Panel II Jänschwalde Oxyfuel demonstartion plant.

Transcription

1 Panel II Jänschwalde Oxyfuel demonstartion plant. IEAGHG 2nd Oxyfuel Conference th 16th of Sept 2011 Yeppoon QLD, Australia Lars Strömberg Vattenfall AB 1 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

2 View on Oxyfuel Pilot Plant 2 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

3 CCS Demonstration Plant Jänschwalde 3 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

4 Requirements on the CCS demonstration plant Demonstration of two CCS- Technologies for Lignite Oxyfuel-Kessel Entstaubung Kohletrocknung Maschinenhaus LZA PCC Process parameters are all state of the art with supercritcal steam data High total thermal efficiency including capture reached by adwanced design = 36 % (38 %) REA Kühlturm Use of integrated coal drying Wide range Base load operation (50 bis 103 %) for intergration with renewable enrgy sources High plant availability ( 97 %) Capture and storage of 1,7 Million tonnes CO 2 per Year 4 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

5 Demonstration Plant Jänschwalde Technical data Oxyfuel: New build single block at existing power plant site Capacity 250 MWe Efficiency (net) 37 % Separated CO 2 1,34 Mio.t/a Specific CO 2 -emissions 78 g/kwh Post combustion capture Retrofitting of a part of an existing unit Capacity 50 MWe Separated CO2 0,39 Mio.t/a Specific CO2-emissions 107 g/kwh 5 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

6 Demonstration Plant Jänschwalde Investment cost CCS demonstration project Jänschwalde Total investment: approx. 1.5 bln. (1,2 bln. Capture (oxyfuel and post comb.) and 0.3 bln. Transport & Storage 6 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

7 Demonstration Plant Jänschwalde Capture in detail Post Combustion Capture (PCC) Lignite Dryer Machine House Air Separation Unit CO 2 -Compression Oxyfuel-Boiler Cooling Tower Desulphurization Particulate removal 7 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

8 Oxyfuel process flow sheet transport gas sealing gas FG-Bypass Cooling tower Vent gas Kesse Boiler SCR Gas pre-heater SDA Filter FF GGH Fan 1 Recirculation fan Heat recovery FGD Fan 2 FGC CO2 plant GPU O 2 TBK Technical specifications: optimization and layout for oxyfuel operation flue gas recirculation after FGD (reduction of SO 2 content of flue gas) oxygen content of oxidant 27 vol %(f) 8 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

9 Water-steam cycle 9 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

10 Status deconstruction initial situation 10 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

11 Demolition works - underground pipeworks for site preparation Preparations are almost finished The process is complete at the end of August Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

12 Oxyfuel boiler G technical data forced-circulation tower boiler state of the art steam parameters steam temp. 600/610/610 C steam pressure 286 bar steam massflow 178 kg/s specifications: - fired with dry lignite - flue gas recirculation - gas pre-heater - DeNOx in 2nd draught (optional) - CO 2 sealing gas system - CO 2, O 2 alarm devices - co-firing of residual gases from PFBD 12 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

13 Requirements turboset material choice for supercritical steam parameters: 276 bar, 600/ 620 C high load flexibility steam cogeneration for process steam: 15.5 bar, 34 kg/s coupling of steam from brine evaporator between medium pressure and low pressure-turbine: 3.4 bar, 24 kg/s 8 unregulated tappings for regenerative preheating and prozess steam low temperature difference of 2 K to achieve a low condenser vacuum of 34 mbar 13 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

14 Turboset 250 MW 14 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

15 Pilot plant for PFBD lignite drying Lignite drying in pressurized fluidized bed up to 5.5 bar heated by steam of 17 bar 15 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

16 Functions of PFBD in unit G Supplied with prepared raw fine lignite (0 10 mm) from ordinary coal preparation after bunker Transport of raw fine lignite to the mills and grind to a fineness of 0 1 mm (with oversized grains) Coal drying in PFBD at approx. 4 bar by steam extracted at 15 bar Temporary storage of non-cooled and cooled dry lignite Transport of the dry lignite with maximum water content of 12 mass % to the boiler Supply of filtered and pressurized vapour to the vent condenser/brine evaporator for steam energy recovery 16 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

17 Specifications of drying plant 3 drying lines Throughput raw lignite: 79 t/h x 3 Watercontent raw lignite: 53.4 % Throughput dry lignite: 44 t/h x 3 Watercontent dry lignite:<12 mass % Heat supply 25 MW each line Massflow steam 13 kg/s each line 17 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

18 Brine evaporator 18 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

19 ASU Unit G 115,500 Nm³/h key numbers compression lines 2 x 50% cryogenic part single train installation load range ASU % load range main air compressors % load change requirements 5%/min O 2 2% oxygen pressure to boiler 1.2bar 50mbar O 2 backup system 60% ASU load for 4h limited energy consumption 38MW el 19 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

20 Dimension impressions ASU 1x63,000 Nm³/h GOX (NL) pre cooling/ molsieve station coldbox and columns & MHEx 20 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

21 Flue gas particulate removal Demonstration der großtechnischen CO 2 Abscheidung ESP low pressure loss low power consumption low costs for operation and maintenance uncomplicated performance in service during start-up/ shut down procedure and failure components (electrodes) with long service run established and proven equipment in Vattenfall 21 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

22 Oxyfuel boiler G DeNOx selective catalytic reduction (SCR) reducing agent: pure ammonia NH 3 -slip <1,5 mg/m³ SO 2 /SO 3 conversion <1% catalyst lifetime >18000 operating hours acoustic cleaning 22 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

23 Flue gas desulphurisation (FGD) Design conditions: wet FGD technology, absorbent limestone product marketable gypsum scrubber outdoors material: alloy or steel rubberized or glass reinforced plastics specifics: operation of FGD with flue gas nearly free from nitrogen and very high CO 2 content scrubber with external oxidation of CaSO 3 to CaSO 4 (gypsum) without air input into gas stream 23 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

24 Flue gas desulphurisation (FGD) Neubau 24 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

25 3D animation CO 2 processing unit (CPU) CO 2 - capture + heavy metall adsorber CO 2 product and raw gas compression direct cooler with integrated heat recovery system dryer / adsorber flue gas condenser 25 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

26 Alternative flue gas and CO2 processing Pilot plant recently comissioned and first experiences gained with excellent results Integrated flue gas treatment, CO 2 -separation Membrane unit Technology proved in laboratory scale, now validated Specific energy demand reduced %/t CO 2 sep. Budget 10 Mio Capital Costs 1,6 Mio R&D Costs 26 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

27 CCS Demo Plant, Jänschwalde unit G 27 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

28 28 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011

29 Back up? 29 Lars Strömberg, IEA Oxyfuel Combustion conference Australia Sept. 2011