Technical specification “Device for sampling flue gases of NGRES boilers. Boiler auxiliary equipment Technical conditions t 150 cyclone tgm 84

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Technical specification “Device for sampling flue gases of NGRES boilers. Boiler auxiliary equipment Technical conditions t 150 cyclone tgm 84

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Federal Agency for Education

State educational institution

higher professional education

"Ural State Technical University- UPI

Named after the first President of Russia B.N. Yeltsin" -

branch in Sredneuralsk

SPECIALTY: 140101

GROUP: TPP -441

COURSE PROJECT

THERMAL CALCULATION OF BOILER UNIT TGM - 96

IN THE DISCIPLINE “Boiler installations of thermal power plants”

Teacher

Svalova Nina Pavlovna

Kashurin Anton Vadimovich

Sredneuralsk

1.Assignment for course project

2. a brief description of and parameters of the TGM-96 boiler

3. Excess air coefficients, volumes and enthalpies of combustion products

4. Thermal calculation of the boiler unit:

4.1 Heat balance and fuel calculation

4.2 Regenerative air heater

A. cold part

b. hot part

4.4 Output screens

4.4 Entrance screens

Bibliography

1. Course project assignment

For the calculation, a TGM-96 drum boiler unit was used.

Job input data

Boiler parameters TGM - 96

Boiler steam output - 485 t/h

· The pressure of superheated steam at the outlet of the boiler is 140 kgf/cm 2

· Temperature of superheated steam - 560 °C

· Operating pressure in the boiler drum - 156 kgf/cm 2

· Temperature of feed water at the entrance to the boiler - 230°C

· Feed water pressure at the entrance to the boiler - 200 kgf/cm 2

· Temperature of cold air at the entrance to the RVP - 30°C

2 . Description of the thermal circuit

The boiler feedwater is turbine condensate. Which is heated by a condensate pump sequentially through the main ejector, seal ejector, stuffing box heater, PND-1, PND-2, PND-3 and PND-4 to a temperature of 140-150°C and supplied to deaerators 6 ata. In deaerators, gases dissolved in the condensate are separated (deaeration) and additional heating occurs to a temperature of approximately 160-170°C. Then the condensate from the deaerators is fed by gravity to the suction of the feed pumps, after which the pressure rises to 180-200 kgf/cm² and the feed water through PVD-5, PVD-6, and PVD-7, heated to a temperature of 225-235°C, is supplied to the reduced boiler power supply unit. Behind the boiler power regulator, the pressure drops to 165 kgf/cm² and is supplied to the water economizer.

Feedwater flows through 4 chambers D 219x26 mm into hanging pipes D 42x4.5 mm Art. 20, located in increments of 83 mm, 2 rows in each half of the flue. The outlet chambers of the hanging pipes are located inside the flue, suspended on 16 pipes D 108x11 mm, art. 20. From the chambers, water is supplied through 12 pipes D 108x11 mm to 4 condensers and then to the wall-mounted economizer panel. At the same time, flows are transferred from one side to the other. The panels are made of pipes D28x3.5 mm Art. 20 and shield side walls and a rotating camera.

Water passes in two parallel streams through the upper and lower panels and is directed into the inlet chambers of the convective economizer.

The convective economizer consists of upper and lower packages, the lower part is made in the form of coils made of pipes with a diameter of 28x3.5 mm art. 20, staggered with a pitch of 80x56 mm. It consists of 2 parts located in the right and left flue ducts. Each part consists of 4 blocks (2 upper and 2 lower). The movement of water and flue gases in a convective economizer is countercurrent. When operating on gas, the economizer has a boiling point of 15%. The separation of steam generated in the economizer (the economizer has a boiling point of 15% when operating on gas) occurs in a special steam separation box with a labyrinth water seal. Through an opening in the box, a constant amount of feed water, regardless of the load, is supplied along with steam into the volume of the drum under the flushing shields. Water is discharged from the flushing panels using drain boxes.

The steam-water mixture from the screens flows through steam removal pipes into distribution boxes, and then into vertical separation cyclones, where primary separation occurs. There are 32 double and 7 single cyclones installed in the clean compartment, and 8 in the salt compartment - 4 on each side. To prevent steam from cyclones from entering the downpipes, boxes are installed under all cyclones. The water separated in the cyclones flows down into the water volume of the drum, and the steam, together with a certain amount of moisture, rises up, passing by the reflective cover of the cyclone and enters the washing device, which consists of horizontal perforated shields, to which 50% of the feed water is supplied. The steam, passing through the layer of the washing device, gives it the main amount of silicon salts contained in it. After the washing device, the steam passes through a louvered separator and is additionally cleaned of moisture droplets, and then through a perforated ceiling shield, which equalizes the velocity field in the steam space of the drum, enters the superheater.

All separation elements are made dismountable and are fastened with wedges, which are welded to the separation parts.

The average water level in the drum is 50 mm below the middle of the average water gauge glass and 200 mm below the geometric center of the drum. The upper permissible level is +100 mm, the lower permissible level is 175 mm according to the water meter glass.

To heat the drum body during kindling and cooling when the boiler is stopped, a special device according to the UTE design is installed in it. Steam is supplied to this device from a nearby operating boiler.

Saturated steam from the drum with a temperature of 343°C enters 6 panels of the radiant superheater and is heated to a temperature of 430°C, after which it is heated to 460-470°C in 6 panels of the ceiling superheater.

In the first desuperheater, the steam temperature is reduced to 360-380°C. Before the first desuperheaters, the steam flow is divided into two streams, and after them, to equalize the temperature sweep, the left steam flow is transferred to the right side, and the right steam flow is transferred to the left. After transfer, each steam flow enters 5 inlet cold screens, followed by 5 outlet cold screens. In these screens, steam moves countercurrently. Next, the steam flows in a direct flow into 5 hot input screens, followed by 5 output hot screens. Cold screens are located on the sides of the boiler, hot screens are located in the center. The steam temperature level in the screens is 520-530oC.

Next, through 12 steam transfer pipes D 159x18 mm, st. 12Х1МФ, the steam enters the inlet package of the convective steam superheater, where it is heated to 540-545 ° C. If the temperature rises above the specified one, the second injection comes into operation. Further along the bypass pipeline D 325x50 st. 12Х1МФ enters the output package of the gearbox, where the temperature increase is 10-15°C. After it, the steam enters the output manifold of the gearbox, which towards the front of the boiler passes into the main steam line, and 2 main workers are mounted in the rear section safety valves.

To remove salts dissolved in the boiler water, continuous blowing is carried out from the boiler drum; the amount of continuous blowing is adjusted according to the instructions of the chemical shop shift manager. To remove sludge from the lower collectors of the screens, the lower points are periodically purged. To prevent the formation of calcium scale in the boiler, phosphate the boiler water.

The amount of introduced phosphate is regulated by the senior machinist on the instructions of the shift manager of the chemical workshop. To bind free oxygen and form a passivating (protective) film on the internal surfaces of boiler tubes, dose hydrazine into the feed water, maintaining its excess at 20-60 μg/kg. Dosing of hydrazine into the feed water is carried out by the personnel of the turbine department on the instructions of the shift supervisor of the chemical workshop.

To recover heat from continuous blowing of boilers Poch. 2 continuous blowdown expanders are installed in series.

Extender 1 tbsp. has a volume of 5000 l and is designed for a pressure of 8 atm with a temperature of 170 ° C, the vapor is directed to the heating steam collector 6 atm, the separator through the condensation pot into the Poch expander.

