Compiler: M.V. Kalmykov UDC 621.1 Design and operation of the Boiler TGM-84: Method. Decree / Samar. State tehn un-t; Cost. M.V. Kalmykov. Samara, 2006. 12 s. The main technical characteristics, layout and description of the design of the TGM-84 boiler and the principle of its work are considered. The drawings of the layout of the boiler unit with auxiliary equipment are given, general view Boiler and its nodes. A diagram of the steaming path of the boiler and the description of its work is presented. Methodical instructions are designed for students of the specialty 140101 "Heat electric stations". Il. 4. Bibliogr.: 3 Names. Printed by the decision of the editorial-publishing council SamgTa 0 The main characteristics of the boiler unit Boiler aggregates TGM-84 are designed to obtain steam high pressure When burning gaseous fuel or fuel oil and are designed for the following parameters: Rated steam output ..................................................................................................................... Working For main vapor latch ................ The temperature of the superheated pair .............................................. The temperature of the nutrient water ............................................. The temperature of hot air a) when burning fuel oil ................................................ b) when burning gas .................................................... 420 t / h 155 Ata 140 Ata 550 ° C 230 ° C 268 ° C 238 ° C Boiler unit TGM-84 vertically water-tube, single-backed, puppy layout, with natural circulation. It consists of a flue chamber, which is the ascending gas duct and the lowered convective shaft (Fig. 1). The cooler is divided by a two-switch screen. The lower part of each side screen goes into a slightly inclined sublict screen, the lower collectors of which are attached to the reservoirs of the two-fold screen and are jointly moved with heat deformations during extracts and boiler stops. The presence of a two-fold screen provides more intensive cooling of the fuel gases. Accordingly, the thermal voltage of the flue volume of this boiler was chosen significantly higher than in dust aggregates, but lower than in other sizes of gas-contained boilers. This was facilitated by the working conditions of the pipes of the two-shield, which perceive the greatest amount of heat. In the upper part of the furnace and in the rotary chamber there is a semi-radiative wide steamer. In a convective mine, a horizontal convective steamer and a water economizer are placed. The water economizer has a camera with adopted shotgun bunkers. Two inclied parallel regenerative air heater rotating type RVP-54 are installed after a convective mine. The boiler is equipped with two blowing fans of type VDN-26-11 and two D-21 smoke. The boiler was repeatedly subjected to reconstruction, as a result of which the model TGM-84A appeared, and then TGM-84B. In particular, unified scrolls were introduced and a more uniform distribution of steam between the pipes was achieved. A transverse pitch of pipes was increased in horizontal packages of the convective part of the steam-1 of the superheater, thereby decreased the likelihood of its pollution of fasonry. 2 0 p and s. 1. Longitudinal and transverse sections of the gas-gas boiler TGM-84: 1 - heat chamber; 2 - burners; 3 - drum; 4 - shirma; 5 - convective steamer; 6 - condensation installation; 7 - Economyzer; 11 - shotgun; 12 - Remote separation cyclone The boilers of the first modification of TGM-84 were equipped with 18 gas-gas burners placed in three rows on the front wall of the fiber chamber. Currently establish either four or six burners greater performance, which simplifies the maintenance and repair of boilers. The burner devices The furnace chamber is equipped with 6 gas-gas burners installed in two tiers (in the form of 2 triangles in a row, vertices up, on the front wall). Lower tier burners are set at 7200 mm, upper Yarusa at a mark of 10200 mm. The burners are designed for separate burning of gas and fuel oil, vortex, single-threaded with central gas distribution. The extreme burners of the lower tier are unfolded towards the axis of the semi-powder by 12 degrees. To improve the mixing of fuel with air, the burners have guides, passing that the air is spinning. On the axis of burners on the boilers, fuel oil nozzles with a mechanical spray, the length of the fuel oil nozzle is 2700 mm. The design of the furnace and layout of the burner