Modelling of a chemical looping combustion system equipped with a two- stage fuel reactor

Transcription

1 Engineering Conferences International ECI Digital Archives Fluidization XV Proceedings 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., solimene@irc.cnr.it 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 Follow this and additional works at: 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). 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 in Fluidization XV by an authorized administrator of ECI Digital Archives. For more information, please contact franco@bepress.com.

2 Università degli Studi del Sannio Dipartimento di Ingegneria Università degli Studi di Napoli Federico II Dipartimento di Ingegneria Chimica, dei Materiali e della Produzione Industriale MODELLING OF A CHEMICAL LOOPING COMBUSTION SYSTEM EQUIPPED WITH A TWO-STAGE FUEL REACTOR Antonio Coppola, Roberto Solimene Consiglio Nazionale delle Ricerche, IRC Napoli (Italy) Giuseppe Diglio, Piero Bareschino Università degli Studi del Sannio, DING Benevento (Italy) Piero Salatino Università degli Studi di Napoli Federico II, DICMaPI- Napoli (Italy) FluidizationXV May 22-27, 2016

3 Exploiting of CLOU effect for combustion of the most difficult part of the fuel: Char Two-stage Fuel Reactor: better utilization of the oxygen carrier Conversion of VM using the residual oxidative potential of the OC RTD is closer to a plug flow than a singlestage FR

4 Literature Most of numerical simulations of CLC in DIFB are focused only on kinetic scheme What you need? An appropriate hydrodynamic model of the whole system in order to point out stable operating conditions. Aim of the work To develop a simple mathematical tool coupling a CLC reactive scheme and a simple hydrodynamic model of a DIFB system.

5 FR split in two zones: dense zone below diluted zone/freeboard (FB) Dense zone is modelled as a CSTR, while FB is modelled as a PFR Instantaneous devolatilization AR is modelled as CSTR (dense regime) or PFR (diluted regime) The rate of heterogeneous reactions is ruled by chemical kinetics Conversion is uniform throughout solid particles Conversion of oxygen carrier and char in the air reactor is complete.

6 m *+, = m m 01 + m " + m 2/04 m -.- = A -.- g ' P -.- m 01 = 1 ε 8 ' ρ : ' A 1: ' L < I <> + 1 ε 8 ' ρ : ' A 1? ' I 1? + 1 ε " ' ρ : ' A "? ' h "? m " = A " g ' P " m 2/04 = 1 ε A ' ρ : ' A A ' L A + 1 ε 4 ' ρ : ' A 2 ' H ' η L 4 H + L 4 ' η H L 4 dm 2/04 dt = W " W < dm " dt = W 01 W " dm 01 dt = W - W 0<

7 Bubbling Fluidized Beds (BFBs) hp: elutriation is negligible Mass flow rate to the riser W - = H 0 h 2,- < h - W < h 2,- h - Pressure drop P -.- = ρ : ' 1 ε 2 ' g ' h 2,-

8 Loop Seal Loop Seal works in complete fluidization condition between Supply Chamber (SC) and Recycle Chamber (RC). Mass flow rate W 01 = W < Aeration gas flow rate Q 01 = Q 1? + Q "? Gas leakage between SC and RC W " ' ε 8Q U 0< U 8Q A 1? ' ρ : ' 1 ε 8Q

9 Risers hp: transition between dense and dilute phase takes place when mass flow rate approaches the value corresponding to saturation carrying capacity. Mass flow rate G < = H G S = β ' ρ : ' 1 ε 8Q ' U " G < G S G U = U 1 h " ' m " A " G < < G S Pressure drop P " = ρ : ' 1 ε 2 ' g ' h 2 + g ' W " A " ' U 1 ' h " h 2

10 Cyclone hp: Collection efficiency was assumed to be 1 Pressure drop P?V? = ρ Q ' K? ' U? Downcomer/L-Valve Pressure drop P 2XS H L Y = K 4 ' u Q[ u <[ P 04 L A = K A ' u Q\ u <\ P 04 = ' ρ : a.bbc ' L A D 04 a.efg ' d : a.hif Aeration gas flow rate Q 04 = Q A + Q 4 W 1 A " a.jfk

11 Oxygen carrier: CuO (50% in mass) on ZrO2 Fuel: bituminous South-African coal (VM: CO CO2 H2 H2O CH4) Fluidization XV May 22-27, 2016

12 Mass Balances Dense regime/phase Q l,*+ ' C n,*+ Q l,opq ' C n,l + m <>,l ' * r * ' α n =0 W l,*+ ' C <>,*+ W l,opq ' C <>,l + M <> ' m <>,l ' * r * ' α n =0 Dilute regime/free Board 1 A l dn n,l dh l Energy balances = w r * ' α n wn * *+ ' c z,* ' T a T * *+ * + w H } a ' r n + Q = 0 + w n * opq ' c z,* ' T * opq T a Operating conditions Properties of bed materials T fuel [K] 300 ρ p [kg m -3 ] 2540 P [Pa] 10 5 d p [m] m inv [kg] 56.7 ε mf [-] U B [m s -1 ] 0.5 ε D [-] U R [m s -1 ] 12 ε B [-] Q LV [m 3 s-1 ] ε V [-] U LS [m s -1 ] 2U mf ε H [-] GEOMETRICAL CHARACTERISTICS Riser L-Valve D R [m] D LV [m] 0.04 h R [m] 5.6 L H [m] 0.4 Air reactor L E [m] 0.4 D B [m] 0.38 Cyclone h BFB [m] (2x)1 K c [-] 78 Downcomer Loop-Seal D D [m] 0.04 A sc [m 2 ] L V [m] 3.6 h rc [m] 0.2

13 Time evolution up to the steady-state conditions of: A)Solids inventory in the return leg m lv B)Solids inventory in the riser m r C) Riser mass flow rate W r D)Solids mass flux G S

14 Steady-state conditions Fuel mass flow rate 1 kg s -1 Recirculated OC mass flux 116 kg m -2 s -1 Air Reactor temperature 1223 K Fluidizing gas temperature Fuel Reactor 623 K Fuel inlet temperature 300 K Fluidizing gas temperature Air Reactor 300 K Bottom bed inventory 15 kg Top bed inventory 15 kg Fuel Reactor pressure 10 5 Pa Fuel reactor temperature 10 3 K Riser pressure drop 2966 Pa Carbon conversion degree 0.58 CO 2 Capture Capacity 0.62 η?x = η?? = Carbon conversion degree total CO h at the outlet of the FR produced by fuel combustion total carbonaceous fuel fed to the FR CO 2 capture capacity total C at the outlet of the FR (in the gas stream) total C fed to the FR

15 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.

16 Thank you for your kind attention