Extender P st. has a volume of 7500 liters and is designed for a pressure of 1.5 ata with an ambient temperature of 127 ° C, the vapor is directed to the low pressure control unit and is connected in parallel to the vapor of the drainage expanders and the reduced steam pipeline of the ignition ROU. The expander separator is directed through a water seal 8 m high into the sewer. Drainage supply of expanders P art. prohibited from entering the circuit! For emergency drainage from boilers P och. and purging of the lower points of these boilers, 2 parallel-connected expanders with a volume of 7500 liters each and a design pressure of 1.5 ata are installed in KTC-1. The vapor from each periodic blowdown expander is directed into the atmosphere through pipelines with a diameter of 700 mm without shut-off valves and discharged to the roof of the boiler shop. The separation of steam generated in the economizer (the economizer has a boiling point of 15% when operating on gas) occurs in a special steam separation box with a labyrinth water seal. Through an opening in the box, a constant amount of feed water, regardless of the load, is supplied along with steam into the volume of the drum under the flushing shields. Water is discharged from the flushing panels using drain boxes

3 . Excess air coefficients, volumes and enthalpiescombustion products

Calculated characteristics of gaseous fuel (Table II)

Excess air coefficients for gas ducts:

· Excess air coefficient at the furnace outlet:

t = 1.0 + ? t =1.0 + 0.05 = 1.05

· ?Coefficient of excess air behind the gearbox:

checkpoint = t + ? Gearbox = 1.05 + 0.03 =1.08

· Excess air coefficient for wind turbine:

VE = gearbox + ? VE =1.08 + 0.02 =1.10

· Excess air coefficient behind RVP:

RVP = VE + ? RVP =1.10 + 0.2 = 1.30

Characteristics of combustion products

Calculated value	Dimension	V°=9,5 2	V° H2O= 2 , 10	V° N2 = 7 , 6 0	V RO2=1, 04	V°g=10, 73
		GASES
		Firebox				Ugh. gases
Excess air coefficient, ? ?
Excess air ratio, average? Wed
V H2O =V° H2O +0.0161* (?-1)* V°
V Г =V RO2 +V° N2 +V H2O + (?-1)*V°
r RO2 =V RO2 /V G
r H2O =V H2O /V G
rn=r RO2 +r H 2O

Theoretical air quantity

V° = 0.0476 (0.5CO + 0.575H 2 O +1.5H 2 S + U(m + n/4)C m H n - O P)

Theoretical nitrogen volume

Theoretical volume of water vapor

Volume of triatomic gases

Enthalpies of combustion products (J - table).

J°g, kcal/nmі

J°в, kcal/nmі

J=J°g+(?-1)*J°w,kcal/nmі

Firebox

Flue gases

1, 09

1,2 0

1,3 0

4.Heatnew calculation of the boiler unit

4.1 Heat balance and fuel calculation

Calculated value	Designation	Size-ness	Formula or rationale	Calculation
Heat balance
Available fuel heat
Flue gas temperature
Enthalpy			According to the J-table
Cold air temperature
Enthalpy			According to the J-table
Heat loss:
From mechanical underburning
from chemical underburning			According to table 4
with flue gases			(Jух-?ух*J°хв)/Q р р	(533-1,3090,3)100/8550=4,9
into the environment
Amount of heat losses
Boiler unit efficiency (gross)
Superheated steam consumption
Superheated steam pressure behind the boiler unit
Temperature of superheated steam behind the boiler unit
Enthalpy			According to the table XXVI(N.m.p.221)
Feed water pressure
Feed water temperature
Enthalpy			According to the table XXVII (N.m. p.222)
Purge water flow				0,0150010 3 =5,0*10 3
Purge water temperature			t n at P b =156 kgf/cm 2
Enthalpy of purge water	ipr.v= i? instrumentation		According to the table XX1II (N.M. p.205)
Calculated value	Designations	Dimension	Formula or rationale	Calculation

4.2 Regenon-active air heater

Calculated value	Designation	Dimension	Formula or rationale	Calculation
Rotor diameter			According to design data
Number of air heaters per housing			According to design data
Number of sectors			According to design data	24 (13 gas, 9 air and 2 separating)
Proportions of surface washed by gases and air

Cold part
Equivalent diameter			p.42 (Normal)
Sheet thickness			According to design data (smooth corrugated sheet)
			0.785Din 2 хгКр	0,7855,4 2 0,5420,80,81*3=26,98
			0.785Din 2 hvKr	0,7855,4 2 0,3750,80,81*3=18,7
Packing height			According to design data
Heating surface			According to design data
Air inlet temperature
Enthalpy of air at inlet			By J-? table
Ratio of air flow at the outlet of the cold part to the theoretical
Air suction
Outlet air temperature (intermediate)			Preliminarily accepted
Enthalpy of air at outlet			By J-? table
			(V"hh+??hh) (J°pr-J°xv)	(1,15+0,1)*(201,67 -90,3)=139
Outlet gas temperature
Calculated value	Designation	Dimension	Formula or rationale	Calculation
Enthalpy of gases at the outlet			According to the J-table
Enthalpy of gases at the inlet			Juх+Qb/c -??хч*J°хв	533+139 / 0,998-0,1*90,3=663
Gas inlet temperature			By J-? table
Average gas temperature
Average air temperature
Average temperature difference
Average wall temperature			(хг?ср+хвtср)/ (хг+хв)	(0,542140+0,37549)/(0,542+0,375)= 109
Average gas speed			(ВрVг(?ср+273))/	(3704712,6747(140+273))/(293600273)=6,9
Average air speed			(ВрVє(в"хч+хч/2)*(tср+273))/	(370479,52(1,15+0,1)(49+273))/ (3600273*20,07)=7,3
		kcal/ (m 2 h *deg)	Nomogram 18 SnSfSy*?n	0,91,241,0*28,3=31,6
		kcal/ (m 2 h *deg)	Nomogram 18 SnS"fSy*?n	0,91,161,0*29,5=30,8
Usage rate
Heat transfer coefficient		kcal/ (m 2 h *deg)		0,85/(1/(0,54231,6)+1/(0,37530,8))=5,86
Heat absorption of the cold part (according to the heat transfer equation)				5,86975091/37047=140
Thermal perception ratio				(140/ 139)*100=100,7

Calculated value	Designation	Dimension	Formula or rationale	Calculation
Hot part
Equivalent diameter			p.42 (Normal)
Sheet thickness			According to design data
Live cross section for gases and air			0.785Din 2 хгКрКл*n	0,7855,4 2 0,5420,8970,89*3=29,7
			0.785Din 2 hvKrKl*n	0,7855,4 2 0,3750,8970,89*3=20,6
Packing height			According to design data
Heating surface			According to design data
Air inlet temperature (intermediate)			Pre-accepted (in the cold part)
Enthalpy of air at inlet			By J-? table
Air suction
Ratio of air flow rates at the outlet of the hot part to the theoretical
Outlet air temperature			Preliminarily accepted
Enthalpy of air at outlet			By J-? table
Thermal perception of the stage (balanced)			(v"gch+??gch/2)* *(J°gv-J°pr)	(1,15+0,1)*(806- 201,67)=755
Outlet gas temperature			From the cold part
Enthalpy of gases at the outlet			According to the J-table
Enthalpy of gases at the inlet			J?hch+Qb/ts-??gch*	663+755/0,998-0,1*201,67=1400
Gas inlet temperature			By J-? table
Average gas temperature			(?ch+??xch)/2	(330 + 159)/2=245
Average air temperature
Average temperature difference
Average wall temperature			(хг?ср+хвtср)	(0,542245+0,375164)/(0,542+0,375)=212
Average gas speed			(ВрVг(?ср+273))	(3704712,7(245 +273)/29,73600273 =8,3
Calculated value	Designation	Dimension	Formula or rationale	Calculation
Average air speed			(VrVє(v"vp+?? rch (tav+273))/(3600273 Fв)	(370479,52(1,15+0,1)(164+273)/ /360020,6*273=9,5
Heat transfer coefficient from gases to the wall		kcal/ (m 2 h *deg)	Nomogram 18 SnSfSy*?n	1,61,01,07*32,5=54,5
Heat transfer coefficient from wall to air		kcal/ (m 2 h *deg)	Nomogram 18 SnS"fSy*?n	1,60,971,0*36,5=56,6
Usage rate
Heat transfer coefficient		kcal/ (m 2 h *deg)	o / (1/ (хг?гк) + 1/(хв?вк))	0,85/ (1/(0,54259,5)+1/0,37558,2))=9,6
Thermal absorption of the hot part (according to the heat transfer equation)				9,63645081/37047=765
Thermal perception ratio				765/755*100=101,3
The values of Qt and Qb differ by less than 2%.