should provide a steady combustion process, its control, and also exclude the possibility of forming poorly ventilated zones. Gas burners must work steadily, without separation and sprinkle of the torch in the heat load range of the boiler. Gas burners used on boilers should be certified and have a passport of factory manufacturers. The coaching chamber The prismatic chamber is divided into two half-windows. The volume of the furnace chamber is 1557 m3, the heat voltage of the flue volume is 177,000 kcal / m3 ּ hour. The side and rear walls of the chamber are shielded by evaporative pipes with a diameter of 60 × 6 mm in 64 mm increments. The side screens in the lower part have slopes to the middle of the furnace with a slope of 15 degrees to the horizontal and form under. In order to avoid the bundle of a steam mixture in a slightly blocker to horizontal pipes, the portions of the side screens forming under, coated with chamoten brick and chromite mass. The on-screen system with the help of the thrust is suspended to the metal structures of the ceiling overlap and has the ability to freely drop down when thermal expansion. Pipes of evaporative screens were welded with each other with a rod of D-10 mm with an interval at a height of 4-5 mm. To improve the aerodynamics of the top of the furnace chamber and protect the rear screen cameras from radiation, the rear screen pipes in the upper part form a protrusion into the firebox with a departure of 1.4 m. The protrusion is formed by 70% of the rear screen pipes. 3 In order to reduce the influence of uneven heating on circulation, all screens are partitioned. Two-minute and two side screens have three circulation circuits, rear - six. TGM-84 boilers operate on a two-stage evaporation scheme. The first step of evaporation (pure compartment) includes drums, rear panels, two-sweat screens, 1st and 2nd from the front of the side screens panel. The second stage of evaporation (salt compartment) includes 4 remote cyclones (two on each side) and third on the front of the side screens panel. To six lower rear screen cameras, water from the drum is supplied by 18 water pipes, three to each collector. Each of the 6 panels includes 35 screen pipes. The upper ends of the pipes are connected to the cameras, of which the steam mixture comes through 18 pipes into the drum. The two-shield screen has windows formed by laying pipes to equalize the pressure in the half-gun. To the three lower chambers of the two-fold screen, water from the drum comes through 12 water pipes (4 pipes per collector). Extreme panels have 32 screen pipes, Average - 29 pipes. The upper ends of the pipes are connected to the three top cameras, of which the steam mixture of 18 pipes is sent to the drum. To the four front bottom collectors of the side screens, water comes from the drum over 8 water pipes. Each of these panels contains on the 31st screen tube. The upper ends of the on-screen pipes are connected to 4-chambers, of which the steam mixture falls into the drum along 12 pipes. The lower chambers of salt compartments are powered by 4 remote cyclones in 4 water pipes (from each cyclone on one pipe). Packs of salt compartments contain 31 on-screen pipes. The upper ends of the on-screen pipes are connected to the chambers, of which the steam-cutting mixture of 8 pipes enters 4 remote cyclones. The drum and the separation device of the drum has an inner diameter of 1.8 m, length of 18 m. All the drums are made of sheet steel 16 Gnm (manganese-nickemolybdenum steel), the thickness of the wall is 115 mm. The weight of the drum is about 96600 kg. The boiler drum is designed to create a natural circulation of water in the boiler, cleaning and separating the steam obtained in the on-screen pipes. A separation of a steam mixture of the 1st stage of evaporation was organized in the drum (separation of the 2nd stage of evaporation is made on boilers in 4 removal cyclones), flushing of the entire pair is carried out nutrient water Following the capture of moisture from steam. The entire drum is a pure compartment. A steaming mixture from the upper collectors (except for collectors of salt compartments) enters the drum on both sides and enters a special sinking box, from which it is sent to cyclones, where the initial separation of steam from water occurs. In the borants of the boilers, 92 cyclone was installed - 46 left and 46 right. 