Epstein N., Grace J.R. Spouted and Spout-Fluid Beds: Fundamentals and Applications
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Hydrodynamics of spout-fluid beds 117
65
60
55
50
0
0.25
0.32
0.46
45
40
35
30
25
20
0.1 0.2 0.3 0.4
P (MPa)
U
a
/U
mf
u
msi
(m/s)
Figure 6.16. Effect of pressure on minimum spouting velocity
45
(D = 0.1 m, D
i
=0.01 m, θ =60
◦
,
d
p
= 2.3 mm, ρ
p
= 1330 kg/m
3
, H
0
/D = 1.5).
1.0
0.8
0.6
0.4
0.2
Spout-fluid bed by Zhong et al.
45
0.0
0.0 0.2
P = 0.1 MPa
P = 0.1 MPa
P = 0.24 MPa
P = 0.35 MPa
P = 0.2 MPa
P = 0.3 MPa
P = 0.4 MPa
0.4 0.6
Dimensionless vertical level, z/H
(P – P
H
)/(–ΔP)
0.8 1.0
UBC spouted bed
46
Figure 6.17. Effect of pressure on axial dimensionless pressure drop
45, 46
(D = 100 mm, D
i
= 10
mm, θ = 60
◦
, d
p
= 2.3 mm, ρ
p
= 1330 kg/m
3
, H
0
/D
0
= 3.0, U
s
/U
ms
= 1.35, U
a
/U
mf
= 0.6)
45
;
(D
0
= 76.2 mm, D
i
= 9.5 mm, θ = 60
◦
, d
p
= 1.09 mm, ρ
p
= 2445 kg/m
3
, H
0
/D = 1.78,
U
s
/U
ms
= 1.2).
46
6.1.9 Hydrodynamics at elevated pressures and temperatures
Increasing the pressure leads to decreases in both minimum spouting velocity (Fig-
ure 6.16) and spout-fluidizing velocity.
45
Pressure increases also cause an increase in
fountain height. As for the conventional spouted bed tested by He et al.,
46
the axial
pressure profile in a spout-fluid bed is insensitive to changes in mean pressure
45
(see Figure 6.17), whereas the amplitude of pressure fluctuations is reduced at
elevated pressures. As shown in Figure 6.18, the overall extent of the stable flow
118 Wenqi Zhong, Baosheng Jin, Mingyao Zhang, and Rui Xiao
2.4
2.0
1.6
1.2
0.8
0.4
0.0
0.0
(a)
0.4 0.8 1.2 1.6 2.0 2.4
SA
SF
JFS
FB
Q
s
/Q
mf
Q
a
/Q
mf
JFB
2.4
2.0
1.6
1.2
0.8
0.4
0.0
0.0 0.4 0.8 1.2 1.6 2.0 2.4
SA
SF
JFS
JFB
FB
Q
s
/Q
mf
Q
a
/Q
mf
(b)
Figure 6.18. Typical flow pattern map at various operating pressures
47
(D = 0.1 m, D
i
= 0.01 m,
θ = 60
◦
, d
p
= 2.3 mm, ρ
p
= 1330 kg/m
3
, H
0
/D = 2.0): (a) 0.1 MPa; (b) 0.3 MPa.
regions – that is, JFB, SA, and SF ranges – becomes larger when the bed pressure
is increased.
47
For l arge particles, the minimum spouting velocity generally increases with increasing
temperature, whereas for small particles it decreases. Auxiliary air has more influence on
the minimum spouting velocity at elevated temperature than at room temperature.
48
Each
of the flow regimes observed at low temperatures can also occur at high temperatures.
However, high temperatures tend to shift the behavior to less stable flow regimes –
pulsatory spouting, submerged jets, and slugging are more likely to occur at high
temperatures than at room temperature.
49
Hydrodynamics of spout-fluid beds 119
(a) DEM
(b) Eulerian
(c) Experiment
Figure 6.19. Typical simulated flow patterns compared with experiment
53
(A = 0.3 m × 0.03 m,
A
i
= 0.03 m × 0.03 m, θ = 60
◦
, H
0
= 500 mm, d
p
= 2.8 mm, ρ
p
= 1020 kg/m
3
, U
s
/U
ms
= 0.76,
U
a
/U
mf
= 0.78).