vp=330°С tgv=260°С

Јвп=1400 kcal/nm 3 Јгв=806 kcal/nm 3

khch=159°С tpr=67°С

Јхч=663 kcal/nm 3

Јpr=201.67 kcal/nm 3

хх=120°С tхв=30°С

Јхв=90.3 kcal/nm 3

Јух=533 kcal/nm 3

4.3 Firebox

Calculated value	Designation	Dimension	Formula or rationale	Calculation
Diameter and thickness of screen pipes			According to design data
			According to design data
Total surface of the combustion chamber walls			According to design data
Volume of the combustion chamber			According to design data
				3,6*1635/1022=5,76
Excess air coefficient in the furnace
Air sucks into the boiler furnace
Hot air temperature			Based on the air heater
Enthalpy of hot air			By J-? table
Heat introduced by air into the firebox			(?t-??t)* J°gv + +??t*J°hv	(1,05-0,05)806+0,0590,3= 811,0
Useful heat release in the firebox			Q р р*(100-q 3) / 100+Qв	(8550*(100-0,5)/100)+811 =9318
Theoretical combustion temperature			By J-? table
Relative position of maximum temperatures along the height of the furnace			xt =xg =hg/Ht
Coefficient			p.16 0.54 - 0.2*xt	0,54 - 0,2*0,143=0,511
			Preliminarily accepted
			By J-? table
Average total heat capacity of combustion products		kcal/(nm*deg)	(Qt- J?t)*(1+Chr)	(9318 -5 018 )*(1+0,1) (2084-1200) =5,35
Work		m*kgf/cmI		1,00,27985,35=1,5
Coefficient of attenuation of rays by triatomic gases		1/ (m**kgf/ /cm 2)	Nomogram 3
Optical thickness				0,380,27981,0*5,35=0,57
Calculated value	Designation	Dimension	Formula or rationale	Calculation
Torch blackness level			Nomogram 2
Thermal efficiency coefficient of smooth tube screens			shekr=x*f shek = w at x = 1 according to table. 6-2
Blackness level of the combustion chamber			Nomogram 6
Gas temperature at the furnace outlet			Ta/[M((4.910 -8 * shekrFstatTai)/(ts* Вр*Vср)) 0.6 +1]-273	(2084+273)/-273=1238
Enthalpy of gases at the exit from the furnace			By J-? table
The amount of heat absorbed in the firebox				0,998*(9318-5197)=4113
Average thermal load of the radiation-receiving heating surface			Вр*Q t l/Nl	37047*4113/ 903=168742
Thermal stress of the combustion volume			Вр*Q р n/Vт	37047*8550/1635=193732

4.4 HotwIrma

Calculated value	Convoy- otherwise- tion	Dimension	Formula or rationale	Calculation
Pipe diameter and thickness			According to drawing
			According to drawing
Number of screens			According to drawing
Average step between screens			According to drawing
Longitudinal pitch			According to drawing
Relative lateral pitch
Relative longitudinal pitch
Screen heating surface			According to design data
Additional heating surface in the hot screen area			According to drawing	6,65*14,7/2= 48,9
Entrance window surface			According to drawing	(2,5+5,38)*14,7=113,5
			Nin*(НшI/(НшI+HdopI))	113,5*624/(624+48,9)=105,3
			N in - N lshI
Live cross section for gases			According to design data
Live section for steam			According to design data
Effective thickness of the radiating layer			1.8 / (1/ A+1/ B+1/ C)
Gas inlet temperature			Based on the firebox
Enthalpy			By J-? table
Coefficient
Coefficient
	kcal/(m 2 h)	in * z in * q l	0,61,35168742=136681
Radiant heat absorbed by the plane of the inlet section of hot screens			(q lsh *N in) / (Vr/2)	(136681113,5)/ 370470,5=838


Calculated value	Designation	Dimension	Formula or rationale	Calculation
Temperature of gases at the exit from the screens I and?? steps			Preliminarily accepted
			By J-? table
Average temperature of gases in hot screens				(1238+1100)/2=1069
Work		m*kgf/cmI		1,00,27980,892=0,25
			Nomogram 3
Optical thickness				1,110,27981,0*0,892=0,28
			Nomogram 2
			v ((th/S1)І+1)th/S1
			(Q l in?(1-a)??ts w)/in+ +(4.910 -8 aZl.out* T av 4 op) / Vr0.5	(838 (1-0,245)0,065)/0,6+(4,910 -8 0,245(89,8)(1069+273) 4 0,7)/ 370470,5)= 201
Heat received by radiation from the firebox by stage I screens	Q lshI + extra		Q l in - Q l out
			Q t l - Q l in
			(Qscreen?Vr) / D	(3912*37047)/490000=296
Quantity radiant heat, taken from the firebox by screens			QлшI + extra* Nlsh I/(Nlsh I+Nl additional I)	637*89,8/(89,8+23,7)= 504
			Q lsh I + add * N l add I / (N lsh I + N l add I)	637*23,7/(89,8+23,7)= 133
				0,998*(5197-3650)= 1544
Including:
the screen itself			Preliminarily accepted
additional surfaces			Preliminarily accepted
			Preliminarily accepted
Enthalpy there
Calculated value	Designation	Dimension	Formula or rationale	Calculation
			(Qbsh+ Qlsh)*Vr	(1092 + 27 2 ,0 )* 3 7047 *0,5
Enthalpy of steam at outlet				747,8 +68,1=815,9
Temperature is the same			According to table XXV
Average steam temperature				(440+536)/2= 488
Temperature difference
Average gas speed
				520,9850,6*1,0=30,7
Pollution factor		m 2 h deg/ /kcal
				488+(0,0(1063+275)33460/624)=
				2200,2450,985=53,1
Usage rate
Heat transfer coefficient from gases to the wall				((30,73,140,042/20,04750,98)+53,1) *0,85= 76,6
Heat transfer coefficient				76,6/ (1+ (1+504/1480)0,076,6)=76,6
			k? НшI ??t / Вр*0.5	76,6624581/37047*0,5=1499
Thermal perception ratio			(Q tsh / Q bsh)??100	(1499/1480)*100=101,3
			Preliminarily accepted
			k? NdopI ? (?av?-t)/Br	76,648,9(1069-410)/37047=66,7
Thermal perception ratio	Q t add / Q b add		(Q t extra / Q b extra)??100	(66,7/64)*100=104,2

ValuesQtsh andQ

AQt additional andQ

4.4 ColdwIrma

Calculated value	Designation	Dimension	Formula or rationale	Calculation
Pipe diameter and thickness			According to drawing
Number of pipes connected in parallel			According to drawing
Number of screens			According to drawing
Average step between screens			According to drawing
Longitudinal pitch			According to drawing
Relative lateral pitch
Relative longitudinal pitch
Screen heating surface			According to design data
Additional heating surface in the screen area			According to drawing	(14,7/26,65)+(26,65*4,64)=110,6
Entrance window surface			According to drawing	(2,5+3,5)*14,7=87,9
Ray-receiving surface of screens			Nin*(НшI/(НшI+HdopI))	87,9*624/(624+110,6)=74,7
Additional beam-receiving surface			N in - N lshI
Live cross section for gases			According to design data
Live section for steam			According to design data
Effective thickness of the radiating layer			1.8 / (1/ A+1/ B+1/ C)	1,8/(1/5,28+1/0,7+1/2,495)=0,892
Temperature of gases leaving cold			Based on hot
Enthalpy			By J-? table
Coefficient
Coefficient
	kcal/(m 2 h)	in * z in * q l	0,61,35168742=136681
Radiant heat absorbed by the plane of the input section of the screens			(q lsh N in) / (Vr 0.5)	(13668187,9)/ 370470,5=648,6
Correction factor for taking into account radiation per beam behind screens

Calculated value	Designation	Dimension	Formula or rationale	Calculation
Temperature of gases at the inlet to cold screens			Based on hot
Enthalpy of gases at the exit from the screens at the accepted temperature			According to J-table
Average temperature of gases in screens?st.				(1238+900)/2=1069
Work		m*kgf/cmI		1,00,27980,892=0,25
Ray attenuation coefficient: triatomic gases			Nomogram 3
Optical thickness				1,110,27981,0*0,892=0,28
Blackness degree of gases in screens			Nomogram 2
Angular coefficient from the input to the output section of the screens			v ((1/S 1)І+1)-1/S 1	v((5.4/0.7)І+1) -5.4/0.7=0.065
Heat radiation from the firebox to the entrance screens			(Ql in? (1-a)??tssh)/v+(4.910 -8 aZl.out(Tsr) 4 *op) / Vr	(648,6 (1-0,245)0,065)/0,6+(4,910 -8 0,245(80,3)(1069+273)4 0,7)/ 370470,5)= 171,2
Heat received by radiation from the firebox by cold screens			Ql in - Ql out	648,6 -171,2= 477,4
Heat perception of combustion screens			Qtl - Ql in	4113 -171,2=3942
Increase in enthalpy of the medium in screens			(Qscreen?Vr) / D	(3942*37047)/490000=298
The amount of radiant heat absorbed from the firebox by the entrance screens			QлшI + extra* Nlsh I/(Nlsh I+Nl additional I)	477,4*74,7/(74,7+13,2)= 406,0
The same with additional surfaces			Qlsh I + add * Nl add I / (NlshI + Nl add I)	477,4*13,2/(74,7+13,2)= 71,7
Thermal absorption of stage I screens and additional surfaces according to balance			c* (Ј "-Ј "")	0,998*(5197-3650)=1544

