development of a fluidized bed coal gasification technology jerzy tomeczek department of process...
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DEVELOPMENT OF A FLUIDIZED BED DEVELOPMENT OF A FLUIDIZED BED COAL GASIFICATION TECHNOLOGYCOAL GASIFICATION TECHNOLOGY
Jerzy TOMECZEKJerzy TOMECZEKDepartment of Process EnergyDepartment of Process Energy
Silesian University of TechnologySilesian University of Technology
Presentation, Gliwice, 22 November 2005Presentation, Gliwice, 22 November 2005
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RESEARCH ACTIVITY
Clean Coal Technologies:· Gasification,· Combustion.Low Pollutants Emission Combustion:· Mechanisms of NOx Formation,
· NOx Abatement Technologies.
Heat and Mass Transfer in Furnaces:· Mathematical Modelling,· Semi-Isothermal Combustion Conditions,· Fluidized Bed Structure Modelling,· Prediction of Deposits in Boilers.
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INDUSTRIAL FLAME RESEARCH LABORATORY
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INDUSTRIAL FLAME RESEARCH LABORATORY
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HIGH TEMPERATURE FURNACE LABORATORY
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COAL GASIFICATION PILOT PLANT
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CONCEPT OF ELEKTRO-GAS PLANT
DEVOLATILIZER
GASIFICATION
CHAR
LIQUID HYDROCARBONS
FUEL GAS
COAL
ELECTRIC ENERGY
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RANGE OF PARAMETERS USED IN GASIFICATION EXPERIMENTS
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CHARACTERISTICS OF GASIFIED MATERIALS
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FLUIDIZED BED GASIFIER
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D
D1
D D
1.3D1 1.3D1
1.5
m
1.5
m
2.0
m
D2 D2D2
D3 D3D3
Characteristic of tested variants of reactor geometry: D=100mm, D1=140 mm, D2=240 mm, D3=300 mm.
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LOWER GAS HEATING VALUE, MJ/m3
COAL/AIR RATIO kg/kg/ ,C am m
2/ 0H O am m Gas heating value as function of coal/air ratio for :
1- coal ● – A and ▲ - B, d=1.0-1.5 mm; 2- coal ○ – A and Δ - B, d=0.5-1.0mm;
3 - char ■ – C and □ - E.
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STEAM/AIR RATIO kg/kg2/ ,H O am m
LOWER GAS HEATING VALUE,MJ/m3
Gas heating value as function of steam/air ratio: 1- char Δ – C, □ - D and ■ – E, Tb=900oC;
2- coal ● – A and ▲ - B, d=1.0-1.5 mm, Tb=900oC.
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DECOMPOSED STEAM XH2O, %
STEAM/AIR RATIO kg/kg
Decomposed steam as function of steam/air ratio: 1- coal ○ – A and ● – B, char ■ – C and Δ – D for Tb=900oC;
2- coal for Tb=800oC by Tomeczek et al. (1983).
2/ ,H O am m
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LOWER GAS HEATING VALUE, MJ/m3
PARTICLE RESIDENCE TIME t, minGas heating value as function of bed residence time for air gasification and
Tb=900oC: 1- coal ● – A and ▲ - B, d=1.0-1.5 mm; 2- coal ○ – A and Δ - B, d=0.5-1.0mm;
3 - char ■ – C and □ - E, d=0.5-1.5mm.
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PARTICLE RESIDENCE TIME t, min
CARBON CONVERSION xc, %
Carbon conversion as function of particle residence time for Tb=900oC: 1- coal ○– A and ● - B air gasification; 2- char Δ – C, ◊ - D and □ - E air
gasification,▲ – C and ■ -E steam - air gasification.
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Schematic diagram of the devolatilizer
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AMOUNT OF LIQUIDS, kg liquids/kg coal daf
PYROLYSYS TEMPERATURE, oCAmount of liquids as a function of pyrolysis temperature:
— coal “Siersza” (Tomeczek et al, 1988), — coal “Loy Yang” (Edwards et al, 1985)
— coal “Millmerran” (Edwards et al, 1985), — coal eastern U.S. bituminous (Sass, 1988).
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COAL DEVOLATILIZATION UNIT DIAGRAM
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DEVOLATILIZER
BOILERCOMBUSTION
GASES
HEAT CHAR
AIR
WATER
TAR
GAS
COAL
STEAM
Connection of a coal devolatizer with the boiler
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CHARACTERISTICS OF 1, 15, 50 t/h REACTORS