Effektiv kraftvarme fra affaldsfraktioner - Energinet.dk

Test CFB 03/14A CFB 03/14B CFB 03/14B1 CFB 03/14B2
Fuel Packing material
ESR-mix ESR-mix ESR-mix
Bed material 1 S 50% P3 50 S 25 % P3 75 % S 25 % P3 75 S 25 % P3 75 %
%
%
Bed material feed rate, mg/s 0.8 1.3 1.3 1.3
T (riser bottom), o C 880 890 880 900
T (riser top), o C 870 900 880 910
Pressure, bar (abs) 1.1 1.1 1.1 1.1
Fuel moisture content, wt-% 8.1 5.5 5.5 5.5
Fuel feed rate, g/s
Gasification agents, g/s
13.8 7.3 8.6 7.0
- primary air 14.2 13.1 13.8 12.8
- secondary air + steam 2.4 4.2 3.3 5.0
Nitrogen feed rate, g/s 2 2.0 1.7 1.9 1.6
Air ratio 0.24 0.29 0.25 0.32
dp bed, mbar 50 49 52 48
Gas velocity (riser bottom) 2.9 3.1 3.1 3.1
m/s 3
Gas velocity (riser top) m/s 4 6.2 5.0 4.9 5.1
Gas flow rate, m 3 n/h (wet) 99 78 78 79
Dry gas composition, vol-%
CO 15.6 9.8 9.7 9.6
CO2 16.3 14.7 13.4 14.8
H2 13.8 9.6 9.5 9.6
N2(+Ar) 48.4 60.5 61.6 61.0
CH4 4.10 3.47 3.99 3.17
C2Hy 1.8 1.3 1.8 1.2
C3Hy - C5Hy 0.04 0.01 0.01 0.01
NH3 0.05 - - 0.70
H2S ppmvol - - - 60
HCl ppmvol - - - 4000
H2O in wet gas gas, vol-% 17 20 19 22
Tars + benzene, g/m 3 n 15.2 60 94.1 44.0
Tar yield, g/kg daf fuel 29.5 156 208 128
Carbon conversion, wt-%
to dry gas 88.3 71.9 62.1 74.9
to gas and tars 94.1 96.6 94.9 95.6
to gas and tars 5 93.3 93.8 92.6 92.7
Mass balance closures
C-balance 0.99 1.00 0.98 1.00
O-balance 1.01 0.94 0.88 0.93
Ash balance 0.95 1.02 1.07 0.98
1 P3=Limestone Parfil 3, S= silica sand
2 Total amount of nitrogen used as purging gas (in feeding and ash removal hoppers etc)
3 Based on air and steam flow rates, empty reactor diameter and actual p and T
4 Based on product gas flow rate, empty reactor diameter and actual p and T
5 Including limestone C in the input of carbon
Tabel 3.8: Driftsdata og resultater af forgasningsforsøg
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