Modelling of a chemical looping combustion system equipped with a

Engineering Conferences International
ECI Digital Archives
Fluidization XV
Proceedings
5-25-2016
Modelling of a chemical looping combustion
system equipped with a two- stage fuel reactor
Roberto Solimene
Istituto di Ricerche sulla Combustione, Consiglio Nazionale delle Ricerche, Italy., [email protected]
Antonio Coppola
Istituto di Ricerche sulla Combustione, Consiglio Nazionale delle Ricerche, Italy.
Piero Bareschino
Dipartimento di Ingegneria, Università degli Studi del Sannio, Italy.
Piero Salatino
Dipartimento di Ingegneria Chimica, dei Materiali e della Produzione Industriale, Università degli Studi di Napoli Federico II,
Italy
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Part of the Chemical Engineering Commons
Recommended Citation
Roberto Solimene, Antonio Coppola, Piero Bareschino, and Piero Salatino, "Modelling of a chemical looping combustion system
equipped with a two- stage fuel reactor" in "Fluidization XV", Jamal Chaouki, Ecole Polytechnique de Montreal, Canada Franco
Berruti, Wewstern University, Canada Xiaotao Bi, UBC, Canada Ray Cocco, PSRI Inc. USA Eds, ECI Symposium Series, (2016).
http://dc.engconfintl.org/fluidization_xv/112
This Abstract and Presentation is brought to you for free and open access by the Proceedings at ECI Digital Archives. It has been accepted for inclusion
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UniversitàdegliStudidelSannio
DipartimentodiIngegneria
UniversitàdegliStudidiNapoliFedericoII
DipartimentodiIngegneriaChimica,dei
MaterialiedellaProduzioneIndustriale
MODELLINGOFACHEMICALLOOPINGCOMBUSTIONSYSTEM
EQUIPPEDWITHATWO-STAGEFUELREACTOR
AntonioCoppola,RobertoSolimene
ConsiglioNazionale delle Ricerche, IRC– Napoli(Italy)
GiuseppeDiglio,PieroBareschino
Università degliStudidelSannio,DING – Benevento (Italy)
PieroSalatino
Università degliStudidiNapoliFederico II,DICMaPI- Napoli(Italy)
Fluidization XV– May 22-27,2016
ExploitingofCLOUeffectfor
combustionofthemost
difficultpartofthefuel:Char
Two-stage Fuel Reactor:
better utilization
of theoxygen carrier
ConversionofVM
usingtheresidual
oxidativepotential
oftheOC
RTDiscloserto
aplugflow
thanasinglestageFR
FluidizationXV– May22-27,2016
Literature
Most of numerical simulations of CLC in DIFB are focused only on
kinetic scheme
Whatyouneed?
An appropriate hydrodynamic model of the whole system in order to
point out “stable” operating conditions.
Aim ofthework
To develop a simple mathematical tool coupling a CLC reactive
scheme and a simple hydrodynamic model of a DIFB system.
FluidizationXV– May22-27,2016
1
• FRsplitintwozones:densezonebelowdilutedzone/FreeBoard (FB)
2
• DensezoneismodelledasaCSTR,whileFBismodelledasaPFR
3
• Instantaneousdevolatilization
4
• ARismodelledasCSTR(denseregime)orPFR(dilutedregime)
5
• Therateofheterogeneousreactionsisruledbychemicalkinetics
6
• Conversionisuniformthroughoutsolidparticles
7
• Conversionofoxygencarrierandcharintheairreactoriscomplete.
FluidizationXV– May22-27,2016
𝑚*+, = 𝑚-.- + 𝑚01 + 𝑚" + 𝑚2/04
𝑚-.- = 𝐴-.- ⁄𝑔 ' ∆𝑃-.𝑚01 = 1 − 𝜀8 ' 𝜌: ' 𝐴1: ' 𝐿< − 𝐼<> +
1 − 𝜀8 ' 𝜌: ' 𝐴1? ' 𝐼1?+ 1 − 𝜀" ' 𝜌: ' 𝐴"? ' ℎ "?