4 At the exit of steam from cyclones, horizontal plate separators are installed, steam, passing them, enters the barbaste-washing device. Here, under the flushing device of the pure compartment, pairs of remote cyclones were tested, inside which the separation of the steam mixture is also organized. Couple, having passed a barbages and flushing device, enters a holey sheet, where the steam separation and the leveling of the flow occurs simultaneously. Passing a hole leaf, couples 32 steaming pipes are allocated to the input chambers of the wall-mounted steam steamper and 8-pipes to the condensate installation. P and s. 2. Two-stage evaporation scheme with remote cyclones: 1 - drum; 2 - remote cyclone; 3 - lower collector of the circulation circuit; 4 - steam generating pipes; 5 - sink pipes; 6 - supply of nutrient water; 7 - removal of purge water; 8 - water supply tube from drum in cyclone; 9 - par pilot tube from cyclone in the drum; 10 - a steaming pipe from the unit on a barbage-washing device is fed about 50% of the nutrient water, and the rest of it through the distribution collector merges into the drum under the water level. Average level Water in a 200 mm drum below its geometric axis. Permissible level fluctuations in the drum of 75 mm. For the alignment of the saline in salt compartments of the boilers, two waterproof pipes are made, so the right cyclone nourishes the left bottom collector of the salt compartment, and the left nourishes right. 5 The design of the surface of the heating surface of the steamer is placed in a float chamber, a horizontal gas duct and a sink mine. The steamer scheme is made of two-way with repeated stirring and a steam transfer along the width of the boiler, which makes it possible to align thermal sprinkle for individual coins. By the nature of the heat perception, the steamer is conditionally divided into two parts: radiation and convective. The radiation part includes a wall-mounted steamer (NPP), the first series of ShirM (SPP) and a portion of the ceiling steamer (PPP), shielding the ceiling of the coaming chamber. By convective - the second series of shirm, part of the ceiling steamer and convective steamer (PPC). Radiation Wall-mounted NPP Pipe Steamer Shielded Front Wall of the Floor Camera. The NPP consists of six panels, two of them have 48, and the remaining 49 pipes, the step between the pipes is 46 mm. In each panel 22 pipes are lowered, the rest of the lifting. Input and output collectors are located in a non-heated zone above the heat chamber, intermediate collectors - in a non-heated zone below the heat chamber. The upper chambers with the help of thrust are suspended with the ceiling overlap metal structures. The fastening of pipes is carried out in 4 tiers in height and allows vertical movement of panels. Ceiling superheater The ceiling steamer is located above the furnace and horizontal gas duct, consists of 394 pipes placed in 35 mm increments and connected input and output collectors. Shirm Steam-Steel Warmer Steamer consists of two rows of vertical shutters (30 shirm in each row) located in the upper part of the heat chamber and the swivel gas duct. Step between shirms 455 mm. Shirma consists of 23 coils of the same length and two collectors (input and output), installed horizontally in a non-heated zone. Convective steamer Convective horizontal type steamer, consists of the left and right parts located in the gas duct of the hydrocarbon mine over a water economizer. Each party in turn is divided into two straight-flow steps. 6 Steam path of the boiler The saturated pairs of the boiler of the boiler on 12 steamed pipes enters the upper collectors of the NPP, of which 6 panels are moving down and enters 6 bottom collectors, after which it rises up extreme pipes 6 panels to the top Collectors, of which on 12-reheated pipes are sent to the input collectors of the ceiling steamer. Next, steam across the entire width of the boiler moves along the ceiling pipes and enters the output collectors of the steamer, located at the rear wall of the convective gas plant. From these collectors, steam is divided into two streams and is sent to the chambers of the steamers of stage I, and then in the chambers of the extreme shots (7 left and 7 right), passing which both streams of steam fall into intermediate steamers of stage II, left and right. In steamers I and II, steam steam are transferred from the left side to the right and, on the contrary, in order to reduce thermal reassembly caused by gas bumps. Coming out of the intermediate vaporochlastors