X hits on this document

PDF document

Biomass gasification for DRI production - page 2 / 5

19 views

0 shares

0 downloads

0 comments

2 / 5

Compressor

2

1

4

HYL Reactor

37401 m3(STP)/hour 10.4 m3(STP)/s

3

Heater

7

5

6

To package boiler To produce steam

10

9

~ ~

Fuel

11

Compressor

8

Syngas flow rate (from biomass gasification) 1 0 1 1 4 0 m 3 ( S T P ) / h o u r 2 8 . 1 m 3 ( S T P ) 10.5 GJ/t DRI / s

1 33.5 23.5 22.1

2 40.9 28.7 27.0

3 40.9 28.7 27.0

4 40.9 28.7 27.0

5 55.3 38.8

6 48.2 43.4

7 48.2 43.4

8 38.8 49.5

9 38.8 49.5

10 38.8 49.5 5.4

11 36.0 4.0 5.0

1.5

3.2

3.2

5.4

5.4

2.0 18.9

2.5 0.9

2.5 0.9

2.5 0.9

3.4 1.1

1.9 3.3

1.9 3.3

0.0 6.3

0.0 6.3

0.0 6.3

51.0 4.0

162400 475

132900 35

4980 35

127920 90

94680 42

165490 45

165490 820

15350 45

15000 45

70790 45

100000 40

H2 (% vol) CO (% vol)

H2O (% vol)

Flow rate (m3/h) Temp (°C)

Figure 1. Mass and energy balance for a DRI process carried out with syngas from biomass gasification (calculations supplied by HYL).

CO2

(% vol)

CH4

(% vol)

In the figure the flow sheet of this process is re- ported together with data of flow rate, composition and temperature of the gas in the different stages of the cycle, when the HYL is coupled with a biomass gasifier.

1.800

Gasification processes for Biomass wc=0,5 kg/kg dm af (wc*=0,04166 kmol/kg), wo=0,44 kg/kg dm af, wh = 0,06 kg/kg dm af

1.600

Cokemaking

Gasification technologies characterisation

and

biomass

According to the large quantity of gas to be intro- duced only systems of fluidised bed gasification and operation with technological oxygen at high pres- sures is proposed. The application of biomass gasifi- cation technology to supply reducing gas for DRI and CO2 capture and storage, requires sufficient heating value (LHV), and no nitrogen. These criteria can be fulfilled with the operation with oxygen of technical purity (95% O2).

Gasification Temperature [°C]

1.400

Transport reactor Slag smelting gasification

1.200

1.000

800

Pyrolysis (reforming)

600

Pyrolysis

Fluidized bed gasification with O2

wo Biomass = 0,44 = 0,01375 kmol O2/kg dm

400 0,000

0,005

0,010

0,015 0,020 0,025 0,030 0,035 O2 for Gasification [kmol/kg Biomass dm af]

0,040

Figure 2. Gasification processes.

Burning 0,04276 kmol O2/kg dm

0,045

0,050

Figure 2 shows a map of different gasification proc- ess for biomass.

45.000

LHV of Hydrocarbons LHV=34.835*wC+93.870*wH-10.800*wO

Oil sec.

Oil prim.

40.000

Hard coal

Figure 3 shows LHV as a function of carbon contents of various types of combustibles.

35.000

30.000

Brown coal

Coke

LHV [kJ/kg dm]

25.000

20.000

Hydrogen content wH Oxygen content = Difference to 1

wH=0

Biomass

15.000

wH=0,15

10.000

Trend of VM

wH=0,10

5.000

wH=0,05

-

  • 0

    0,1

0,2

0,3

0,4 0,5 0,6 Carbon content wC [kg C/kg dm]

0,7

0,8

0,9

1

Figure 3. Low calorific values of combustibles as a function of carbon content.

T. Buergler and A. Di Donato

2

SP12 – ULCOS-4, October 2008

Document info
Document views19
Page views19
Page last viewedWed Dec 07 00:34:36 UTC 2016
Pages5
Paragraphs318
Words3304

Comments