4,1a ASME TEST FORM SUMMARY SHEET FOR ABBREVIATED EFFICIENCY TEST PTC 4.1-a(1964) TEST NO BOILER NO DATE OWNER OF PLANT LOCATION TEST CONDUCTED BY OBJECTIVE TEST DURATION BOILER MAKE & TYPE RATED CAPACITY STOKER TYPE & SIZE PULVERIZER, TYPE & SIZE BURNER, TYPE & SIZE FUEL USED MINE COUNTY STATE SIZE AS FIRED PRESSURE & TEMPERATURES FUEL DATA 1 STEAM PRESSURE IN BOILER DRUM psia COAL AS FIRED PROX.ANALYSIS % wt OIL 2 STEAM PRESSURE AT S.H. OUTLET psia 37 MOISTURE 51 FLASH POINT F* 3 STEAM PRESSURE AT R.H.INLET psia 38 VOL MATTER 52 Sp.Gravity Deg.API* 4 STEAM PRESSURE AT R.H OUTLET psia 39 FIXED CARBON 53 VISCOSITY AT SSU* BURNER SSF* 5 STEAM TEMPERATURE AT S.H. OUTLET F 40 ASH 44 TOTAL HYDROGEN % wt data inputan 6 STEAM TEMPERATURE AT R.H. INLET F TOTAL 41 Btu per lb perhitungan 7 STEAM TEMPERATURE AT R.H. OUTLET F 41 Btu per lb AS FIRED nilai dari tabel 8 WATER TEMP.ENTERING (ECON.)(BOILER) F 42 ASH SOFT TEMP. ASTM METHOD GAS % VOL not clear 9 STEAM QUALITY % MOISTURE OR P.P.M. F COAL OR OIL AS FIRED ULTIMATE ANALYSIS 54 CO 10 AIR TEMP.ARROUND BOILER (AMBIENT) F 43 CARBON 55 CH4 METHANE 11 TEMP AIR FOR COMBUSTION (This is Reference Temperature) ** F 44 HYDROGEN 56 C2H2 ACETYLENE 12 TEMPERATURE OF FUEL F 45 OXYGEN 57 C2H4 ETHYLENE 13 GAS TEMP.LEAVING (Boiler)(Econ.)(Air Htr.) F 46 NITROGEN 58 C2H6 ETHANE 14 GAS TEMP.ENTERING AH (If conditions to be corrected to guarantee) F 47 SULPHUR 59 H2S U N I T Q U A N T I T I E S 40 ASH 60 CO2 15 ENTHALPY OF SAT.LIQUID (TOTAL HEAT) Btu/lb 37 MOISTURE 61 H2 HYDROGEN 16 ENTHALPY OF (SATURATED) (SUPERHEATED) STM. Btu/lb TOTAL 0.000 TOTAL 0.000 17 ENTHALPY OF SAT.FEED TO (BOILER) (ECON.) Btu/lb COAL PULVERIZATION TOTAL HYDROGEN % wt ERROR:#DIV/0! 18 ENTHALPY OF REHEATED STEAM R.H. INLET Btu/lb 48 GRINDABILITY INDEX * 62 DENSITY 68 F ' ATM.PRESS. 19 ENTHALPY OF REHEATED STEAM R.H. OUTLET Btu/lb 49 FINESS % THRU 50 M* 63 Btu PER CU FT 20 HEAT ABS/LB R.H.STEAM (ITEM 16 - ITEM 17) Btu/lb 0 50 FINESS % THRU 200 M* 41 Btu PER LB 21 HEAT ABS/LB R.H.STEAM (ITEM 19 - ITEM 18) Btu/lb 0 64 INPUT-OUTPUT ITEM 31 X 100 ERROR:#DIV/0! EFFICIENCY OF UNIT % ITEM 29 22 DRY REFUSE (ASH PIT+FLY ASH) PER LB AS FIRED FUEL lb/lb HEAT LOSS EFFICIENCY Btu/lb A.F. FUEL % of A.F. FUEL 23 Btu PER LB IN REFUSE (WEIGHTED AVERAGE) Btu/lb 65 HEAT LOSS DUE TO DRY GAS ERROR:#DIV/0! ERROR:#DIV/0! 24 CARBON BURNED PER LB AS FIRED FUEL lb/lb 0 66 HEAT LOSS DUE TO MOISTURE IN FUEL 0.000 ERROR:#DIV/0! 25 DRY GAS PER LB AS FIRED FUEL BURNED lb/lb ERROR:#DIV/0! 