6.1.10 Numerical simulation of hydrodynamics
Two kinds of CFD models – Eulerian-Lagrangian
50–54
and Eulerian-Eulerian
55,56
– have been developed to predict the hydrodynamics of spout-fluid beds (see Chap-
ter 4). These models can be used to predict the gas-solid flow regimes (see Figure 6.19).
They may also provide information that is very difficult to obtain experimentally. For
example, DEM simulation shows that the drag force dominates the particle motion in
the jet region, whereas interparticle contact forces dominate the particle motion in the
dense annular region, especially near the wall.
54
Eulerian simulation shows that particle
velocities and concentrations at high temperature and pressure behave in similar manners
to those at ambient pressure and temperature.
56
Eulerian simulations are useful to pre-
dict the hydrodynamics of large-scale spout-fluid beds because of limited computational
requirements (CPU and memory).
In addition to the simulation of hydrodynamics, the kinetic theory of granular flow,
based on the Eulerian method and involving mass transfer, momentum transfer, heat
transfer, and chemical reaction, has been demonstrated to be effective in analyzing and
optimizing energy-conversion processes in spout-fluid beds, such as for pressurized coal
gasification.
57,58
6.2 Typical applications
6.2.1 Combustion
Researchers at the University of British Columbia have investigated the combustion
of low-grade solid fuels in spout-fluid beds
49,59,60
in a 0.15-m diameter half-column
120 Wenqi Zhong, Baosheng Jin, Mingyao Zhang, and Rui Xiao
Viewing
ports
Cyclone
To stack
Water
Heat
exchanger
Condensate
Gas sample
Water
Ash
receivers
Tan k
Combustor
Fuel hopper
Rotary
feeder
Propane burner
Air
Propane
Nitrogen or air
Air
Dryer
Filter
O
2
monitor
Figure 6.20. Schematic of spout-fluid bed combustion system at University of British Columbia.
60
and a 0.3-m-diameter cylindrical spout-fluid bed combustor. Three bituminous coals or
coal rejects of differing ash contents were burned in the spout-fluid bed to compare
the relative throughput capacity and combustion efficiency of spouted and fluidized
beds. A schematic of the 0.3-m-diameter spout-fluid bed combustion system is shown
in Figure 6.20. Experimental results indicate that the spout-fluid bed gave somewhat
higher combustion efficiencies at low temperatures, greater temperature uniformity, and
improved bed-to-surface heat transfer compared with the other modes of operation.
60
The Asian Institute of Technology in Thailand has also carried out combustion of coal
and carbon in spouted and spout-fluid beds to test the use of Thai lignite and pyrolyzed
electrode carbon as fuels.
61
Mindanao Polytechnic State College of the Philippines
applied different configurations of “spout-fluidized” beds, namely, a multiple-spouted
and a spout-fluid bed, to combustion of rice husk fuel.
62
The spout-fluidized bed
combustor body was made of 3.4-mm-thick mild steel with a cross-sectional area of
0.7 m × 0.7 m. The emission of pollutants and the feasibility of burning rice husk
in these different configurations at different excess airflow rates, primary-to-secondary
air ratios, and method of feeding fuel were tested. The work showed that spout-fluid
bed combustion could be a suitable technology for converting a wide range of agricul-
tural residues into energy because of its fuel flexibility, low emission of pollutants, low
operating temperature, and isothermal operating conditions.
6.2.2 Gasification
The British Coal Corporation developed a spout-fluid bed gasification process at its Coal
Research Establishment for the production of low-calorific-value fuel gas.
63
The work
Hydrodynamics of spout-fluid beds 121
Coal and
limestone
Coal and
limestone
Gas
cooler
Cyclone
Gasifier
Loop
seal
Steam
Fluid gas
Steam
Mixer
Startup
burner
Ash
Ash
Air
preheater
Ash lock
hopper
Ash lock
hopper
Lock
hopper
Lock
hopper
Lock
hopper
Lock
hopper
Primary
cyclone
Secondary
cyclone
Air
Sprayer
Muffler
Gas burner
Air
Injector
Star
feeder
Air
Injector
Water-cooled
screw feeder
Slag lock
hopper
Slag
Figure 6.21. Pilot-scale pressurized spout-fluid bed coal partial gasification system operated by
the Southeast University of China.
