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• W249948496 abstract "A time-averaged simulation approach is applied to a 135 MWe circulating fluidized bed combustor located in Ruzhou, China, in which also measurements were carried out. The simulation results show a vertical solids distribution typical for a CFB. Gas composition profiles show plausible but not fully correct distributions of oxygen and combustion products inside the furnace. INTRODUCTION Dense gas-solid flows are usually computed as timedependent requiring a small time step and a fine mesh which lead to time-consuming simulations. To reduce computing time, Taivassalo & al. (1) introduced a timeaveraged CFD model and in Taivassalo & al. (2), the approach was applied on CFB combustion in Chalmers 12 MW boiler. In addition to hydrodynamics, models for heat transfer and chemistry, including homogeneous and heterogeneous reaction mechanisms, were included in the modeling. The behavior of fuel particles was simulated with a Lagrangian approach. The time-averaged simulation approach is applied to a 135 MWe circulating fluidized bed combustor located in Ruzhou, China, to examine how the modeling approach behaves in a commercial scale CFB. A measurement campaign was carried out at 120 MWe load. In the paper, results from the simulations are presented and compared with measurement data, including pressure and temperature distributions and gas composition data. MEASUREMENTS AND SIMULATION SETUP The combustion chamber geometry of the Ruzhou power plant is shown in Figure 1 in the simplified form in which it is described in the CFD simulation. The conical bottom section of the furnace is refractory lined while other walls are membrane walls. The figure also shows the six hanging super heaters and four re-heaters in the upper part of the furnace. In the middle of the furnace there is a membrane wall that to a large extent splits the furnace in two sections. This allows flexible Figure 1. Boiler geometry furnace operation. In the case measured and simulated in the present work, more fuel and secondary air was fed to one side of the furnace. In the boiler, coal is fed through six coal feeders located on the front wall. Secondary air enters from two levels at the front and back walls and some air also enters from the sides of the furnace from the four ash coolers located next to the corners of the furnace. The furnace is equipped with two cyclones, of which only the exit and return channels, shown in the picture, are included in the simulated domain. Primary and secondary air flows into the furnace and coal feed rates are listed in Table 1. The primary air flow is 41% of the total air flow, which in this geometry results in a relatively low primary fluidization velocity (1.96 m/s at assumed 800 °C temperature). The total coal feed rate is adjusted on basis of the oxygen balance based on the measured O2 concentration in the backpass. Table 1. Air and fuel flow rates. Air flow Primary To coal feeders To ash coolers To loop seal Upper secondary Lower secondary Left Right Left Right Left Right kg/s 46.5 4.7 10.7 0.34 0.35 21.7 9.2 19.1 11.0 Fuel flow Feeder 1 Feeder 2 Feeder 3 Feeder 4 Feeder 5 Feeder 6 kg/s 6.3 7.9 8.1 7.9 4.0 3.0 The fuel used in the experiments was a local high ash coal. Its size distribution and primary fragmentation tendency were measured. The initial size distribution and the distribution after primary fragmentation, which was used as an input to the simulation, are shown in Table 2. Table 2. Particle size distribution of coal before and after primary fragmentation. Size, mm 0.0 0.5 0.5 – 1.0 1.0 – 2.0 2.0 3.2 3.2 – 6.0 > 6.0 Before, % 28.7 13.9 25.1 15.2 10.1 7.0 After, % 31.2 16.2 26.3 11.1 8.5 6.7 The chemical composition of the fuel is listed in Table 3. The heating value of the fuel is 7.7 MJ/kg (a.r.). Table 3. Fuel analysis Volatiles [wt% daf] Proximate [wt% a.r.] Ultimate [wt% daf] Comb. Ash Moist. C H O S N 41.7 32.6 62.6 4.8 56.9 7.7 32.1 1.8 1.6 Pressure and temperature profiles, flue gas composition and heat exchanger data were collected during the experiment from the control system. A bottom ash sample was taken for analysis of particle size distribution and the amount of unburned in each size fraction. Additional measurements were carried out at four distances from the wall through four measurement ports on the right side wall of the furnace. The first measurement location was at 17.9 m height, the second at 27.4 m height, the third in the cyclone inlet channel at 30.6 m height and the fourth at cyclone outlet. In addition to measurements of temperature and gas composition, a suction probe was used to take samples of the solids. The measurements were conducted in between normal power plant operation so that the time the power plant was kept at the studied condition was only a few hours. Thus the bed inventory and particle size distribution differ from what would prevail at steady state." @default.
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• W249948496 date "2013-01-01" @default.
• W249948496 modified "2023-09-25" @default.
• W249948496 title "Time-averaged simulation of the furnace of a commercial CFB boiler" @default.
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