𝑚" = 𝐴" ⁄𝑔 ' ∆𝑃"
𝑚2/04 = 1 − 𝜀A ' 𝜌: ' 𝐴A ' 𝐿A +
1 − 𝜀4 ' 𝜌: ' 𝐴2 ' 𝐻 ' 𝜂 𝐿4 − 𝐻 + 𝐿4 ' 𝜂 ∗ 𝐻 − 𝐿4
𝑑𝑚2/04
= 𝑊" − 𝑊<
𝑑𝑡
𝑑𝑚"
= 𝑊01 − 𝑊"
𝑑𝑡
𝑑𝑚01
= 𝑊- − 𝑊0<
𝑑𝑡
FluidizationXV– May22-27,2016
BubblingFluidizedBeds(BFBs)
hp: elutriation is negligible
• Massflowratetotheriser
0 → ℎ 2,- < ℎ 𝑊- = H
𝑊< → ℎ 2,- ≥ ℎ • Pressuredrop
∆𝑃-.- = 𝜌: ' 1 − 𝜀2 ' 𝑔 ' ℎ 2,-
FluidizationXV– May22-27,2016
LoopSeal
Loop Seal works in complete fluidization condition
between Supply Chamber (SC) and Recycle
Chamber (RC).
• Massflowrate
𝑊01 = 𝑊<
• Aerationgasflowrate
𝑄01 = 𝑄1? + 𝑄"?
• Gas“leakage” betweenSCandRC
𝑊" ' 𝜀8Q
𝑈0< ≥ 𝑈8Q −
𝐴1? ' 𝜌: ' 1 − 𝜀8Q
FluidizationXV– May22-27,2016
Risers
hp: transition between dense and dilute phase takes place when
mass flow rate approaches the value corresponding to
saturation carrying capacity.
• Massflowrate
𝐺< = H
𝐺S = 𝛽 ' 𝜌: ' 1 − 𝜀8Q ' 𝑈" → 𝐺< ≥ 𝐺S
𝐺U = 𝑈1 ⁄ℎ " ' 𝑚" ⁄𝐴" → 𝐺< < 𝐺S
• Pressuredrop
∆𝑃" = 𝜌: ' 1 − 𝜀2 ' 𝑔 ' ℎ 2 +
𝑔 ' 𝑊"
' ℎ" − ℎ2
𝐴" ' 𝑈1
FluidizationXV– May22-27,2016
Cyclone
hp: Collection efficiency was assumed to be 1
• Pressuredrop
∆𝑃?V? = 𝜌Q ' 𝐾? ' 𝑈?
Downcomer/L-Valve
• Pressuredrop
∆𝑃2XS
= 𝐾4 ' 𝑢Q[ − 𝑢<[
𝐻 − 𝐿Y
∆𝑃04
= 𝐾A ' 𝑢Q\ − 𝑢<\
𝐿A
0.0649 ' 𝜌: a.bbc ' 𝐿A 𝑊1
∆𝑃04 =
𝐷04 a.efg ' 𝑑: a.hif 𝐴"
a.jfk
• Aerationgasflowrate
𝑄04 = 𝑄A + 𝑄4
FluidizationXV– May22-27,2016
Oxygencarrier:CuO (50%inmass)onZrO2
Fuel:bituminous South-African coal
(VM:COCO2 H2H2O CH4)
FluidizationXV– May22-27,2016
Mass Balances
Dense regime/phase
𝑄l,*+ ' 𝐶n,*+ − 𝑄l,opq ' 𝐶n,l + 𝑚<>,l ' ∑* 𝑟* ' 𝛼n =0
𝑊l,*+ ' 𝐶<>,*+ − 𝑊l ,opq ' 𝐶<>,l + 𝑀<> ' 𝑚<>,l ' ∑* 𝑟* ' 𝛼n =0
Dilute regime/Free Board
1 𝑑𝑛n,l
= w 𝑟* ' 𝛼n
𝐴l 𝑑ℎ l
*
Energy balances
w𝑛̇ **+ ' 𝑐 z,* ' 𝑇 a − 𝑇**+ + w 𝑛̇ *opq ' 𝑐 z,* ' 𝑇*opq − 𝑇 a
+ w −∆𝐻|a} ' 𝑟n + 𝑄̇ = 0
Operatingconditions
Tfuel [K]
300
P[Pa]
105
minv [kg]