67 HEAT LOSS DUE TO H2O FROM COMB.OF H2 0.000 ERROR:#DIV/0! HOURLY QUANTITIES 68 HEAT LOSS DUE TO COMBUST.IN REFUSE 0.000 ERROR:#DIV/0! 26 ACTUAL WATER EVAPORATED lb/hr 0 69 HEAT LOSS DUE TO RADIATION ERROR:#DIV/0! ERROR:#DIV/0! 27 REHEAT STEAM FLOW lb/hr 0 70 UNMEASURED LOSSES 0.000 ERROR:#DIV/0! 28 RATE OF FUEL FIRING (AS FIRED wt) lb/hr 0 71 TOTAL ERROR:#DIV/0! ERROR:#DIV/0! 29 TOTAL HEAT INPUT (Item 28 x Item 41) kB/hr 0 72 EFFICIENCY = (100 - Item 71) ERROR:#DIV/0! 1000 30 HEAT OUTPUT IN BLOW-DOWN WATER kB/hr 0 31 TOTAL kB/hr 0 HEAT (Item 26 x Item 20) + (Item 27 x Item 21) + Item 30 OUTPUT 1000 FLUE GAS ANAL.(BOILER)(ECON)(AIR HTR) OUTLET 32 CO2 % VOL 33 O2 % VOL 34 CO % VOL 35 N2 (BY DIFFERENCE) % VOL 36 EXCESS AIR % ERROR:#DIV/0! 4,1b PTC 4.1-a(1964) ASME TEST FORM CALCULATION SHEET FOR ABBREVIATED EFFICIENCY Revised September, 1965 lb of water blowdown per hr = TEST NO BOILER NO DATE 0 30 HEAT OUTPUT IN BOILER BLOW-DOWN WATER = LB OF WATER BLOW-DOWN PER HR x Item 15 Item 17 kB/hr 0 - 0 0 1000 24 If impractical to weight refuse, this item can be estimated as follows NOTE : IF FLUE DUST & ASH PIT REFUSE DIFFER MATERIALLY IN COMBUSTIBLE CONTENT, THEY SHOULD BE ESTIMATED SEPARATELY. SEE SECTION 7, COMPUTATIONS. DRY REFUSE PER LB OF AS FIRED FUEL= pds3: jumlah bahan yang tidak terbakar terhadap bahan yang terbakar % ASH IN AS FIRED COAL 100 - % COMB.IN REFUSE SAMPLE CARBON BURNED ITEM 43 ITEM 22 ITEM 23 PER LB AS FIRED = = 0 - 0.00 x 0 = 0.000 FUEL 100 14,500 25 DRY GAS PER LB AS FIRED FUEL = 11CO2 + 8O2 + 7(N2 + CO) x (LB CARBON BURNED PER LB AS FIRED FUEL + 3 5 ) BURNED 3 (CO2 + CO ) 8 ITEM 32 ITEM 33 ITEM 35 ITEM 34 ITEM 24 + ITEM 47 = 11 x 0 + 8 x 0 + 7 0 + 0 x 0 0 ERROR:#DIV/0! 267 ITEM 32 ITEM 34 3 x 0 + 0 36 EXESS O2 - CO ITEM 33 - ITEM34/2 AIR 1 = 100 x 2 = 100 x 0 0 = ERROR:#DIV/0! .2682N2 - O2 - CO .2682 (ITEM 35) - ITEM 33 -ITEM 34/2 2 0 0 - 0 1 psi = 0,069 bar H E A T L O S S E F F I C I E N C Y Btu/lb LOSS x LOSS AS FIRED HHV % FUEL 100 65 HEAT LOSS DUE LB DRY GAS ITEM 25 x ((ITEM 13) - (ITEM 11)) 65 X 100 TO DRY GAS = PER LB AS x CP x (tjvg - t air) = 0.24 = ERROR:#DIV/0! 41 ERROR:#DIV/0! FIRED FUEL Unit ERROR:#DIV/0! 0 - 0 66 HEAT LOSS DUE LB H2O PER LB 0 x 66 X 100 MOISTURE IN FUEL = AS FIRED FUEL x [(ENTHALPY OF VAPOR AT 1 PSIA & T GAS LVG) 0.000 pds3: pds3: ini kan temperatur?? Bukan entalpi??? 41 ERROR:#DIV/0! - (ENTHALPY OF LIQUID AT T AIR)] = ITEM 37/100 x [(ENTHAPLY OF VAPOR AT 1 PSIA & T ITEM 13) - (ENTHALPY OF LIQUID AT T ITEM 11)] = â¦â¦ 67 HEAT LOSS DUE TO H2O FROM COMB.OF H2 = 9H2 x [(ENTHALPY OF VAPOR AT 1 PSIA & T GAS 67 X 100 0 LVG) - (ENTHALPY OF LIQUID AT T AIR)] 0.000 pds3: pds3: ini kan temperatur?? Bukan entalpi??? 