65
provided a flexible low-cost process for onsite production of industrial fuel gas (gross
calorific value ∼4MJ/m
3
) as an integral component of a high-efficiency (conversion
efficiency up to 95%), low-cost electric power generation system, known as the British
Coal topping cycle.
Southeast University of China constructed spout-fluid bed pressurized coal partial
gasification-based advanced pressurized fluidized bed combustion-combined cycle sys-
tems for low rank coals. They built 0.08-m-, 0.1-m-, and 0.45-m-diameter cylindrical
pressurized spout-fluid bed gasifiers.
64–66
A schematic of the pilot scale spout-fluid bed
coal partial gasification system is shown in Figure 6.21. For a deep-bed gasification
process (H
0
/D up to 9), the temperature in the dense bed was uniform (variation along
the bed height <30
◦
C), and the gas generated had a heating value up to 4.8 MJ/Nm
3
.
The product gas could burn steadily in the combustor at a temperature of 1100
◦
Cto
1150
◦
C, allowing a gas turbine inlet temperature range of 1100
◦
C to 1300
◦
C without
adding auxiliary fuels.
The Asian Institute of Technology of Thailand presented a feasible option for
converting municipal solid waste (MSW) to useful energy based on spout-fluid bed
gasification.
67
The gasifier was 0.45 m square in cross-section with a height of 3 m
from the distributor plate to the top of the enlargement zone. The producer gas higher
heating value (HHV) was in a narrow range of 4.4 to 4.6 MJ/Nm
3
. The gasification effi-
ciency and carbon conversion efficiency were raised, respectively, from 35.8 percent and
55.3 percent (25% of stoichiometric air at base case) to 39.0 percent and 65.3 percent
(25% of stoichiometric air without secondary air supply). The range of compositions
were CO 14.8%∼18.5%, H
2
7.1%∼9.7%, CH
4
2.8%∼3.1%, and CO
2
16.6%∼18.5%.
122 Wenqi Zhong, Baosheng Jin, Mingyao Zhang, and Rui Xiao
Producer gas
outlet
Producer gas
sampling
outlet
Cyclone
separator
Return leg
Secondary air inlet
Bed zone
Distributor plate
Fluidizing air inlet
Spouting air inlet
Water
jacket
Screw
feeder
Fuel hopper
RDF
Enlargement
zone
Partial
oxidation
zone
Figure 6.22. Spout-fluid bed gasification setup for municipal solid waste.
67
The producer gas could be used for direct heat application or industrial steam production
(Figure 6.22).
6.2.3 Other applications
Other applications, such as biomass gasification,
68
drying,
69
and production of gran-
ules or particles through granulation,
70
are under development. In addition, there are
successful applications of spout-fluid beds with draft tube, such as for dry premixing
of cementitious materials and sand
71,72
and for drying of agricultural products,
73
as
covered i n other chapters.
6.3 Closing remarks
As a modified gas-solid contacting technique, the spout-fluid bed reduces some of the
limitations of both conventional spouting and gas-fluidization. However, the hydro-
dynamics of spout-fluid beds are more complex than those for conventional spouted
beds. Hydrodynamic properties and scaleup cannot, at this stage, be predicted with
confidence. This chapter summarizes information on the fundamentals and applications
of spout-fluid beds without a draft tube, based on the limited work reported this far.
More experimental and theoretical work is required to more fully understand and apply
spout-fluid beds.
Hydrodynamics of spout-fluid beds 123
Chapter-specific nomenclature
D
ref
reference diameter
18
of column, m
H
msf
maximum spoutable height of spout-fluid bed, m
H
ms
maximum spoutable height of spouted bed, m
L
j
jet penetration depth, m
Q
s
volumetric flow rate of entering spouting gas, m
3
/s
Q
t
total gas volumetric flow rate, m
3
/s
U
a
superficial velocity of entering auxiliary gas, based on D,m/s
U
msf
superficial gas velocity at minimum spout-fluidizing, m/s
U
s
superficial velocity of entering spouting gas, based on D,m/s
Greek letters
ϕ hole orientation angle
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