脱硫设计计算方法.ppt

* * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * 吸收塔尺寸 烟气流量 SO2浓度 SO2-脱硫率 液气比: L/G = 12 [l/Am3] at absorber outlet (假定) 吸收塔循环浆液流量及每泵的流量 Absorber temperature = 48 [°C] 喷淋层数 (pumps) = 3 吸收塔尺寸 吸收塔直径 吸收塔烟气流速w = 3,7 [m/s] (assumption) 吸收塔循环区体积 循环浆液停留时间 t = 4,3 min (assumption) 吸收塔尺寸 吸收塔循环浆液区高度 Sump height 11,9 [m] Height till flue gas duct 1,5 [m] Flue gas duct height 4,0 [m] Height to first spray bank (from flue gas duct) 2,5 [m] Spraying banks: 2x1,5 [m] 3,0 [m] Height till mist eliminator 1,3 [m] Height of two stage droplet separators 2,5 [m] Height flue gas outlet duct 3,0 [m] Sum 29,7 [m] Total absorber height: H = 30 [m] 吸收塔尺寸 增压风机和循环泵的能耗 增压风机 吸收塔压损 (assumption) 10 [mbar] GGH压损 12 [mbar] 烟道压损 7 [mbar] 总压损 29 [mbar] Specific flue gas transport work For booster fan with 85 [%] effectiveness 功率消耗 Pump efficiency = 0,89 Volume flow (pump) = 5.300 [m3/h] Liquid level = 11,9 [m] Geod. height = 1,5 [m] + 4,0 [m] + 2,5 [m] + 1,5 [m] = 9,5 [m] Pressure at nozzles = 10 [m] ~ (1 [bar]) Pressure height pipes = 3 [m] sum = 22,5 [m] 增压风机和循环泵的能耗 中间层泵的能耗  三层泵的总能耗 增压风机和循环泵的能耗 烟道尺寸 净烟气烟道直径 Flue gas velocity w = 18 [m/s] (assumption) Saturated clean gas 原烟气烟道直径 管道计算 1) 石灰石浆液输送管 Particle size limestone =90 [%] ≤ 44 μm d50 ~ 15 μm Concentration 30 [%] total solids amount Transport velocity ≥ 6 x settling velocity Normally wtransport ~2,5 [m/s] Volume flow suspension = 8 [m3/h] 石灰石浆液输送管直径 石灰石浆液循环管直径 Volume flow circulation 2·Vsuspension (Absorber) 管道计算 2) 石膏浆液管径 Particle size gypsum d50 = 35 – 50 μm Transport velocity ≥ 6 x setting velocity Normally wtransport ~2,5 [m/s] 至旋流器石膏浆液管径 管道计算 氧化风计算 强制氧化 SO2 + H2O → HSO3- + H+ HSO3- + ? O2 → SO42-+H+ 1 mol SO2 needs ? mol O2 1 kg SO2 needs 32:2/64 kg O2 Stoichiometric factor for O2-absorption in absorber sump ~2,5 → specific weight O2: → O2体积: →空气体积: 氧化风计算 氧化风压头