Post on 27-Jan-2022
OXYCOAL-AC
1
Numerical Simulation of a 1200 MWth
Pulverised Fuel Oxy-firing Furnace
Jens Erfurth
Dobrin Toporov, Malte Förster, Reinhold Kneer
Institute of Heat
and Mass
Transfer
RWTH Aachen University
CCT2009, Dresden, 18-21 May 2009
OXYCOAL-AC
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0,6
0,7
0,8
0,9
1
1,1
1,2
19 21 23 25 27 29 31 33O2, %
Q/Q
_AIR AIR
OXY21wetOXY21dryOXY27wetOXY30dry
Overview
23.8
% 28.6
%
ConclusionsResults
ModellingMotivation
0 1000 2000 3000 4000 5000 6000 7000 80000
0.5
1a) Transmissivities of Bands m
Wavenumber ν [1/cm]
0 1000 2000 3000 4000 5000 6000 7000 80000
0.5
1b) Total Absorptivities
Wavenumber ν [1/cm]
0 1000 2000 3000 4000 5000 6000 7000 80000
0.5
1c) Normalised Planck Distribution
Wavenumber ν [1/cm]
I ν/I ν
,max
Tgas = 1810 KT = 1000 K
CO2
H2OCO
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Motivation: the
Case
for
CCS Retrofit
■
300 GW of capacity will have to be installed in the EU-25 until 2020.
■
Coal plants built before CCS is available (ca. 2020) pose risk of „carbon lock-in“.
■
Plants built between now and then could be retrofitted for CCS
Sources: VGB Powertech, EU Energy and Transport Outlook
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Oxyfuel Retrofit
Can a boiler originally designed for air operation be operated in oxy-firing at the same thermal load?
■
Criteria:•
Burnout
•
Heat transfer
•
Furnace exit temperature
•
Corrosion in the furnace
■
Parameters available to meet these requirements:•
Oxygen concentration
•
Water content of oxidiser (wet or dry recycling)
•
…
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Previous Experimental Work in Aachen■
Oxycoal test facility with 120 kWth
■
Oxycoal
swirl burners
•
Able to operate within wide range of oxygen O2
content and in air
•
Measures for oxycoal swirl flame stabilisation derived
•
Design of industrial burners based on these measures
Experiments CFD Simulations
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■
Heterogeneous and homogeneous reactions are modelled as User Defined Functions (UDFs)
■
Changes in the CFD model for oxy-firing:•
Modelling of heterogeneous reactions:
Cs
+ 0.5 O2
→ CO
Oxidation, exothermal
Cs
+ CO2
→ 2 CO
BoudouardGasification, endothermal
Cs
+ H2
O → CO + H2
Water Gas Reaction
•
Adjustment of radiation model
CFD Models
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Exponential Wide
Band Model (EWBM)*
EWBM
COp2H Op
2COpL tp0,mλBand locations T
mτ mλΔ
lk for
10 spectral
regions
l
Algorithm
11 single
Bands m (CO2
, H2
O, CO)
*Edwards D. K., Advances in Heat Transfer, vol.12, 1976
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Results
of EWBM
Example:
L = 0.1 m
T = 1800 K
Spectral
absorptivities of flue
gas
0 1000 2000 3000 4000 5000 6000 7000 80000
0.5
1
Wavenumber [1/cm]
0 1000 2000 3000 4000 5000 6000 7000 80000
0.5
1
Wavenumber [1/cm]
Air combustion:
Oxyfuel combustion, wet
recycling:
α
α
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Furnace designed for Air firing■
Thermal power: 1210 MW (RPP NRW)
■
18 burners → 70 MW each (λ
= 0.95)
•
Burner geometry designed based on criteria developed by the authors*
■
12 OFA nozzles (λtot
= 1.15)
■
Fired by South African hard coal
■
5 Cases:
•
AIR
•
Same oxygen: OXY21dry, OXY21wet
•
Same temperature:
OXY30dry,
OXY27wet
* Toporov et al, CCT 2007
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Temperature
Fields, dry
Recycling
T [K]
2300
300AIR OXY21dry OXY30dry
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Temperature
Fields, wet
Recycling
T [K]
2300
300AIR OXY21wet OXY27wet
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CO Source
from
Particle
Oxidation, dry
Recycling
log SCO[kg/m3s]
3
1e-4AIR OXY21dry OXY30dry
Cs
+ 0.5 O2
→ CO
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CO Source
from
Particle
Oxidation, wet
Recycling
AIR OXY21wet OXY27wet
Cs
+ 0.5 O2
→ CO
log SCO[kg/m3s]
3
1e-4
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CO Source
from
Particle
Gasification, dry
Recycling
AIR OXY21dry OXY30dry
Cs
+ CO2
→ 2 CO
and Cs
+ H2
O → CO + H2
log SCO[kg/m3s]
0.5
1e-4
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CO Source
from
Particle
Gasification, wet
Recycling
AIR OXY21wet OXY27wet
log SCO[kg/m3s]
0.5
1e-4
Cs
+ CO2
→ 2 CO
and Cs
+ H2
O → CO + H2
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Surface
Incident
Radiation, dry
Recycling
Q´´[kW/m2]
500
0AIR OXY21dry OXY30dry
Locally
increased
wall temperature
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Surface
Incident
Radiation, wet
Recycling
500
0AIR OXY21wet OXY27wet
Q´´[kW/m2]
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Comparison: radiative
Heat
Transfer in Furnace
0,6
0,7
0,8
0,9
1
1,1
1,2
19 21 23 25 27 29 31 33O2, %
Q/Q
_AIR AIR
OXY21wetOXY21dryOXY27wetOXY30dry
1.2
1.1
0.9
0.8
0.7
0.628.6 %23.8 %
integrated
over
furnace
walls
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0,85
0,9
0,95
1
1,05
0,9 0,95 1 1,05 1,1 1,15 1,2 1,25
H/H_AIR,exit
T/T_
AIR
,exi
tAIROXY21wetOXY21dryOXY27wetOXY30dry
1.0
5
0.9
5
0.
9
0.8
5
Comparison: Temperature* and Enthalpy
Flow
* averaged
at furnace
exit
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Heat
Transfer in the
convective
Section
■
Theoretical
considerations:
TubeAsh
Layer
Incident
Radiation
Emitted
Radiation
Tsurface
Tsteam Tsurface
Tgas
EWBM (Gas Radiation
only)
h
d
Leff
, αsurface
, εgas
εash
htotal
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Heat
Transfer: Differences
Air -
Oxy-firing
■
Energy balance
at pipe
surface:
800steamT K=
30 , 30
,
( )( )
OXY dry surface OXY dry steam
surface AIR steamAIR
Q T TT TQ
⋅
⋅
−Δ = =
−
261AIRWh
m K=
For OXY30dry
Leff
= 0.1 m Leff
= 1 m
Tgas
= 1000 K Δ
= 1.25 Δ
= 1.21
Tgas
= 1600 K Δ
= 1.25 Δ
= 1.23
30 266OXY dryWh
m K=
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Conclusions
■
CFD simulations
of a state
of the
art furnace
in air
and oxy-firing
of coal
were
conducted
using
a non-grey
implementation
of the
EWBM
■
Surface
incident
radiation
increases
relative to air…
•
…by
6 % for
dry
recycling
•
…by
14 % for
wet
recycling
■
In oxy-firing
gasification
gains
importance
•
Reason: abundance
of CO2
and water
vapour
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Conclusions: Retrofit
Criteria:
■
Burnout
can
be
achieved
■
Furnace
exit
temperature
below
ash
melting
point
■
Overall heat
transfer:
•
Similar
in furnace
for
OXY30dry
•
In convective
section: increase
by
20-25 % for
OXY30dry, but
particles
will dampen
this
effect.
■
Wall temperatures: care
must
be
taken
to ensure
corrosion
does
not
unduly
increase
?
?
••
•
?