Calculated value	Designation	Dimension	Formula or rationale	Calculation
Including:
the screen itself			Preliminarily accepted
additional surfaces			Preliminarily accepted
Steam temperature at the outlet of the inlet screens			Based on weekends
Enthalpy there			According to table XXVI
Increase in steam enthalpy in screens			(Qbsh+ Qlsh)*Vr	((1440+406,0)* 37047) / ((490*10 3)=69,8
Enthalpy of steam at the entrance to the entrance screens				747,8 - 69,8 = 678,0
Steam temperature at the screen inlet			According to table XXVI (P=150kgf/cm2)
Average steam temperature
Temperature difference				1069 - 405=664,0
Average gas speed			In r? V g? (?av+273) / 3600 * 273* Fg	3704711,2237(1069+273)/(360027374,8 =7,6
Convection heat transfer coefficient				52,00,9850,6*1,0=30,7
Pollution factor		m 2 h deg/ /kcal
Temperature of the outer surface of contaminants			t av + (e? (Q bsh + Q lsh)*Вр / НшI)	405+(0,0(600+89,8)33460/624)=
Radiation heat transfer coefficient				2100,2450,96=49,4
Usage rate
Heat transfer coefficient from gases to the wall			(? k? pd / (2S 2 ? x)+ ? l)?? ?	((30,73,140,042/20,04750,98)+49,4) *0,85= 63,4
Heat transfer coefficient			1 / (1+ (1+ Q lsh / Q bsh)?? ??? ? 1)	63,4/(1+ (1+89,8/1440)0,065,5)=63,4
Thermal perception of screens according to the heat transfer equation			k? НшI ??t / Вр	63,4624664/37047*0,5=1418
Thermal perception ratio			(Q tsh / Q bsh)??100	(1418/1420)*100=99,9
Average steam temperature in additional surfaces			Preliminarily accepted
Calculated value	Designation	Dimension	Formula or rationale	Calculation
Thermal perception of additional surfaces according to the heat transfer equation			k? NdopI ? (?av?-t)/Br	63,4110,6(1069-360)/37047=134,2
Thermal perception ratio	Q t add / Q b add		(Q t extra / Q b extra)??100	(134,2/124)*100=108,2

ValuesQtsh andQbsh differ by no more than 2%,

AQt additional andQb additional - less than 10%, which is acceptable.

Bibliography

Thermal calculation of boiler units. Normative method. M.: Energy, 1973, 295 p.

Rivkin S.L., Aleksandrov A.A. Tables of thermodynamic properties of water and water vapor. M.: Energy, 1975.

Fadyushina M.P. Thermal calculation of boiler units: Guidelines to complete a course project in the discipline “Boiler plants and steam generators” for full-time students of specialty 0305 - Thermal power plants. Sverdlovsk: UPI im. Kirova, 1988, 38 p.

Fadyushina M.P. Thermal calculation of boiler units. Guidelines for completing a course project in the discipline “Boiler plants and steam generators”. Sverdlovsk, 1988, 46 p.

1 SUBJECT

In accordance with the Environmental Program of OJSC Enel OGK-5 for 2011-2015, the Nevinnomyssk State District Power Plant branch of OJSC Enel OGK-5 requires the following:

Determination of the actual concentration of nitrogen oxides, carbon monoxide, methane at different loads and different operating modes of TGM-96 boilers (boiler No. 4) performer's instrument park.
Determination of the distribution density of nitrogen dioxide over the convective surface area in the control section.

3. Assessment of the reduction in the formation of nitrogen oxides through the use of regime measures and changes in the technical and economic indicators of boiler operation ( determining the effectiveness of the use of regime measures).

4. Development of proposals for the use of low-cost reconstructive measures aimed at reducing nitrogen oxide emissions.

2GENERAL DESCRIPTION OF THE OBJECT

General information

Nevinnomyssk State District Electric Power Station (NGRES) with a design capacity of 1340 MW is intended to cover the needs for electrical energy North Caucasus and supply of thermal energy to enterprises and the population of the city of Nevinnomyssk. Currently, the installed capacity of Nevinnomysskaya GRES is 1,700.2 MW.

The state district power plant is located on the northern outskirts of the city of Nevinnomyssk and consists of a combined heat and power plant (CHP), open-type condensing power units (block part) and a combined cycle gas plant (CCP).

Full name of the facility: Nevinnomyssk State District Power Plant branch of the open joint stock company"Enel is the fifth generating company of the wholesale electricity market" in Nevinnomyssk Stavropol Territory.

Location and mailing address: Russian Federation, 357107, Nevinnomyssk, Stavropol Territory, Energetikov Street, building 2.

^ Climatic conditions

Climate: temperate continental

Climatic conditions and ambient air parameters in this area correspond to the location of the state district power plant (Nevinnomyssk) and are characterized by the data in Table 2.1.

Table 2.1 Climatic data of the region (Nevinnomyssk from SNiP 01/23/99)

edge, point	Outside air temperature, degrees. WITH
	Outdoor air temperature, monthly average, degrees. WITH
	I	II	III	IV		V	VI		VII	VIII		IX	X	XI		XII
Stavropol	-3,2	-2,3	1,3	9,3		15,3	19,3		21,9	21,2		16,1	9,6	4,1		-0,5
					Less than 8℃						Less than 10℃
Average annual	The coldest five-day period with a security of 0.92				Duration, days.			Average temperature, degrees. WITH			Duration, days				Average temperature, degrees. WITH
9,1	-19				168			0,9			187				1,7

Perennial average temperature coldest air winter month(January) is minus 4.5°C, the hottest (July) is +22.1°C.

The duration of the period with persistent frosts is about 60 days,

The wind speed, the frequency of which does not exceed 5%, is 10-11 m/sec.

The dominant wind direction is east.

The annual relative humidity is 62.5%.

^ CHARACTERISTICS AND BRIEF DESCRIPTION OF THE TGM-96 BOILER UNIT.

Gas-oil boiler type TGM-96 of the Taganrog Boiler Plant, single-drum, with natural circulation, steam capacity 480 t/h with the following parameters:

Drum pressure - 155 ati

Pressure behind the main steam valve - 140 ati

Superheated steam temperature - 560С

Feed water temperature - 230С
^ Basic design data of the boiler when burning gas:
Steam capacity t/hour 480

Superheated steam pressure kg/cm 2 140

Temperature of superheated steam С 560

Feed water temperature С 230

Cold air temperature before RVV С 30

Hot air temperature С 265
^ FIREBOX CHARACTERISTICS

Volume of the combustion chamber m 3 1644 Thermal voltage of the combustion chamber kcal/m 3 h 187.10 3

Hourly fuel consumption VR nm 3 /h t/h 37.2.10 3

^ STEAM TEMPERATURE

Behind the wall superheater С 391 In front of the outer screens С 411

After the outer screens С 434 After the middle screens С 529 After the inlet packages of the convective superheater С 572

After the output packages of convective p/p. С 560

^ GASE TEMPERATURE

Behind the screens С 958

Behind the convective p/p С 738 Behind the water economizer С 314

Exhaust gases С 120
The boiler layout is U-shaped, with two convective shafts. The combustion chamber is shielded by evaporation pipes and radiant superheater panels.

The furnace ceiling of the horizontal flue duct of the rotating chamber is shielded by ceiling superheater panels. A screen superheater is located in the rotating chamber and the transition flue.

The side walls of the turning chamber and the slopes of the convective shafts are shielded with panels of a wall-mounted water economizer. The convective shafts contain a convective steam superheater and a water economizer.

The convective superheater packages are mounted on the hanging pipes of the water economizer.

Convective water economizer packages rest on air-cooled beams.

The water entering the boiler passes through overhead pipes, condensers, wall-mounted water economizer, convective water economizer and enters the drum.

Steam from the drum enters 6 panels of the wall-mounted radiant superheater, from the radiation one enters the ceiling, from the ceiling to the screen, from the screen to the ceiling-wall and then to the convective superheater. The steam temperature is controlled by two injections of its own condensate. The first injection is carried out on all boilers in front of the screen superheater, the second on K-4.5 and the third on 5A injections between the input and output packages of the convective sub-heater, the second injection on K-5A in the cut of the outer and middle screens.

To heat the air necessary for fuel combustion, three regenerative air heaters are installed, located on the rear side of the boiler. The boiler is equipped with two VDN-26 type blower fans. II and two smoke exhausters type DN26x2A.

The combustion chamber of the boiler unit has a prismatic shape. Dimensions of the combustion chamber in the clear:

Width - 14860 mm

Depth - 6080 mm

The volume of the combustion chamber is 1644 m3.

Visible thermal stress of the combustion volume at a load of 480 t/hour: - on gas 187.10 3 kcal/m 3 hour;

On fuel oil - 190.10 3 kcal/m 3 hours.