41 ERROR:#DIV/0! = 9 x ITEM 44 x [(ENTHALPY OF VAPOR AT 1 PSIA & T ITEM 13) - (ENTHALPY OF LIQUID AT 100 T ITEM 11)] = 68 HEAT LOSS DUE TO ITEM 22 ITEM 23 68 X 100 COMBUSTIBLE IN REFUSE = 0 x 0 = 0.000 41 ERROR:#DIV/0! 69 HEAT LOSS DUE TO TOTAL BTU RADIATION LOSS PER HR ERROR:#DIV/0! 69 X 100 RADIATION * = LB AS FIRED FUEL - ITEM 28 = - 0 41 ERROR:#DIV/0! 70 UNMEASURED LOSSES ** 70 X 100 41 ERROR:#DIV/0! 71 TOTAL ERROR:#DIV/0! ERROR:#DIV/0! 72 EFFICIENCY = ( 100 - ITEM 71) ERROR:#DIV/0! inputan 1 Inputan untuk Boiler Test eficiency berdasar PTC 4,1 No Data yang harus diinput Nilai satuan Pressure & Temperature 1 Steam Pressure In Boiler Drum psia 2 Steam Pressure at S.H. Outlet psia 3 Steam Pressure at R.H. inlet psia 4 Steam Pressure at R.H. outlet psia 5 Steam Temperature at S.H. outlet F 6 Steam Temperature at R.H. inlet F 7 Steam Temperature at R.H. outlet F 8 Water Temp. Entering (Econ.)(Boiler) F 9 Steam Quality % moisture or p.p.m F 10 Air Temp. Arround Boiler (ambient) F 11 Temp air for Combustion (This is Reference Temperature) ** F 12 Temperature of fuel F 13 Gas Temp. Leaving (Boiler)(Econ.)(Air Htr.) F 14 Gas Temp. Entering AH (If conditions to be corrected to guarantee) F Coal as fired 15 Moisture % wt 16 Vol Matter % wt 17 Fixed Carbon % wt 18 Ash % wt 19 Btu per lb AS FIRED % wt 20 Ash Soft Temp. ASTM Method % wt Coal or Oil as fired ultimate Analysis 21 Carbon % wt 22 Hydrogen % wt 23 Oxygen % wt 24 Nitrogen % wt 25 Sulphur % wt 26 Ash % wt 27 Moisture % wt Oil 28 Flash Point F 29 Sp.Gravity Deg. API 30 Viscosity at SSU* Burner at SSF* 31 Total Hydrogen % wt 32 Btu per lb Gas 33 CO % vol 34 CH4 Methane % vol 35 C2H2 Acetylene % vol 36 C2H4 Ethylene % vol 37 C2H6 Ethane % vol 38 H2S % vol 39 CO2 % vol 40 H2 Hydrogen % vol Coal Pulverization 41 Grindability Index * 42 Fineness % Thru 50 M* 43 Fineness % Thru 200 M* 44 45 Density 68 F atm.Press. 46 Btu Per cu ft 47 Btu Per lb Flue Gas Analysis (Boiler)(Econ)(Air Heater) Outlet 48 CO2 % vol 49 O2 % vol 50 CO % vol 51 N2 (by Difference) % vol 52 Excess Air % vol 4,1 with sorbent Table 13 B Combustion Calculations - Btu Method (with Sorbent) INPUT CONDITIONS - BY TEST OR SPECIFICATION INPUT - Bituminous coal 1 Exess air at burner/leaving boiler/econ. % by weight 15 Ultimate Analysis 16 Theo Air lb/100 lb fuel 17 H2O. Lb/100 lb fuel tulisan merah = inputan 2 Entering air temperature, F Constituent % by weight K1 [15] X K1 K2 [15] x K2 tulisan hitam = output 3 Reference temperature, F A C 0.00 4 Fuel temperature, F B S 0.00 5 Air temperature leaving air heater, F C H2 0.00 0.00 6 Flue gas temperature leaving (excluding leakage).F D H2O 0.00 7 Moisture in air. Lb/lb dry air E N2 8 Additional moisture. Lb/100 lb fuel F O2 -4.32 0.00 9 Residue leaving boiler/economizer. % Total G Ash 10 Output. 