flue Gas, based on Fuel Flow from PI Fuel Flow & XA% & FuelSG Correlation
Fuel 145,833.3 scfh Convert PI Fuel Flow to SCFH from MMSCFD
Q water 897,890.0 BTUH Calc Water Heat duty Required by Eq#2Flue Gas 34,029.5 SCFM Convert Flue Gas from SCFH to SCFM
dT FlueGas 22.4 F Flue Gas dT by eqn 1 & Heat Duty of Eq2
T FlueGas out 352.1 F Flue Gas T out by PI Flue Gas T & dT above
TH2O out 364.0 F Water T out by Assumed Inlet Water T & dTwater
LMTD 73.7 F LMTD by Text, (d1-d2)/ln(d1/d2)
Ax 573.6 Feet squared Recovery Exchanger Area by Eq.7 at F=0.85
Calc_F211_BOIL
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Fuel Saved 4,681.4 SCFH
Fuel Cost 3.5 $/mSCF
Annual $ $131,079.7 $/year Fuel Saving in $/year
NPV $ at 7 $917,557.67 $ Calc_F211_BOIL
Pump HP 0.3 HP at 40 psi dP additional dP over what is used already
Pump elect 1,840.8 KWHR/YR to feed boilers
$/KWHR 0.035 e Cost unit
$ elec/yr 64.4 $ electri/yr use BFW Pump to Feed Heat Recovery
If steam is produced use above to calc Sensible Heat dT1 dT2
Then Carry the value to cal. Latent Heat Requirements 242.1 10.4
H liq at T 337.0 Btu/# Tsat= 364 F use stm table for H
H vap at T 1204.0 Btu/# Psat= 160 psia use stm table for H
dH stm at T 867.0 Btu/# net Latent Heat Required
flow H2O 3500.0 #/hr frm B16 Convert gpm500=#/hr
Latent Q 3034500.0 BTUH (BTU/#)(#/HR)
dT flue gas 75.6 F by ratio of above 224
T flue out 374.4 F Calc_F211_BOIL
LMTD 48.2 F
Ax 3.4 SQ Ft. Job Scope
53.2 Add WHR unit to Stack on both Furnace, G80F10&11
Recv./furn 4.2 MW/Furnace Use Single 4" feed & Return Pipe, insulate Return to G82F10&11
Recv in BTUH 14.3 mmbtuh/fur Add Control Valve at G82 BFW Pumps and BL Isolation Valves
net dHs 1116.0 btu/# Stm Relocate Stack TI to top of WHR HX
H2O mass 12833.3 #S/hr/furn Use FBE Pipe as inplant Runs since T does not exceed FBE Limits.
H2O volume 25.7 gpm/furn Used Finned Tubes in Coiled Arrangement approx 32ft L x 5ftOD-400SF extended area
numb Furn 4.0 number
max H2O 102.7 gpm avail 4.2MW/Furnace
required H2O 210.0 gpm req'd 70*3boilers
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Summary Apr.28/09 T, F, five yr look back Fuel gpm BFW pH gpm T, F dT H2O PV CRF=3 PV CRF=5
MEAN Range L R Hi mmscfd water Steam Inlet W 2 100 175
F1 G26AH 490 385 580 3.5 70 25 110 3 140 253
F2G26AH 515 440 625 3.5 70 25 110 4 170 319
F211G57A 450 365 545 3.5 70 25 110 6 171 396
F212AM 4 310 255 380 7 79 341
F212 OinA 195 155 235
F212 Oout 265 255 380
Based on Heat Recovered and Fuel Heat Value at 83% Boiler Effiency, study to confirm Boiler Effiency Orsat
Fuel Ax
gpm H2O m$/yr Ft2 gpm H2O Fuel at 3yr CapX guess Fuel at 5yr
2 38 78 2 113 13 100 188 13 175
3 56 128 3 169 28 140 281 28 253
4 75 191 4 224 54 170 373 54 319
6 112 387 6 337 166 171 562 166 396
7 131 577 7 393 314 79 655 314 341
sf total 577
Calc_F211_BOIL
0
50
100
150
200
250
300
350
400
450
0 1 2 3 4 5 6 7 8
PV CRF=3
PV CRF=5
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based on this, average water flow is 70 gpm
3units at 35,000#H2O/hr and 35,000/500= 70 gpm G26E310A-C
based on chart avg BFW T is 110F
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SFUT_56FI1530.PV Split flow to F1, F2, F211
G26E310A-C SFUT_56FI1531.PV
SFUT_56FI1532.PV
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SFWC_53FI1437.pv Fuel F212
SFDS_85FI1100.PV Q-F212-3 Fuel
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Q-F212-3 Fuel
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avg=3.5mmscfd G26F1Fuel
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G26F1Fuel
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310F avg Stack T F212_486AM-
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F1Stack SFDS_75TI247A.PV F2Stack SFDS_75TI247E.PV F1F2 Stack T_G26AH-
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460 F211_G57AH.