The combustion chamber is completely shielded by evaporation pipes dia. 60x6 with a pitch of 64mm and overheating pipes. To reduce the sensitivity of circulation to various thermal and hydraulic distortions, all evaporation screens are sectioned, with each section (panel) representing independent circuit circulation.

Boiler burner apparatus.

Name of quantities Unit. measured Gas Fuel oil

1. Nominal performance kg/hour 9050 8400
2. Air speed m/sec 46 46
3. Gas flow rate m/sec 160 -
4. Burner resistance kg/m2 150 150

by air.
5. Maximum productivity - nm 3 / hour 11000

Gas information
6. Maximum production - kg/hour - 10000

ness for fuel oil.
7. Permissible limit of regulation % 100-60% 100-60%

load change. from nominal from nominal
8. Gas pressure in front of the burner. kg/m 2 3500 -
9. Oil pressure before burner - kgf/cm 2 - 20

coy.
10. Minimum pressure drop - - - 7

fuel oil concentration at reduced

load.

Short description burners - GMG type.
The burners consist of the following components:

a) a volute designed for uniform supply of peripheral air to the guide vanes,

b) guide vanes with a register installed at the entrance to the peripheral air supply chamber. Guide vanes are designed to turbulize the peripheral air flow and change its twist. Increasing its twist by covering the guide vanes increases the taper of the torch and reduces its range and vice versa,

c) a central air supply chamber formed with inside pipe surface dia. 219 mm, which simultaneously serves to install a working fuel oil nozzle in it and with outside pipe surface dia. 478 mm, which is also the inner surface of the chamber at the exit to the firebox, has 12 fixed guide vanes (rosette), which are designed to turbulize the air flow directed to the center of the torch.

d) chambers for peripheral air supply, formed on the inside by the surface of a pipe dia. 529 mm, which is both the outer surface of the central gas supply chamber and the outer surface of the pipe dia. 1180mm, which is also the inner surface of the peripheral gas supply chamber,

e) a central gas supply chamber, which has a row of nozzles with a diameter on the side exiting the furnace. 18 mm (8 pcs) and a number of holes dia. 17 mm (16 pcs). Nozzles and holes are located in two rows along the circumference of the outer surface of the chamber,

e) a chamber for peripheral gas supply, which has two rows of nozzles with a diameter on the side exiting the furnace. 25 mm in the amount of 8 pieces and dia. 14 mm in the amount of 32 pcs. The nozzles are located around the circumference of the inner surface of the chamber.

To be able to regulate air flow, the burners are equipped with:

General gate on the air supply to the burner,

Gate on the peripheral air supply,

Gate on the central air supply.

To prevent air from suction into the firebox, a damper is installed on the guide pipe of the fuel oil nozzle.

Description of the steam boiler TGM-151-B

Laboratory work №1

on the course "Boiler installations"

Completed by: Matyushina E.

Pokachalova Yu.

Titova E.

Group: TE-10-1

Checked by: Shatskikh Yu.V.

Lipetsk 2013

1. Purpose of the work……………………………………………………………………………….3

2. Brief characteristics of the TGM-151-B boiler………………………………………………………..….3

3. Boiler and auxiliary equipment……………………………...……………….4

4. Characteristics of equipment……………………………...…………………………7

4.1 Technical characteristics……………………………….………………….7

4.2 Description of design……………………………………..……………….7

4.2.1 Combustion chamber……………………….…..………………………….….7

4.2.2 Superheater……………………...…………………………….8

4.2.3 Device for regulating the temperature of superheated steam………………………………………………………………………………………….…….11

4.2.4 Water economizer…………………...…...………………………......11

4.2.5 Air heater…………………………...………………..…..…12

4.2.6 Draft devices……………………...………………………..…12

4.2.7 Safety valves………………..……………………………13

4.2.8 Burner devices…………………………..………………………..13

4.2.9 Drum and separation devices…………………………………......14

4.2.10 Boiler frame…………....……………………………………………………………16

4.2.11. Boiler lining……….…....………………………………….…….….16

5. Safety precautions during work……………………………………….16

Bibliography………………………..………………………………………………………...17

1. Purpose of the work

Thermal testing of boiler installations is carried out to determine the energy characteristics that determine their operating performance depending on the load and type of fuel, to identify their operational features and design flaws. To instill practical skills in students, it is recommended that this work be carried out in production conditions at existing thermal power plant installations.

The purpose of the work is to familiarize students with the organization and methodology for carrying out balance tests of a boiler unit, determining the number and selection of measurement points for boiler operating parameters, the requirements for installing instrumentation, and the methodology for processing test results.

Brief characteristics of the TGM-151-B boiler

1. Registration number No. 10406

2 Manufacturing plant Taganrog boiler house

Krasny Kotelshchik plant

3. Steam capacity 220 t/h

4. Steam pressure in the drum 115 kg/cm2

5. Nominal pressure of superheated steam 100 kg/cm2

6. Temperature of superheated steam 540 °C

7. Feedwater temperature 215 °C

8. Hot air temperature 340 °C

9. Water temperature at the economizer outlet 320 °C

10. Flue gas temperature 180 °C

11. Main fuel Coke blast furnace gas and natural gas

12 Reserve fuel fuel oil

Boiler and auxiliary equipment.

1. Type of smoke exhauster: D-20x2

Capacity 245 thousand m3/h

Smoke exhaust vacuum - 408 kgf/m2

Power and type of electric motor No. 21 500 kW A13-52-8

No. 22 500 kW A4-450-8

2. Blower type: VDN -18-11

Productivity - 170 thousand m/h

Pressure - 390 kgf/m2

Power and type of electric motor No. 21 200 kW AO-113-6

No. 22 165 kW GAMT 6-127-6

3. Burner type: Turbulent

Number of burners (natural gas) - 4

Number of burners (coke blast furnace gas) 4

Minimum air pressure - 50mm h.st.

Air flow through the burner - 21000 nm/hour

Air temperature in front of the burner - 340 C

Natural gas flow through the burner - 2200 nm/hour

Consumption of coke blast furnace gas through the burner - 25000 nm/hour

Figure 1. Gas-oil boiler TGM-151-B for 220 t/h, 100 kgf/cm^2 (longitudinal and cross sections): 1 – drum, 2 – remote separation cyclone, 3 – combustion chamber, 4 – fuel burner, 5 – screen, 6 – convective part of the superheater, 7 – economizer, 8 – regenerative air heater, 9 – shot catcher (cyclone) of the shot blasting unit, 10 – hopper of the shot blasting unit, 11 – box that removes flue gases from the economizer to the air heater, 12 – gas box to smoke exhauster, 13 – cold air box.

Figure 2. General scheme boiler TGM-151-B: 1 – drum, 2 – remote separation cyclone, 3 – burner, 4 – screen pipes, 5 – lowering pipes, 6 – ceiling superheater, 7 – radiation screen superheater, 8 – convective screen superheater, 9 – 1st stage of convective superheater, 10 – 2nd stage of convective superheater, 11 – 1st injection desuperheater,

12 – 2nd injection desuperheater, 13 – water economizer packages, 14 – regenerative rotating air heater.

4. Equipment characteristics

4.1 Technical characteristics

The TGM-151/B boiler is gas-oil, vertical-water-tube, single-drum, with natural circulation and three-stage evaporation. The boiler was manufactured by the Taganrog boiler plant "Krasny Kotelshchik".

The boiler unit has a U-shaped layout and consists of a combustion chamber, a rotary chamber and a lower convective shaft.

In the upper part of the furnace (at the exit from it), the screen part of the superheater is located in the rotating chamber, and the convective part of the superheater and the economizer are located in the lower gas duct. Two regenerative rotating air heaters (RAH) are installed behind the convective flue.

Operational indicators, parameters:

4.2 Design description

4.2.1 Combustion chamber

The combustion chamber has a prismatic shape. The volume of the combustion chamber is 780 m3.

The walls of the combustion chamber are shielded with pipes Ø 60x5, made of steel 20. The ceiling of the combustion chamber is shielded with pipes of a ceiling superheater (Ø 32x3.5).

The front screen consists of 4 panels - 38 pipes in the outer panels and 32 pipes in the middle ones. The side screens have three panels - each with 30 pipes. The rear screen has 4 panels: the two outer panels consist of 38 pipes, the middle ones - of 32 pipes.

To improve the flushing of screens with flue gases and protect the rear screen cameras from radiation, the rear screen pipes in the upper part form a protrusion into the firebox with an overhang of 2000 mm (along the axes of the pipes). Thirty-four pipes do not participate in the formation of the overhang, but are load-bearing (9 pipes in the outer panels and 8 in the middle ones).

