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
2 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
View on Oxyfuel Pilot Plant
3 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
CCS Demonstration Plant Jänschwalde
3 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia
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
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
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
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
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
9 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Water-steam cycle
10 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Status deconstruction – initial situation
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
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
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
14 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Turboset 250 MW
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
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
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
18 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Brine evaporator
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
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
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
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
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
24 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Flue gas desulphurisation (FGD)
Neubau
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
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
27 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
CCS Demo Plant, Jänschwalde unit G
28 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
29 | Lars Strömberg, IEA Oxyfuel Combustion conference Australia | Sept. 2011
Back – up ?