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Acknowledgements
This work was conducted in the framework of the project OXYCOAL-AC and was funded by:
German Federal Ministry of Economics and
Technology
Ministry for Innovation, Science, Research and Technology of the State
of North Rhine-Westphalia
RWE Power
WS Wärmeprozesstechnik
Linde
MAN Turbo Hitachi Power Europe
E.ON Energie
OXYCOAL-AC
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Thank
you
for
your
attention
OXYCOAL-AC
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OXYCOAL-AC
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CFD Radiation
Modelling
in Coal Combustion
■
Radiation
Transport Equation
for
a given
wavelength
λ:
4
,4
''' 1( ) ( ) ( )4
PP s P i P
qdI Tk I k I I I dds π
σ σπ π π
⋅⎡ ⎤
= − + − − − Ω Φ Ω Ω⎢ ⎥⎣ ⎦
∫
Gas emission
and absorption
Particle
emission
and absorption
Particle
outscattering
and inscattering(Gas scattering
is
neglected)
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CFD Radiation
Modelling
in Coal Combustion
■
Radiation
Transport Equation
for
a given
wavelength:
■
Particle
emission
in a given
control
volume:
■
Particle
absorption
in a given
control
volume
:
■
Particle
Scattering: (homogeneous, isotropic)
4
,4
''' 1( ) ( ) ( )4
PP s P i P
qdI Tk I k I I I dds π
σ σπ π π
⋅⎡ ⎤
= − + − − − Ω Φ Ω Ω⎢ ⎥⎣ ⎦
∫
, 4, ,
1'''
NP n
P P n P nn
Aq T
Vε σ
⋅
=
=∑
,,
1
NP n
P P nn
Ak
Vε
=
=∑
, 0,6s Pσ = ( ) 1PΦ Ω =
(Sum
over
particles)
(Sum
over
particles)
OXYCOAL-AC
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CFD Radiation
Modelling
in Coal Combustion
■
Radiation
Transport Equation
for
a given
wavelength:
■
Particle
emission:
■
Particle
absorption:
■
Particle
Scattering: (homogeneous, isotropic)
4
,4
''' 1( ) ( ) ( )4
PP s P i P
qdI Tk I k I I I dds π
σ σπ π π
⋅⎡ ⎤
= − + − − − Ω Φ Ω Ω⎢ ⎥⎣ ⎦
∫
, 4, ,
1'''
NP n
P P n P nn
Aq T
Vε σ
⋅
=
=∑
,,
1
NP n
P P nn
Ak
Vε
=
=∑
2 2( , , , , , ) ?CO H O CO tk k T p p p pλ= =
Absorption coefficient
k:
, 0,6s Pσ = ( ) 1PΦ Ω =
OXYCOAL-AC
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CO Source
from
Particle
Oxidation, dry Recycling
SCO[kg/m3s]
≥
0.05
0AIR OXY21dry OXY30dry
Cs
+ 0.5 O2
→ CO
Same thermal load
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CO Source
from
Particle
Oxidation, wet Recycling
AIR OXY21wet OXY27wet
≥
0.05
0
Cs
+ 0.5 O2
→ CO
Same thermal load
SCO[kg/m3s]
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CO Source
from
Particle
Gasification, dry
Recycling
≥
0.05
0AIR OXY21dry OXY30dry
Cs
+ CO2
→ 2 CO
and Cs
+ H2
O → CO + H2
Same thermal load
SCO[kg/m3s]
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CO Source
from
Particle
Gasification, wet
Recycling
AIR OXY21wet OXY27wet
≥
0.05
0
Same thermal load
Cs
+ CO2
→ 2 CO
and Cs
+ H2
O → CO + H2
SCO[kg/m3s]
OXYCOAL-AC
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0,6
0,7
0,8
0,9
1
1,1
1,2
19 21 23 25 27 29 31 33O2, %
Q/Q
_AIR AIR
OXY21wetOXY21dryOXY27wetOXY30dryOXY238wetOXY286dry
Comparison: radiative
Heat
Transfer in Furnace
1.2
1.1
0.9
0.8
0.7
0.6