解决六角切圆锅炉结渣问题的研究及工程应用

7 V ol.24 No.7 Jul. 2004 2004 7 Proceedings of the CSEE?2004 Chin.Soc.for Elec.Eng.

0258-8013 (2004) 07-0231-05 TK223 A 470?20

1,2 1 1,2 3 1

(1. 150001 2.

154007 3. 150040

RESEARCH AND ENGINEERING APPLICATION ON SOLVING SLAGGING PROBLEM OF HEXAGONAL TANGENTIALLY FIRED BOILER

ZHAO Yu-xiao1,2, LI Rui-yang1, SUN Bin1,2, LU Wei3, QIN Yu-kun1

(1. Harbin Institute of Technology, Harbin 150001, China; 2. Jiamusi University, Jiamusi 154007,

China; 3. Harbin University of Science and Technology, Harbin 150040,China)

ABSTRACT In order to solve the slagging problem happened on the water-cooled wall and super-heater at the exit of furnace of a hexagonal tangentially fired boiler burning pulverized coal, based on the experience and research achievement of quadrangular tangentially fired boiler, the jet deviation and the reason causing slagging were analyzed theoretically, a PDA Particle Dynamics Analyzer cold model experiment of gas-solid two-phase flow near burner zone was also proceeded, and then a retrofit proposal of engineering technology was put forwarded which achieved a good engineering application. Research results show that adopting homocentric two tangential circles of primary air and secondary air properly can improve the flow field distribution in furnace effectively, thus, the slagging of heat-transfer surface is controlled.

KEY WORDS:Thermal power engineering; Hexagonal tangentially firing Slagging Homocentric two tangential circles

PDA Particle Dynamics Analyzer

1

670t/h

[1~5] 13660mm×11660mm 1000mm 3 0.6m×0.95m Φ100mm×12mm 2 0.48m×0.175m 1 2

3

4

5

2

1

6

X

Y

583mm

6

8

3

m

m

1

Fig. 1 Cross section and measuring zone of experimental

furnace

24

115mm

80mm

30mm

0mm

2

Fig. 2 Burner nozzles arrangement and position measuring

section in experiment

t

2

=1198 3.37

t

jz

=1027 [6]

2

2.1

16m/s

0.29

2.2

1 3

1

2

1

2

1

2 3000mm

52° 1 2400mm

56° 2

1

3 1 2

Fig. 3 Schematic diagram for analyzing #1 #2 burner jets

gas compensation condition

2.3

3

233

[7]

4 PDA

4.1

( 1000mm 1500mm 1000mm) [8] (Particle Dynamics Analyzer-PDA) [9,10]

20:1 683mm×583mm 1842mm( ) 13.58 m/s 28.81 m/s 0~10μm 8×10-4s 0~10μm 10~100μm

PDA 2/3

1 1 165mm×200mm

2 165mm×245mm ( y=100mm ) 1 2 00 2

2000 90s X Y Z L

a

=6

4.2

4 1 00

0 50 100 150 200 x/mm0 50 100 150 200 x/mm

50

100

150

200

y/mm

50

100

150

200

y/mm

(a) (b)

4 1 00

Fig. 4 Solid velocity vector graph at the 00 section

of #1 top-layer

4 ( ) ( ) [11]

5 1 +80mm

24

6 2 +30mm

0 50 100 150 200x /mm 0 50 100 150 200 x /mm

0 50

100150200y /mm 0

50

100150200y /mm (a) (b)

5 +80

Fig. 5 Gas velocity vector graph at the +80 section

of #1 top-layer

0 50 100 150 200 x /mm 0 50 100 150 200 x /mm

100

150200250300y /mm 350100

150

200250300y /mm 350(a) (b)

6 2 +30

Fig. 6 Gas velocity vector graph at the +30 section

of #2 top-layer

1

7 2 +115mm

0 50 100 150 200 x /mm 0 50 100 150 200 x /mm

100

150

200250300y /mm 350100

150200250300y /mm 350(a) (b)

72 +115

Fig. 7 Solid velocity vector graph at the +115 section

of #2 top-layer

5

1 16m/s 22m/s 50m/s 45m/s 0.29 0.44

235

2 1 4 56° 63° 2 5 52° 46°

3 6 88° 81° 8

(a) (b)

8

Fig. 8 Schematic diagram of get on the furnace cross section

6

200MW 3 1998 3

M t =22.14% A ar =18.91% Q net,ar =14540kJ/kg 97% 1.63% 462mg/m 3( [O 2]=6%)

4 9

7

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