The screen system, except for the rear screen, is suspended from the upper cameras by means of ties to metal structures ceiling. The rear screen panels are suspended using 12 heated hanging pipes 0 133x10 to the ceiling.

The panels of the rear screens in the lower part form a slope towards the front wall of the firebox with a slope of 15° to the horizontal and form a cold floor, covered on the side of the firebox with fireclay and chrome-plated mass.

All firebox screens expand freely downwards.

Figure 3. Sketch of the combustion chamber of a gas-oil boiler.

Figure 4. Screen heating surfaces of the boiler: 1 – drum; 2 – upper collector; 3 – lowering pipe bundle; 4 – lifting evaporation beam; 9 – lower manifold of the rear screen; 13 – mixture drainage pipes of the rear screen; 14 – heating of the screen with a torch of burning fuel.

4.2.2 Superheater

The boiler superheater consists of the following parts (along the steam path): a ceiling superheater, a screen superheater and a convective superheater. The ceiling superheater shields the ceiling of the firebox and rotary chamber. The superheater is made of 4 panels: the outer panels have 66 pipes each, and the middle panels have 57 pipes each. Pipes Ø 32x3.5 mm made of steel 20 are installed with a pitch of 36 mm. The inlet chambers of the ceiling superheater are made of Ø 219x16 mm from steel 20, the outlet chambers are Ø 219x20 mm from steel 20. The heating surface of the ceiling superheater is 109.1 m 2.

The pipes of the ceiling superheater are attached to special beams using welded strips (7 rows along the length of the ceiling superheater). The beams, in turn, are suspended using rods and hangers from the beams of the ceiling structures.

The screen superheater is located in the horizontal connecting gas duct of the boiler and consists of 32 screens located in two rows along the gas flow (the first row is radiation screens, the second is convective screens). Each screen has 28 coils made of pipes Ø 32x4 mm made of steel 12Х1МФ. The pitch between the pipes in the screen is 40 mm. The screens are installed with a pitch of 530 mm. The total heating surface of the screens is 420 m2.

The coils are fastened to each other using combs and clamps (6 mm thick, made of X20N14S2 steel), installed in two rows in height.

A horizontal type convective superheater is located in a lower convective shaft and consists of two stages: upper and lower. The lower stage of the superheater (the first along the steam flow) with a heating surface of 410 m 2 is counterflow, the upper stage with a heating surface of 410 m 2 is direct flow. The distance between the steps is 1362 mm (along the axes of the pipes), the height of the step is 1152 mm. The stage consists of two parts: left and right, each of which consists of 60 double three-loop coils located parallel to the front of the boiler. The coils are made of pipes Ø 32x4 mm (steel 12Х1МФ) and installed in a checkerboard pattern with steps: longitudinal - 50 mm, transverse - 120 mm.

The coils are supported by racks on support beams cooled by air. The spacing of the coils is carried out using 3 rows of combs and strips 3 mm thick.

Figure 5. Fastening of a convective pipe package with horizontal coils: 1 – support beams; 2 – pipes; 3 – racks; 4 – bracket.

The movement of steam through the superheater occurs in two immiscible flows, symmetrically relative to the axis of the boiler.

In each of the streams, the pair moves as follows. Saturated steam from the boiler drum through 20 pipes Ø 60x5 mm enters two collectors of a ceiling superheater Ø 219x16 mm. Next, the steam moves through the ceiling pipes and enters two outlet chambers Ø 219x20 mm, located at the rear wall of the convective flue. From these chambers, four pipes Ø 133x10 mm (steel 12Х1МФ), steam is directed to the inlet chambers Ø 133x10 mm (steel 12Х1МФ) of the outer screens of the convective part of the screen superheater. Next, to the outer screens of the radiation part of the screen superheater, then to the intermediate chamber Ø 273x20 (steel 12X1MF), from which pipes Ø 133x10 mm are directed to the four middle screens of the radiation part, and then to the four middle screens of the convective part.

After the screens, the steam enters a vertical desuperheater through four pipes Ø 133x10 mm (steel 12Х1МФ), after which it is directed through four pipes Ø 133x10 mm into two inlet chambers of the lower counterflow stage of the convective superheater. Having passed the lower stage coils in countercurrent, the steam enters two output chambers (the diameter of the inlet and outlet chambers is Ø 273x20 mm), of which four pipes Ø 133x10 mm are sent to a horizontal desuperheater. After the desuperheater, the steam enters through four Ø 133x10 mm pipes into the Ø 273x20 mm inlet manifolds of the upper stage. Having passed through the upper stage coils in direct flow, the steam enters the output collectors Ø 273x26 mm, from which it is directed through four pipes into the steam collection chamber Ø 273x26 mm.

Figure 6. Diagram of the steam superheater of the TGM-151-B boiler: a – diagram of ceiling panels and screens, b – diagram of convective pipe packages, 1 – drum, 2 – ceiling pipe panels (only one of the pipes is conventionally shown), 3 – intermediate manifold between ceiling panels and screens, 4 – screen, 5 – vertical desuperheater, 6 and 7 – lower and upper convective tube packages, respectively, 8 – horizontal desuperheater, 9 – steam collector, 10 – safety valve, 11 – air vent, 12 – superheated steam outlet .

4.2.3 Device for regulating the temperature of superheated steam

Control of the temperature of superheated steam is carried out in desuperheaters by injecting condensate (or feedwater) into the steam flow passing through them. On the path of each steam flow, two injection-type desuperheaters are installed: one vertical - behind the screen surface and one horizontal - behind the first stage of the convective superheater.

The desuperheater body consists of an injection chamber, a manifold and an outlet chamber. Injection devices and a protective jacket are located inside the housing. The injection device consists of a nozzle, a diffuser and a pipe with a compensator. Diffuser and inner surface the nozzles form a Venturi tube.

In the narrow section of the nozzle, 8 holes Ø 5 mm were drilled on desupercooler II and 16 holes Ø 5 mm on desupercooler I. Steam enters the injection chamber through 4 holes in the desuperheater body and enters the Venturi nozzle. Condensate (feed water) is supplied to the annular channel by a pipe Z 60x6 mm and injected into the cavity of the Venturi pipe through holes Ø 5 mm located around the circumference of the nozzle. After the protective jacket, the steam enters the outlet chamber, from where it is discharged through four pipes to the superheater. The injection chamber and outlet chamber are made of a pipe Ø G g 3x26 mm, the manifold is made of a pipe Ø 273x20 mm (steel 12Х1МФ).

Water economizer

The steel coil economizer is located in the lower gas duct behind the convective superheater packages (along the gas flow). The height of the economizer is divided into three packages, each 955 mm high, the distance between the packages is 655 mm. Each package is made of 88 double three-loop coils Ø 25x3.5 mm (steel20). The coils are located parallel to the front of the boiler in a checkerboard pattern (longitudinal pitch 41.5 mm, transverse pitch 80 mm). The heating surface of the water economizer is 2130 m2.

Figure 7. Sketch of an economizer with a double-sided parallel front arrangement of coils: 1 – drum, 2 – water bypass pipes, 3 – economizer, 4 – inlet collectors.

Air heater

The boiler unit is equipped with two regenerative rotating air heaters of type RVV-41M. The air heater rotor consists of a shell Ø 4100 mm (height 2250 mm), a hub Ø 900 mm and radial ribs connecting the hub to the shell, dividing the rotor into 24 sectors. The rotor sectors are filled with heating corrugated steel sheets (packing). The rotor is driven by an electric motor with a gearbox and rotates at a speed of 2 revolutions per minute. The total heating surface of the air heater is 7221 m2.

Figure 8. Regenerative air heater: 1 – rotor shaft, 2 – bearings, 3 – electric motor, 4 – packing, 5 – outer casing, 6 and 7 – radial and peripheral seal, 8 – air leakage.

Draft devices

To evacuate flue gases, the boiler unit is equipped with two double-suction smoke exhausters of type D-20x2. Each smoke exhauster is driven by an electric motor with a power of N = 500 kW, with a rotation speed of n = 730 rpm.

The performance and total pressure of smoke exhausters are given for gases at a pressure of 760 mm Hg. Art. and gas temperature at the entrance to the smoke exhauster is 200° C.

Nominal parameters at highest efficiency η=0.7

To supply the combustion air necessary for combustion into the furnace, boiler No. 11 is equipped with two blower fans (DV) of the VDN-18-II type with a capacity of Q = 170,000 m 3 /hour, a total pressure of 390 mm of water. Art. at a temperature working environment 20° C. The fans of boiler No. 11 are driven by electric motors: left - 250 kW, rotation speed n=990 rpm, right - 200 kW, rotation speed n=900 rpm.

