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Claus Riser Reactor Feed Stream Properties Used to Demonstrate the Effects of Backmixing in a Fast Fluidized CFB (P = 216.0 kPa, T = 539 K) aN ee Riser Reactor and Kaiser-201 Catalyst Properties for The Simulation of a Claus Riser Reactor with an Inlet Feed Given in Table 3

Table 3 Claus Riser Reactor Feed Stream Properties Used to Demonstrate the Effects of Backmixing in a Fast Fluidized CFB (P = 216.0 kPa, T = 539 K) aN ee Riser Reactor and Kaiser-201 Catalyst Properties for The Simulation of a Claus Riser Reactor with an Inlet Feed Given in Table 3

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Average Solids Fractions Determined Using The Fully Developec Zone Pressure Gradient Data of Rhodes et al. (1992), The “Plug Flow” Voidage, and Our Model a Average solids fraction determined using the pressure gradient. b Average solids fraction determined using Equation (1). c Average solids fraction determined using our model.
Average Solids Fractions Determined Using The Fully Developec Zone Pressure Gradient Data of Rhodes et al. (1992), The “Plug Flow” Voidage, and Our Model a Average solids fraction determined using the pressure gradient. b Average solids fraction determined using Equation (1). c Average solids fraction determined using our model.
Figure | —— Schematic diagram of our model for the fully devel- oped zone of a circulating fluidized bed riser reactor operating in the fast fluidized regime.
Figure | —— Schematic diagram of our model for the fully devel- oped zone of a circulating fluidized bed riser reactor operating in the fast fluidized regime.
The third equation comes from the following assumption of our model: The solids velocity at the wall is equal to the terminal velocity of a single particle relative to the gas velocity in the annulus. Therefore, with the upward direc- tion being positive, at r= R, The first two equations are derived from the fact that the solids mass flux and velocity at the radius of the core are, by definition, zero. That is, The parameters a, b, c, and d, as well as the gas velocity in the annulus (u,) and core (u is -) must be calculated. (The explanation of why Ugg and Uy, are included in the list of unknowns is forthcoming.) Therefore, six equations govern- ing the CFB system must be known.
The third equation comes from the following assumption of our model: The solids velocity at the wall is equal to the terminal velocity of a single particle relative to the gas velocity in the annulus. Therefore, with the upward direc- tion being positive, at r= R, The first two equations are derived from the fact that the solids mass flux and velocity at the radius of the core are, by definition, zero. That is, The parameters a, b, c, and d, as well as the gas velocity in the annulus (u,) and core (u is -) must be calculated. (The explanation of why Ugg and Uy, are included in the list of unknowns is forthcoming.) Therefore, six equations govern- ing the CFB system must be known.
Figure 2 — Comparison between the predicted (a = 3.14, b = —1.24) and measured solids mass flux profile. [Data of Rhodes et al. (1992); D, = 74.9 um, p, = 2456 kg/m, D = 0.305 m, L = 6.6 m, G, = 60 kg/m?-s, wu, =4 m/s).
Figure 2 — Comparison between the predicted (a = 3.14, b = —1.24) and measured solids mass flux profile. [Data of Rhodes et al. (1992); D, = 74.9 um, p, = 2456 kg/m, D = 0.305 m, L = 6.6 m, G, = 60 kg/m?-s, wu, =4 m/s).
Figure 3 — Comparison between the predicted (a = 4.20, b = 2.00) and measured solids mass flux profile. [Data of Rhodes et al. (1992); D, = 74.9 um, p, = 2456 kg/m}, D = 0.152 m, L = 6.2 m, G, = iit ke/m? ‘$, Uy = 5 m/s}.
Figure 3 — Comparison between the predicted (a = 4.20, b = 2.00) and measured solids mass flux profile. [Data of Rhodes et al. (1992); D, = 74.9 um, p, = 2456 kg/m}, D = 0.152 m, L = 6.2 m, G, = iit ke/m? ‘$, Uy = 5 m/s}.
Figure 4 — Comparison between the predicted (c = 8.95, d = 3.15) and measured solids velocity profile at 4.18 m. [Data of Miller and Gidaspow (1992); D = 75 wm, p, = 1654 kg/m}, R = 3.75 cm, L = 6.58 m, G, = 32.8 kg/m*-s, Ug = 2.89 m/s].
Figure 4 — Comparison between the predicted (c = 8.95, d = 3.15) and measured solids velocity profile at 4.18 m. [Data of Miller and Gidaspow (1992); D = 75 wm, p, = 1654 kg/m}, R = 3.75 cm, L = 6.58 m, G, = 32.8 kg/m*-s, Ug = 2.89 m/s].
Figure 5 ~~ Comparison between the predicted and measured voidage profile at 2.5 m. [Data of Pugsley (1995); D, = 208 um, p, = 2580 kg/m, R = 2.5 cm, L = 6.4 m, G, = 240 fo/m2-s, Ugg = 5 m/s].
Figure 5 ~~ Comparison between the predicted and measured voidage profile at 2.5 m. [Data of Pugsley (1995); D, = 208 um, p, = 2580 kg/m, R = 2.5 cm, L = 6.4 m, G, = 240 fo/m2-s, Ugg = 5 m/s].
Figure 6 —- Model predictions of axial HO concentration profiles for fast fluidized and plug flow reactors in a Claus plant (only the main Claus reaction).
Figure 6 —- Model predictions of axial HO concentration profiles for fast fluidized and plug flow reactors in a Claus plant (only the main Claus reaction).
Figure 7 — Model predictions of axial H,S concentration profiles for fast fluidized and plug flow reactors in a Claus plant (only the main Claus reaction).
Figure 7 — Model predictions of axial H,S concentration profiles for fast fluidized and plug flow reactors in a Claus plant (only the main Claus reaction).
Figure 9 — Model predictions of axial SO, concentration profiles for fast fluidized and plug flow reactors in a Claus plant (only the main Claus reaction).
Figure 9 — Model predictions of axial SO, concentration profiles for fast fluidized and plug flow reactors in a Claus plant (only the main Claus reaction).
evaluated at equilibrium. Note that ~7j,,, has units of mol/s-kg cat. The results of our calculations that give the hydrodynamics within the riser are presented in Table 5. The intrinsic rate expression for the main Claus reaction, Reaction 15, on the Kaiser 201 catalyst is given by the Liu II Model (Birkholz, 1987):
evaluated at equilibrium. Note that ~7j,,, has units of mol/s-kg cat. The results of our calculations that give the hydrodynamics within the riser are presented in Table 5. The intrinsic rate expression for the main Claus reaction, Reaction 15, on the Kaiser 201 catalyst is given by the Liu II Model (Birkholz, 1987):
Related topics:
Chemical EngineeringTwo Phase FlowFluidized Bed ReactorCirculating Fluidized Bed
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