56.7
-1
UB [m·s ]
0.5
-1
UR [m·s ]
12
3 -1
QLV [m ·s ]
2.2·10-4
ULS [m·s-1]
2Umf
Propertiesofbedmaterials
ρp [kg·m -3]
2540
dp [m]
2.55·10-4
εmf [-]
0.445
εD [-]
0.445
εB [-]
0.445
εV [-]
0.423
εH [-]
0.488
GEOMETRICALCHARACTERISTICS
Riser
L-Valve
D R [m]
0.102
DLV [m]
0.04
hR [m]
5.6
LH [m]
0.4
Airreactor
LE [m]
0.4
D B [m]
0.38
Cyclone
hBFB [m]
(2x)1
Kc [-]
78
Downcomer
Loop-Seal
2
D D [m]
0.04
Asc [m ]
0.0025
LV [m]
3.6
hrc [m]
0.2
FluidizationXV– May22-27,2016
Time evolution up to the steady-state
conditions of:
A)Solidsinventoryinthereturnlegmlv
B)Solidsinventoryintherisermr
C)RisermassflowrateWr
D)SolidsmassfluxGS
FluidizationXV– May22-27,2016
Steady-stateconditions
Fuel massflowrate
Recirculated OCmassflux
AirReactor temperature
Fluidizinggastemperature FuelReactor
Fuelinlettemperature
Fluidizinggastemperature AirReactor
Bottombedinventory
Topbedinventory
Fuel Reactor pressure
Fuel reactor temperature
Riser pressure drop
Carbonconversiondegree
CO 2 CaptureCapacity
1kgs-1
116kgm-2 s-1
1223K
623K
300K
300K
15kg
15kg
10 5 Pa
10 3 K
2966Pa
0.58
0.62
Carbonconversiondegree
𝜂?X‰
𝑡𝑜𝑡𝑎𝑙𝐶𝑂h 𝑎𝑡𝑡ℎ𝑒𝑜𝑢𝑡𝑙𝑒𝑡𝑜𝑓𝑡ℎ𝑒𝐹𝑅
𝑝𝑟𝑜𝑑𝑢𝑐𝑒𝑑𝑏𝑦𝑓𝑢𝑒𝑙𝑐𝑜𝑚𝑏𝑢𝑠𝑡𝑖𝑜𝑛
=
𝑡𝑜𝑡𝑎𝑙𝑐𝑎𝑟𝑏𝑜𝑛𝑎𝑐𝑒𝑜𝑢𝑠𝑓𝑢𝑒𝑙𝑓𝑒𝑑𝑡𝑜𝑡ℎ𝑒𝐹𝑅
CO2 capturecapacity
𝜂??
𝑡𝑜𝑡𝑎𝑙𝐶𝑎𝑡𝑡ℎ𝑒𝑜𝑢𝑡𝑙𝑒𝑡𝑜𝑓𝑡ℎ𝑒𝐹𝑅
(𝑖𝑛𝑡ℎ𝑒𝑔𝑎𝑠𝑠𝑡𝑟𝑒𝑎𝑚)
=
𝑡𝑜𝑡𝑎𝑙𝐶𝑓𝑒𝑑𝑡𝑜𝑡ℎ𝑒𝐹𝑅
FluidizationXV– May22-27,2016
A simple tool to evaluate the performances of a novel twostage CLOU process carried out in a MIFB was developed.
The model is able to predict both main hydrodynamic
variables and kinetic performances of the proposed system.
Further work is needed in order to determine the range of
operability of the system and to highlight the effects of
different operating conditions on process performances.
FluidizationXV– May22-27,2016
Thank you foryour
kind attention
FluidizationXV– May22-27,2016