4.2.7 Safety valves

On boiler No. 11, two pulse safety valves are installed on the steam collection chamber. One of them - control - with an impulse from the steam collection chamber, the second - working - with an impulse from the boiler drum.

The control valve is set to operate when the pressure in the steam collection chamber increases to 105 kgf/cm 2 . The valve closes when the pressure drops to 100 kgf/cm2.

The working valve opens when the pressure in the drum increases to 118.8 kgf/cm 2 . The valve closes when the pressure in the drum drops to 112 kgf/cm2.

4.2.8 Burner devices

There are 8 gas-oil burners installed on the front wall of the combustion chamber, arranged in two tiers of 4 burners in each tier.

Combined burners are made of two-flow air.

Each burner of the lower tier is designed to burn a mixture of coke and blast furnace gases and fuel oil, and separate combustion of coke or blast furnace gases in the same burners. The coke blast mixture is fed through a Ø 490 mm manifold. Along the axis of the burner there is a pipe Ø 76x4 for installing an oil nozzle for mechanical atomization. The diameter of the embrasure is 1000 mm.

Each of the 4 upper tier burners is designed to burn natural gas and fuel oil. Natural gas supplied through a manifold Ø 206 mm through 3 rows of holes Ø 6, 13, 25 mm. The number of holes is 8 in each row. The diameter of the embrasure is 800 mm.

4.2.9 Drum and separation devices

The boiler is equipped with a drum with a diameter of 1600 mm, drum wall thickness 100 mm, sheet steel

The boiler has a three-stage evaporation scheme. The first and second evaporation stages are organized inside the drum, the third in external cyclones. The first stage compartment is located in the middle of the drum, two second stage compartments are at the ends. Inside the drum, the water volumes of the salt compartments are separated from the clean compartment by partitions. The feed water for the salty compartments of the second stage is the boiler water of the clean compartment, which enters through the holes in the dividing intercompartment partitions. The feed water for the third evaporation stage is the boiler water of the second stage.

Continuous blowing is carried out from the water volume of remote cyclones.

Feedwater entering the drum from the economizer is divided into two parts. Half of the water is directed through the pipes into the water space of the drum, the second half is introduced into the longitudinal distribution manifold, exits it through the holes and spreads over the perforated sheet through which it passes saturated steam. When steam passes through the feedwater layer, it is washed, i.e. purification of steam from the salts it contains.

After washing the steam, the feed water is drained through boxes into the water space of the drum.

The steam-water mixture, entering the drum, passes through 42 separation cyclones, of which: 14 are located on the front side of the drum, 28 are located on the rear side of the drum (including 6 cyclones stopped in the salt compartments of stepwise evaporation).

In cyclones, rough, preliminary separation of water and steam is carried out. The separated water flows into the lower part of the cyclones, under which trays are installed.

Directly above the cyclones there are louvered shields. Passing through these shields and through the perforated sheet, the steam is directed for final drying into the upper louvered shields, under which the perforated sheet is located. The middle level in the clean compartment is located 150 mm below its geometric axis. Upper and lower permissible levels respectively 40 mm above and below average. The water level in salty compartments is usually lower than in the clean compartment. The difference in water levels in these compartments increases with increasing boiler load.

The phosphate solution is introduced into the drum into a clean staged evaporation compartment through a pipe located along the bottom of the drum.

The clean compartment has a pipe for emergency drainage of water in case of excessive rise in water level. In addition, there is a line with a valve connecting the space of the left remote cyclone to one of the lower chambers of the rear screen. When the valve is opened, boiler water moves from the salty compartment of the third stage into the clean compartment, due to which it is possible, if necessary, to reduce the salt content of water in the compartments. Leveling the salt content in the left and right salty compartments of the third stage of evaporation is ensured by the fact that a pipe comes out of each salty remote compartment, which directs boiler water to the lower screen chamber of the opposite salty compartment.

Figure 11. Scheme of three-stage evaporation: 1 – drum; 2 – remote cyclone; 3 – lower collector of the circulation circuit, 4 – steam generating pipes; 5 – lowering pipes; 6 – feed water supply; 7 – removal of purge water; 8 – water transfer pipe from the drum to the cyclone; 9 – steam transfer pipe from the cyclone to the drum; 10 – steam pipe from the unit; 11- intratympanic septum.

4.2.10 Boiler frame

The boiler frame consists of metal columns related horizontal beams, trusses, braces and serves to absorb loads from the weight of the drum, heating surfaces, lining, service chimes, gas pipelines and other elements of the boiler. The columns of the boiler frame are rigidly attached to the iron foundation of the boiler, and the bases (shoes) of the columns are poured with concrete.

4.2.11 Brickwork

Sheets of lining are layers of fire-resistant and insulating materials, which are attached using brackets and tie rods to a steel frame structure with cladding sheets.

In the panels, sequentially on the gas side, there are: layers of refractory concrete, sovelite mats, a layer of sealing coating. The thickness of the combustion chamber lining is 200 mm, in the area of the two lower economizer packages – 260 mm. The lining of the hearth in the lower part of the combustion chamber is made in a pipe manner. During thermal elongation of the screens, this lining moves along with the pipes. Between the movable and stationary parts of the combustion chamber lining there is an expansion joint sealed with a water seal (hydraulic seal). The lining has holes for manholes, hatches and hatches.

5. Safety precautions during work

On the territory of the power plant, students are subject to all safety and security rules in force at the enterprise.

Before the start of the tests, a representative of the enterprise briefs the students on the procedure for conducting the test and on safety rules, which are recorded in the relevant documents. During tests, students are prohibited from interfering with the actions of maintenance personnel, turning off devices on the control panel, opening peepholes, hatches, manholes, etc.

Bibliography

Sidelkovsky L.N., Yurenev V.N. Boiler installations of industrial enterprises: Textbook for universities. – 3rd ed., revised. – M.: Energoatomizdat, 1988. – 528 p., ill.
Kovalev A.P. and others. Steam generators: a textbook for universities / A.P. Kovalev, N.S. Leleev, T.V. Vilensky; Under general ed. A. P. Kovalev. – M.: Energoatomizdat, 1985. – 376 p., ill.
Kiselev N.A. Boiler installations, Training manual for preparation. workers in production - 2nd ed., revised. and additional – M.: Higher School, 1979. – 270 pp., ill.
Deev L.V., Balakhnichev N.A. Boiler installations and their maintenance. Practical classes for vocational schools. – M.: Higher School, 1990. – 239 p., ill.
Meyklyar M.V. Modern boiler units TKZ. – 3rd ed., revised. and additional – M.: Energy, 1978. - 223 p., ill.

The TGM-84 boiler unit is designed according to a U-shaped layout and consists of a combustion chamber, which is an ascending gas duct, and a lower convective shaft, divided into 2 gas ducts. There is practically no transitional horizontal gas duct between the firebox and the convective shaft. A screen steam superheater is located in the upper part of the firebox and the rotating chamber. In a convective shaft, divided into 2 gas ducts, a horizontal steam superheater and a water economizer are placed in series (along the flow of gases). Behind the water economizer there is a rotating chamber with ash collection bins.

Two regenerative air heaters connected in parallel are installed behind the convective shaft.

The combustion chamber has the usual prismatic shape with dimensions between the axes of the pipes 6016 * 14080 mm and is divided by a two-light water screen into two half-fireboxes. The side and rear walls of the combustion chamber are shielded with evaporation pipes with a diameter of 60 * 6 mm (steel-20) with a pitch of 64 mm. The side screens in the lower part have slopes towards the middle in the lower part at an angle of 15 to the horizontal and form a “cold” floor.

The two-light screen also consists of pipes with a diameter of 60 * 6 mm with a pitch of 64 mm and has windows formed by pipe routing to equalize the pressure in the half-furnaces. The screen system is suspended from the metal structures of the ceiling using rods and has the ability to freely fall down during thermal expansion.

The ceiling of the combustion chamber is made horizontal and shielded by the pipes of the ceiling superheater.

A combustion chamber equipped with 18 oil burners, which are located on the front wall in three tiers. The boiler has a drum with an internal diameter of 1800 mm. The length of the cylindrical part is 16200 mm. In the boiler drum, separation and steam washing with feed water is organized.

Schematic diagram of steam superheaters

The superheater of the TGM-84 boiler is radiation-convective in nature of heat perception and consists of the following three main parts: radiation, screen or semi-radiation and convective.

The radiation part consists of a wall and ceiling superheater.

