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

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

CONCEPT OF ELEKTRO-GAS PLANT

DEVOLATILIZER

GASIFICATION

CHAR

LIQUID HYDROCARBONS

FUEL GAS

COAL

ELECTRIC ENERGY

RANGE OF PARAMETERS USED IN GASIFICATION EXPERIMENTS

CHARACTERISTICS OF GASIFIED MATERIALS 

FLUIDIZED BED GASIFIER

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.

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.

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.

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

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.

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.

Schematic diagram of the devolatilizer

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).

COAL DEVOLATILIZATION UNIT DIAGRAM

DEVOLATILIZER

BOILERCOMBUSTION

GASES

HEAT CHAR

AIR

WATER

TAR

GAS

COAL

STEAM

Connection of a coal devolatizer with the boiler

CHARACTERISTICS OF 1, 15, 50 t/h REACTORS