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267F out T 188F inlet 212HotOil T in 212HotOil T in
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Summary Apr.28/09 T, F, five yr look back mmscfd mmscfd gpm BFW pH gpm
MEAN Range L R Hi fuel flow avg fuel water Steam Oprn sumry
F1 G26AH stack o 490 385 580 3.5 3.5 70 25
F2G26AH stack o 515 440 625 3.5 3.5 70 25
F211G57AH stack o 450 365 545 3.3 3.5 70 25
F212G57AH stack o 310 255 380 2.7 NA na
F212 Oil nAM 486 195 155 235
F212 Oil oAM 486 265 255 380 Oprn sumry
Average Water Flow Per Boiler 70 gpm average fuel flow per furnace 3.5 mmscfd
Steam Pressure 175 psig Steam & Water Phy Prop From eSteam Table
Steam Pressure 160 psia H Sat Stm 160psia 1195.1 btu/lb
Avg Fd Water T 110 F T sat Stm 160psia 363.6 F
H Sat H2O 160psia 336.1 btu/lb
MW Flue Gas 30 #/Mol H Sat H2O 110F 78.0 btu/lb
Cp Flue Gas 0.25 BTU/#/F Cp water 1.018 btu/lb/F
Flue Gas Heat F 1.18 BTU/HR/SCFM/dF dH vap 160psia 859.0 btu/lb
Total dH H2O furn 1117.1 btu/lb
Sen dH H2O furn 258.1 btu/lb
Den BFW 61.9 #/CF
Oprn sumry SG BFW 1.0 v/v
BFW Heat Factor 505.0 BTU/Hr/gpm/dF
dT water 253.6
Oprn sumry
Fuel Gas to Flue Gas Homologues of Parrifinic HC Gas & Stoc. Combustion
C+O2=CO2 H2+0.5O2=H2O
SG gas #C's H2 oC oH Sum O2 N2 Sum Sum air CmbGas FlueGz
0.55 C1 1 2 1 0.5 2.0 7.5 9.5 3 11.2
1.03 C2 2 3 1 0.5 3.5 13.2 16.7 5 19.3
1.52 C3 3 4 1 0.5 5.0 18.8 23.8 7 27.4
2.00 C4 4 5 1 0.5 6.5 24.5 31.0 9 35.5
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G26-F211 and F212 Spec sheets
Furnace Spec Sheets
G26F1 &F2 spec sheet
G26FurnSpecs-DSN
D779316001T01.tiff
D780951001T01.tiff
D780951002T01.tiff
D780951003T01.tiff
D780951004T01.tiff
D780951005T01.tiff
D780951006T01.tiff
Adobe Acrobat
Document
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Saf Fuel Gas Comp Saf Fuel Gas Comp twister SG1 new
BI-224 P/L gas P/L gas P/L gas P/L gas
DBSP.pg9 Lab Sample Saf-S saf-w Saf-S saf-w avg S avg W
WetGas B Ap20/08
N2 0.70 3.19 0.71 0.73 0.71 0.73 0.71 0.73
CO2 1.20 1.23 1.40 1.43 1.40 1.43 1.40 1.43
H2S 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00C1 72.39 65.64 67.42 69.57 67.44 69.40 67.43 69.49
C2 16.90 15.15 16.08 16.09 16.08 16.11 16.08 16.10
C3 7.40 10.77 10.14 9.11 10.14 9.20 10.14 9.15 9.65
iC4 0.20 0.94 0.93 0.72 0.93 0.73 0.93 0.72 0.83
nC4 0.80 2.25 2.47 1.80 2.47 1.84 2.47 1.82 2.15
iC5 0.20 0.23 0.38 0.24 0.38 0.24 0.38 0.24 0.31
nC5 0.20 0.21 0.38 0.26 0.36 0.27 0.37 0.26 0.32
n6 0.00 0.01 0.08 0.04 0.08 0.04 0.08 0.04 0.06
C7+ 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00
nC8 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00
nC9 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00
nC10 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00
O2 0.00 0.38 0.00 0.00 0.00 0.00 0.00 0.00 13.31
H2 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00
He 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00
H2O 0.01 0.00 0.01 0.01 0.01 0.01 0.01 0.01
sum 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00
SG 0.74 0.81
mw 21.58 23.39
cp/cv 1.25
NHV 1148
Tc* R 407.61
Pc* psia 669.3 Saf Fuel Gas Comp
Mx&Norm
sweet
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%Cond HC condy defined as C3+
Apr20 anal 13.655
BI224 dbsp 8.8
1.55 ratio of Conden HC
bpd condy 466 above ratio times 300bpd/10.5mmscfd feed
1020 condy at 23MMSCFD with heavy summer feed
657 condy at 23MMSCFD with light winter feed
Saf Fuel Gas Comp
Recovery Range EstimateBasis: Quote From Twister for Tanajib using BI-224 composition & recovery =300bpd/10.5mmscfd
Consider the summer pipeline gas to be richer as temps are higher, winter has lower dew point
Winter Case considered as BI-224, summer as Apr.20 analysis
case summer winter Saf Fuel Gas Comp
gas mmscfd 23 23
condy recv. 657 1056