The semi-radiation superheater consists of 60 standardized screens. The horizontal type convective superheater consists of 2 parts located in 2 gas ducts of the lower shaft above the water economizer.

A wall-mounted superheater is installed on the front wall of the combustion chamber, made in the form of six transportable blocks of pipes with a diameter of 42*55 (steel 12*1MF).

The outlet chamber of the ceiling substation consists of 2 manifolds welded together, forming a common chamber, one for each semi-furnace. The output chamber of the combustion chamber is one and consists of 6 manifolds welded together.

The inlet and outlet chambers of the screen superheater are located one above the other and are made of pipes with a diameter of 133 * 13 mm.

The convective superheater is made according to a Z-shaped design, i.e. steam enters from the front wall. Each substation consists of 4 single-pass coils.

Devices for regulating steam superheat temperature include condensing unit and injection desuperheaters. Injection desuperheaters are installed in front of the screen superheaters in the screen section and in the convective superheater section. When operating on gas, all desuperheaters operate; when operating on fuel oil, only the one installed in the convective subcooler section.

The steel coil water economizer consists of 2 parts located in the left and right flue ducts of the convection shaft.

Each part of the economizer consists of 4 packages in height. Each package contains two blocks, each block contains 56 or 54 four-way coils made of pipes with a diameter of 25 * 3.5 mm (steel 20). The coils are located parallel to the front of the boiler in a checkerboard pattern with a pitch of 80 mm. The economizer collectors are placed outside the convective shaft.

The boiler is equipped with 2 regenerative rotating air heaters RVP-54.

M. A. Taimarov, A. V. Simakov

RESULTS OF MODERNIZATION AND INCREASE TESTS

THERMAL POWER OF THE TGM-84B BOILER

Key words: steam boiler, testing, thermal power, nominal steam output, gas falling holes.

The work experimentally showed that the design of the TGM-84B boiler makes it possible to increase its steam production by 6.04% and bring it to 447 t/h by increasing the diameter of the gas supply holes of the second row on the central gas supply pipe.

Keywords: the Steam caldron, test, heat power, nominal capacity, gas giving holes.

In work experimentally is obtained, that the construction of the boiler TGM-84B allows to increase it Potency at 6.04% and to finish it up to 447 t/h by magnification of a diameter Gas pipe of orifices of the second number on central Gas pipe.

Introduction

The TGM-84B boiler was designed and manufactured 10 years earlier, compared to the TGM-96B boiler, when the Taganrog Boiler Plant did not have much practical and design experience in the design, manufacture and operation of high-performance boilers. In this regard, a significant reserve of area of heat-receiving screen heating surfaces was made, which, as all experience in operating TGM-84B boilers has shown, is not necessary. The performance of burners on TGM-84B boilers was also reduced due to the smaller diameter of the gas outlet holes. According to the first factory drawing of the Taganrog Boiler Plant, the second row of gas outlets in the burners are provided with a diameter of 25 mm, and later, based on operating experience to increase the thermal intensity of the furnaces, this diameter of the second row of gas outlets was increased to 27 mm. However, there is still room to increase the diameter of the gas outlet openings of the burners in order to increase the steam production of TGM-84B boilers.

Relevance and statement of the research problem

In the near future, the demand for thermal and electrical energy will sharply increase for 5...10 years. The growth in energy consumption is associated, on the one hand, with the use of foreign technologies for advanced processing of oil, gas, wood, and metallurgical products directly on the territory of Russia, and on the other, with the retirement and reduction of power due to the physical wear and tear of the existing fleet of heat and power generating equipment. The consumption of thermal energy for heating purposes is increasing.

There are two ways to quickly meet the growing need for energy resources:

1. Introduction of new heat and electricity generating equipment.

2. Modernization and reconstruction of existing operational equipment.

The first direction requires large investments.

In the second direction of increasing the power of heat and electricity generating equipment, costs are associated with the volume of necessary reconstruction and additions to increase power. On average, when using the second direction of increasing the capacity of heat and electricity generating equipment, the costs are 8 times cheaper than commissioning new capacities.

Technical and design possibilities for increasing the power of the TGM-84 B boiler

A design feature of the TGM-84B boiler is the presence of a two-light screen.

The double-light screen provides more intensive cooling of the flue gases than in the TGM-9bB gas-oil boiler of similar performance, which does not have a double-light screen. The dimensions of the furnaces of the TGM-9bB and TGM-84B boilers are almost the same. Design versions, with the exception of the presence of a two-light screen in the TGM-84B boiler, are also identical. The nominal steam output of the TGM-84B boiler is 420 t/hour, and for the TGM-9bB boiler the nominal steam output is 480 t/hour. The TGM-9b boiler has 4 burners in two tiers. The TGM-84B boiler has 6 burners in 2 tiers, but these burners are less powerful than the TGM-9bB boiler.

The main comparative technical characteristics of the TGM-84B and TGM-9bB boilers are given in Table 1.

Table I - Comparative technical characteristics of the TGM-84B and TGM-96B boilers

Name of indicators TGM-84B TGM-96B

Steam capacity, t/h 420 480

Combustion volume, m 16x6.2x23 16x1.5x23

Dual-light screen Yes No

Nominal thermal power of the burner when burning gas, MW 50.2 88.9

Number of burners, pcs. b 4

Total thermal power of burners, MW 301.2 355.6

Gas consumption, m3/hour 33500 36800

Nominal gas pressure in front of the burners at gas temperature (t = - 0.32 0.32

4 °C), kg/cm2

Air pressure in front of the burner, kg/m2 180 180

Required air flow for blasting at nominal steam 3/ load, thousand m / hour 345.2 394.5

Required performance of smoke exhausters at rated steam 3 / 399.5 456.6

load, thousand m/hour

Certified nominal total capacity of 2 blower fans VDN-26-U, thousand m3/hour 506 506

Certified nominal total capacity of 2 smoke exhausters D-21.5x2U, thousand m3/hour 640 640

From the table 1 shows that the required steam load of 480 t/h in terms of air flow is provided by two VDN-26-U fans with a margin of 22%, and in terms of removing combustion products by two D-21.5x2U smoke exhausters with a margin of 29%.

Technical and Constructive decisions to increase the thermal power of the TGM-84B boiler

At the Department of Boiler Installations of Kazan State Power Engineering University, work was carried out to increase the thermal power of the TGM-84B boiler st. No. 10 NchCHPP. Thermal-hydraulic calculation was carried out

burners with central gas supply, aerodynamic and thermal calculations were performed with an increase in the diameter of the gas supply holes.

On the TGM-84B boiler with station No. 10, on burners No. 1,2,3,4 of the first (lower) tier and No. 5,6 of the second tier, 6 of the existing 12 gas outlet holes were drilled out (evenly around the circumference through one hole) 2- 1st row from diameter 027 mm to diameter 029 mm. The incident flows, flame temperature and other operating parameters of boiler No. 10 were measured (Table 2). The unit thermal power of the burners increased by 6.09% and amounted to 332.28 MW instead of 301.2 MW before drilling. Steam output increased by 6.04% and amounted to 447 t/hour instead of 420 t/hour before drilling.

Table 2 - Comparison of indicators of the TGM-84B boiler st. No. 10 NchCHPP before and after burner reconstruction

Indicators of the boiler TGM-84B No. 10 NchCHPP Hole diameter 02? Hole diameter 029

Thermal power one burner, MW 50.2 55.58

Thermal power of the furnace, MW 301.2 332.28

Increase in thermal power of the furnace,% - 6.09

Boiler steam output, t/hour 420 441

Increase in steam output,% - 6.04

Calculations and tests of modernized boilers have shown that there is no separation of the gas jet from the gas supply openings at low steam loads.

1. Increasing the diameter of the gas supply holes of the 2nd row from 27 to 29 mm on the burners does not cause disruption of the gas flow at low loads.

2. Modernization of the TGM-84B boiler by increasing the cross-sectional area of the gas supply

holes from 0.205 m to 0.218 m made it possible to increase the nominal steam output from 420 t/h to 447 t/h when burning gas.

Literature

1. Taimarov, M.A. High power and supercritical thermal power plant boilers Part 1: tutorial/ M.A. Taimarov, V.M. Taimarov. Kazan: Kazan. state energy univ., 2009. - 152 p.

2. Taimarov, M.A. Burner devices / M.A. Taimarov, V.M. Taimarov. - Kazan: Kazan. state energy univ., 2007. - 147 p.

3. Taimarov, M.A. Laboratory workshop on the course “Boiler installations and steam generators” / M.A. Taimarov. - Kazan: Kazan. state energy univ., 2004. - 107 p.