1.000.000 Btu/h H Total 0 Air 0.00 H2O 0.00 Corrections for sorbent (from table 14 if used) 11 Additional theoritical air. Lb/10.000 Btu Table 14, item [21] 18 Higher heating value (HHV). Btu/lb fuel 0.00 12 CO2 from sorbent. Lb/10.000 Btu Table 14, Item [19] 19 Unburned carbon.loss % fuel input 13 H2O from sorbent, lb/10.000 Btu Table 14, Item [20] 20 Theoretica air. Lb/10.000 Btu [16H] x 100 / [18] ERROR:#DIV/0! 14 Spent sorbent. Lb/10.000 Btu Table 14, Item [24] 21 Unburned carbon. % of fuel [19] x [18] / 14.500 0.00 22 Theoritical air (corected). Lb/10.000 Btu [20] - [21] x 1151 / [18] + [11] ERROR:#DIV/0! 23 Residue from fuel. Lb/10.000 Btu ([15G] + [21]) x 100 / [18] ERROR:#DIV/0! 24 Total residue. Lb/10.000 Btu [23] + [14] ERROR:#DIV/0! A At burners B Infiltration C Leaving Furnace D Leaving Blr/Econ 25 Excess air. % by weight 26 Dry air. Lb/10.000 Btu (1 + [25] / 100) x [22] ERROR:#DIV/0! ERROR:#DIV/0! 27 H2O from air. Lb/10.000 Btu [26] x [7] ERROR:#DIV/0! ERROR:#DIV/0! 28 Additional moisture. Lb/100 lb Btu [8] x 100 / [18] ERROR:#DIV/0! ERROR:#DIV/0! 29 H2O from fuel. Lb/10.000 Btu [17H] X 100 / [18] ERROR:#DIV/0! ERROR:#DIV/0! 30 Wet gas from fuel. Lb/10.000 Btu (100 - [15G] - [21]) x 100 / [18] ERROR:#DIV/0! ERROR:#DIV/0! 31 CO2 from sorbent. Lb/10.000 Btu [12] 0.00 0.00 32 H2O from sorbent. Lb/10.000 Btu [13] 0.000 0.00 0.000 0.00 33 Total wet gas. from Lb/10.000 Btu Summation [26] thrugh [32] ERROR:#DIV/0! ERROR:#DIV/0! 34 Water in wet gas. Lb/10.000 Btu Summation [27] + [28] + [29] + [32] ERROR:#DIV/0! ERROR:#DIV/0! ERROR:#DIV/0! ERROR:#DIV/0! 35 Dry gas. Lb/10.000 Btu [33] - [34] ERROR:#DIV/0! SkyNET: SkyNET: ERROR:#DIV/0! 36 H2O in gas. % by weight [100] x [34] / [33] ERROR:#DIV/0! ERROR:#DIV/0! 37 Residue. % by weight [9] x [24] / [33] ERROR:#DIV/0! ERROR:#DIV/0! EFFICIENCY CALCULATION. % Input from fuel Losses 38 Dry gas. % 0.0024 x [35D] x ([6] - [3]) ERROR:#DIV/0! 39 Water from Enthalpy of steam at 1 psi. T= [6] H1 = (3.958E-5 x T + 0.4329) x T + 1062.2 1,062.2 40 fuel as-fired Enthalpy of water at 1 T= [3] H2 = [3] - 32 -32.0 41 % [29]x([39] - [40]) / 100 ERROR:#DIV/0! 42 Moisture in air. % 0.0045 x [27D] x ([6] - [3]) ERROR:#DIV/0! 43 Unburned carbon. % [19] or [21] x 14.500 / [18] ERROR:#DIV/0! 