F. Vega*, M. Rodríguez-Galán, B. Alonso-Fariñas, B. Navarrete, V. Cortés

Transcription

1 3 rd Oxyfuel Combustion Conference OCC3 Ponferrada (Spain), 9-13 September 2013 F. Vega*, M. Rodríguez-Galán, B. Alonso-Fariñas, B. Navarrete, V. Cortés Assistant Prof. Bernabé Alonso-Fariñas EPE Group, University of Seville, Spain School of Engineering UNIVERSITY OF SEVILLE

2 Brief Description ENVIRONMENTAL AND PROCESS ENGINEERING GROUP

3 Outline CCS technologies COMPARAE Project Modelling Laboratory tests Pilot plant facility Conclusions Future research

4 CCS technologies WORLD ELECTRIC POWER GENERATION Nuclear 3,3% Hyd. 21,0% TWh Others 0,6% 1980 Coal 38,3% Hyd. 16,0% Nuclear 12,9% TWh NG 22,2% Others 3,7% Coal 40,6% Oil 4,6% NG 12,1% Oil 24,7%

5 CCS technologies POST-COMBUSTION OXY-COMBUSTION Advantages Mature Technology Retrofitting Existing Plants Disadvantages Low CO 2 Concentration Large-Size Equipment Advantages High CO 2 Purity Low NO x Emissions Disadvantages High Energy Penalty (ASU) Higher Temperature Profiles

6 CCS technologies PARTIAL OXY-COMBUSTION + POST-COMBUSTION Promising CCS Technology Lower cost of ASU than oxycombustion Lower flue gas flow than post-combustion Retrofitting Existing Plants Higher CO 2 %

7 COMPARAE Project HYBRID OXY-POST COMBUSTION CARACTERIZACION AND OPTIMIZATION SIMULATION MODEL LABORATORY TESTS School of Engineering UNIVERSITY OF SEVILLE DESIGN AND ASSEMBLY OF PILOT FACILITY

8 Modelling Base Design BASE CASE SOLVENT MEA 30% w/w FUEL Anthracite Coal CO2 CAPTURE EFFICIENCY 85% 95% CONFIGURATION Conventional (DOE, 2007) MODELING PARAMETERS COLUMS RadFracc PROPERTY METHOD ELECNRTL NEW SOLVENTS/BLENDS Adding Chemical Reactions Input Data PROCESS Parameter Absorber Stripper Diameter / (mm) 300 Type Nuttering Packed Height 3 m/beds Beds 3 2 Pressure (bar) FLUE GAS Temperature (ºC) 50 Pressure (bar) 1 Flow (Nm 3 /h) 300 Mode AIR OXY40 OXY60 OXY80 Composition (%) CO

9 Modelling Chemical Stability and solubility Net Cyclic Capacity Desorber Energy Consumption Pollutants Concentration Availability and Cost SOLVENTS / BLENDS Test 1 Test 2 MEA DGA MEA / PZ K 2 CO 3 / PZ M D MP KP 1 KP 2 KP 3 KP 4 AIR MODE OXI 40 OXI 60 OXI 80

10 Modelling 300 Qreb (kw) L/G (kmol/kmol M 15 MP 12 KP 1 9 KP 2 6 KP 3 3 M MP KP 1 KP 2 KP 3 0 AIRE OXI 40 OXI 60 OXI 80 0 AIRE OXI 40 OXI 60 OXI kj/kg capt CO 2 Main Results AIRE OXI 40 OXI 60 OXI 80 M MP KP 1 KP 2 KP CO 2 inlet kj/kg capt CO 2 2capturado 2.- MEA Lower improvement 3.- KP-1 y KP-3 BEST POTENCIAL OPTION Partial-Oxy

11 Laboratory tests Main objetives Preliminary identification of the chemical sorbents Solubility and stability capabilities Maximun load capacity (mole CO 2 /mol sorbent) Desorption capacity Determination of the kinetic absortion/desorption Determination of the required regeneration energy CO 2 selectivity (NO X -SO 2 )

12 Laboratory tests Main objetives Model validation

13 Pilot plant facility Air enrichment Flue gas generation CO 2 CO 2 Capture CLEANED GASES AIR O 2 AIR ENRICHED AIR BURNER BOILER BOILER N 2

14 Pilot plant facility DESIGN PARAMETERS RANGE Boiler Thermal Power (kw) 1500 Flow rate (Nm 3 /h) 250/350 Operation mode (O 2 % oxidizer) Gas composition (% molar CO 2 ) Absorption Temperature (ºC) / Pressure (bar) / 1.1 Regeneration Temperature (ºC) / Pressure (bar) / 2-5 Absorber diameter (mm) (packed column) 300 Beds [Height (m) * Number] 3 * 3 Absorber diameter (mm) (pulverized column) 600 Beds [Height (m) * Number] - Stripper diameter (mm) (packet column) 300 Beds [Height (m) * Number] 3 * 2 Vapour Temperature (ºC) / Pressure (bar) 145 / 5 Vapour Consumption (kg/h) 600

15 Pilot plant facility

16 Pilot plant facility Partial Oxy-burner Fuel Diesel Max O 2 % 30 Fuel flow Comburent pressure Fuel pressurre kg/h 50 mbarg 2 barg

17 Pilot plant facility Process optiization % Oxygen enrichment (CO 2 concentration in flue gas) Purity of the O 2 stream Liquid / Gas in the absorber Regeneretion energy consumption Stripper pressure

18 Conclusions Modelling shows Carbonate/PZ blends reduce up to 30% reboiler duty versus MEA in partial oxy-combustion operation mode It has been observed that for similar absorption efficiency, Partial Oxy-combustion required less energy consumption than conventional Post-combustion process This research needs an economic study including air-enriched production cost to validate the promising results of this alternative for CCS A versatile pilot test facility have been designed and erected in order to characterize and optimize a new hybrid CCS process

19 Future Research Amine degradation studies in colaboration with Prof. Mercedes Maroto-Valer research group HYBRICAP Project New sorbent evaluation

20 School of Engineering University of Seville THANK YOU FOR YOUR ATTENTION