Panel II – Jänschwalde Oxyfuel demonstartion plant.€¦ · Lignite drying in pressurized...
Transcript of Panel II – Jänschwalde Oxyfuel demonstartion plant.€¦ · Lignite drying in pressurized...
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1 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Panel II – Jänschwalde Oxyfuel demonstartion plant.
IEAGHG 2nd Oxyfuel Conference 2011 11th – 16th of Sept 2011
Yeppoon QLD, Australia Lars Strömberg Vattenfall AB
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2 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
View on Oxyfuel Pilot Plant
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3 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
CCS Demonstration Plant Jänschwalde
3 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia
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4 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Requirements on the CCS demonstration plant
Kohletrocknung
Kühlturm
PCC
Oxyfuel-Kessel
Entstaubung
REA
LZA
Maschinenhaus
• Demonstration of two CCS-Technologies for Lignite
• Process parameters are all state of the art with supercritcal steam data
• High total thermal efficiency including capture reached by adwanced design • = 36 % (38 %)
• 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 CO2 per Year
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5 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Demonstration Plant Jänschwalde – Technical data
Oxyfuel: • New build single block at existing
power plant site • Capacity 250 MWe • Efficiency (net) 37 % • Separated CO2 1,34 Mio.t/a • Specific CO2-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
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6 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
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
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7 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Demonstration Plant Jänschwalde – Capture in detail
Lignite Dryer
Cooling Tower
Post Combustion Capture (PCC)
Oxyfuel-Boiler Particulate removal
Desulphurization
Air Separation Unit
Machine House
CO2-Compression
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8 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Oxyfuel – process flow sheet
Technical specifications:
optimization and layout for oxyfuel operation
flue gas recirculation after FGD (reduction of SO2 content of flue gas)
oxygen content of oxidant • 27 vol %(f)
GPU
GG
H SDA FF Kesse
SCR
FG-Bypass
CO2 plant FGD Filter Boiler
SCR
FGC Heat
recovery
O 2
TBK
sealing gas
transport gas
Fan 1
Recirculation fan
Fan 2
Cooling tower
Vent gas G
as p
re-h
eate
r
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9 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Water-steam cycle
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10 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Status deconstruction – initial situation
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11 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Demolition works - underground pipeworks for site preparation
• Preparations are almost finished
• The process is complete at the end of August 2011
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12 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
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) - CO2 sealing gas system - CO2, O2 alarm devices - co-firing of residual gases from PFBD
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13 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
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
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14 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Turboset 250 MW
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15 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Pilot plant for PFBD – lignite drying
Lignite drying in pressurized fluidized bed up to 5.5 bar heated by steam of 17 bar
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16 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
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
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17 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
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
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18 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Brine evaporator
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19 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
ASU– Unit G – 115,500 Nm³/h – key numbers
compression lines 2 x 50%
cryogenic part single train installation
load range ASU 50 – 100%
load range main air compressors 75 – 100%
load change requirements 5%/min O2 2%
oxygen pressure to boiler 1.2bar 50mbar
O2 backup system 60% ASU load for 4h
limited energy consumption • 38MWel
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20 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Dimension impressions ASU 1x63,000 Nm³/h GOX (NL)
pre cooling/ molsieve station
coldbox and columns & MHEx
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21 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Flue gas particulate removal
Demonstration der großtechnischen CO2 – 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
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22 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Oxyfuel boiler G – DeNOx
selective catalytic reduction (SCR)
reducing agent: pure ammonia
NH3-slip <1,5 mg/m³
SO2/SO3 conversion <1%
catalyst lifetime >18000 operating hours
acoustic cleaning
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23 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
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 CO2 content scrubber with external oxidation of CaSO3 to CaSO4 (gypsum) without air input into
gas stream
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24 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Flue gas desulphurisation (FGD)
Neubau
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25 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
3D animation CO2 processing unit (CPU)
CO2 product and raw gas compression
CO2- capture + heavy metall adsorber
flue gas condenser
direct cooler with integrated heat recovery system
dryer / adsorber
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26 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Alternative flue gas and CO2 processing
• Integrated flue gas treatment, • CO2-separation • Membrane unit
Technology proved in laboratory scale, now validated
Specific energy demand reduced 30 – 50 %/t CO2 sep.
Budget 10 Mio € Capital Costs 1,6 Mio € R&D Costs
Pilot plant recently comissioned and first experiences gained with excellent results
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27 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
CCS Demo Plant, Jänschwalde unit G
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28 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
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29 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Back – up ?