44 Radiation and convection. % ABMA curve. Chapter 22 45 Unaccounted for and manufactures margin. % 46 Sorbent net losses. % if sorbent is used From Table 14 Item [41] 47 Summation of losses. % Summation [38] through [46] ERROR:#DIV/0! Credits 48 Heat in dry air. % 0.0024 x [26D] x ([2] - [3]) ERROR:#DIV/0! 49 Heat in moisture in air. % 0.0045 x [27D] x ([6] - [3]) ERROR:#DIV/0! 50 Sensible heat in fuel. % (H at T[4] - H at T [3]) x 100 / [18] 51 Others. % 52 Summation of credits. % Summation [48] through [51] ERROR:#DIV/0! 53 Efficiency. % 100 - [47] + [52] ERROR:#DIV/0! KEY PERFORMANCE PARAMETERS Leaving Furnace Leaving Blr / Econ 54 Input from fuel. 1.000.000 Btu/h 100 x [10] / [53] ERROR:#DIV/0! 55 Fuel rate. 1000 lb/h 1000 x [54] / [18] ERROR:#DIV/0! 56 Wet gas weight. 1000 lb/h [54] x [33] / 10 ERROR:#DIV/0! ERROR:#DIV/0! 57 Air to burner (wet). Lb/10.000 Btu (1 + [7]) x (1 + [25A] / 100) X [22] ERROR:#DIV/0! 58 Air to burner (wet). 1000 lb/h [54] x [57] / 10 ERROR:#DIV/0! 59 Heat available. 1.000.000 Btu/h [54] x ([18] - 10.30 x [17H]) / [18] - 0.005 H, 66 O Btu/h x ([44] + [45] + H2 at T[5] x [57] / 10.000 ERROR:#DIV/0! 60 Heat available/lb wet gas. Btu/lb 1000 x [59] / [56] ERROR:#DIV/0! 61 Adiabatic flame temperature. F From Fig. 3 at H = [60]. % H2O = [36] inputan 2 Inputan untuk Boiler Test eficiency berdasar PTC 4,1 with sorbent No Data yang harus diinput Nilai Satuan 1 Exess air at burner/leaving boiler/econ. % by weight 2 Entering air temperature F 3 Reference temperature F 4 Fuel temperature F 5 Air temperature leaving air heater F 6 Flue gas temperature leaving (excluding leakage) F 7 Moisture in air Lb/lb dry air 8 Additional moisture. Lb/100 lb fuel 9 Residue leaving boiler/economizer % Total 10 Output per 1.000.000 Btu/h Ultimate Analysis 11 C % weight 12 S % weight 13 H2 % weight 14 H2O % weight 15 N2 % weight 16 O2 % weight 17 Ash % weight Theoritical Air needed 18 C /100 lb fuel 19 S /100 lb fuel 20 H2 /100 lb fuel 21 O2 /100 lb fuel H2O formed 22 H2 /100 lb fuel 23 H2O /100 lb fuel Corrections for sorbent (from table 14 if used) 24 Additional theoritical air Lb/10.000 Btu 25 CO2 from sorbent Lb/10.000 Btu 26 H2O from sorbent Lb/10.000 Btu 27 Spent sorbent Lb/10.000 Btu 28 Unburned carbon loss % fuel input 29 Excess air at burner % by weight 30 Excess air at infiltration % by weight 31 Excess air leaving furnace % by weight 32 Excess air leaving Boiler/Economizer % by weight 33 Radiation and convection % 34 Unaccounted for and manufactures margin % 35 Sorbent net losses %