DEVELOPMENT OF A FLUIDIZED BED COAL GASIFICATION TECHNOLOGY   Jerzy TOMECZEK Department of Process Energy Silesian University of Technology Presentation, Gliwice, 22 November 2005

RESEARCH ACTIVITY Clean Coal Technologies: · Gasification,   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.

INDUSTRIAL FLAME RESEARCH LABORATORY

INDUSTRIAL FLAME RESEARCH LABORATORY

HIGH TEMPERATURE FURNACE LABORATORY

COAL GASIFICATION PILOT PLANT

DEVOLATILIZER GASIFICATION CONCEPT OF ELEKTRO-GAS PLANT COAL FUEL GAS DEVOLATILIZER LIQUID HYDROCARBONS CHAR GASIFICATION ELECTRIC ENERGY

USED IN GASIFICATION EXPERIMENTS   RANGE OF PARAMETERS USED IN GASIFICATION EXPERIMENTS

CHARACTERISTICS OF GASIFIED MATERIALS   CHARACTERISTICS OF GASIFIED MATERIALS    

FLUIDIZED BED GASIFIER

D3 D3 D3 D2 D2 D2 1.5 m 2.0 m 1.5 m 1.3D1 1.3D1 D1 D D D Characteristic of tested variants of reactor geometry: D=100mm, D1=140 mm, D2=240 mm, D3=300 mm.

LOWER GAS HEATING VALUE, MJ/m3 COAL/AIR RATIO kg/kg 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.

LOWER GAS HEATING VALUE,MJ/m3 STEAM/AIR RATIO kg/kg 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.

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).

LOWER GAS HEATING VALUE, PARTICLE RESIDENCE TIME t, min MJ/m3 PARTICLE RESIDENCE TIME t, min Gas 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.

PARTICLE RESIDENCE TIME t, min CARBON CONVERSION xc, % PARTICLE RESIDENCE TIME t, min 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.

Schematic diagram of the devolatilizer

AMOUNT OF LIQUIDS, kg liquids/kg coal daf PYROLYSYS TEMPERATURE, oC Amount 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).

COAL DEVOLATILIZATION UNIT DIAGRAM

Connection of a coal devolatizer with the boiler GAS DEVOLATILIZER TAR CHAR HEAT AIR BOILER WATER COMBUSTION GASES STEAM Connection of a coal devolatizer with the boiler

CHARACTERISTICS OF 1, 15, 50 t/h REACTORS     CHARACTERISTICS OF THE 1, 15, 50 t/h DEMONSTRATION SCALE REACTORS   CHARACTERISTICS OF 1, 15, 50 t/h REACTORS