of the II injection, the pairs enters the medium-sized collectors (8 left and 8 right), passing which is sent to the PPC input chambers. Between the upper and lower parts of the gearbox, steamers of stage III are installed. Next, overheated steam on steam pipeline is sent to turbines. P and s. 3. Boiler steamer scheme: 1 - boiler drum; 2 - radiation two-way radiation tube panel (left conditionally shown upper collectors, and on the right - lower); 3 - ceiling panel; 4-lady pairoker; 5 - water injection location in pairs; 6 - extreme screens; 7 - average screen; 8 - convective packages; 9 - Couple out of boiler 7 Condensate installation and injection steamers To obtain your own condensate on the boiler, 2 condensate installations are installed (one on each side) located on the ceiling overlap of the boiler over the convective part. They consist of 2 distributing collectors, 4 capacitors and condensate collectors. Each condenser consists of a chamber D426 × 36 mm. The cooling surfaces of the capacitors are formed by pipes welded to the tubular board, which is divided into two parts and forms a drainage and water supply chamber. A saturated pair of boiler drum on 8 pipes is sent to four distributing collectors. Each collector pairs are allocated to two capacitors of pipes of 6 tubes to each condenser. The condensation of a saturated steam coming from the boiler borax is made by cooling it with nutrient water. Nutrient water after a suspended system is fed to the water-powered chamber, passes through the tubes of capacitors and goes into the drainage of the chamber and further to the water economizer. A saturated steam received from the drum fills the steam space between the pipes, comes into contact with them and condenses. The resulting condensate on the 3rd tubes from each condenser enters two collections, from there through regulators is supplied to the pairochholders I, II, III of the left and right injections. Condensate injection occurs at the expense of the head of the spelling out of the difference in the Venturi tube and the pressure drop in the steam path of the steamer from the drum to the injection site. Condensate is injected into the cavity of the tube "Venturi" through 24 holes with a diameter of 6 mm, located around the circle in a narrow place of the pipe. The Venturi tube at full load on the boiler reduces the pair pressure by increasing its speed at the injection site by 4 kgf / cm2. The maximum capacity of one capacitor at 100% load and calculated parameters of steam and nutrient water is 17.1 t / h. Water economizer steel coating water economizer consists of 2 parts placed respectively in the left and right side of the sink shaft. Each part of the economizer consists of 4 blocks: lower, 2 medium and top. In height between blocks made openings. Water economizer consists of 110 packages of coils located in parallel to the front of the boiler. The coils in the blocks are located in a checkerboard with a step of 30 mm and 80 mm. Medium and upper blocks are installed on the beams located in the gas duct. To protect against the gas medium, these beams are covered with insulation protected by metal sheets with a thickness of 3 mm from the effects of the shot blasting. Lower blocks with racks suspended to beams. Racks allow removing the package of coils during repair. 8 The inlet and output chambers of the water economizer are located outside the gas ducts and brackets attached to the boiler frame. Cooling the beams of a water economizer (the temperature of the beams during trails and during operation should not be more than 250 ° C) due to the supply of cold air from the head of blowing fans, with air discharge into suction box of blowing fans. The air heater in the boiler room was installed two regenerative air heater RVP-54. The RVP-54 regenerative air heater is a countercurrent heat exchange unit consisting of a rotator rotor concluded inside a fixed body (Fig. 4). The rotor consists of a shell with a diameter of 5590 mm and a height of 2250 mm made from sheet steel with a thickness of 10 mm and a hub with a diameter of 600 mm, as well as connecting the hub with a shell of radial ribs separating the rotor on 24 sectors. Each sector is divided by vertical sheets on P and C. 4. Constructive diagram of regenerative air heater: 1 - box; 2 - drum; 3 - body; 4 - packing; 5 - shaft; 6 - Bearing; 7 - seal; 8 - electric motor three parts. They are stacked by the sections of the heating sheets. In the height of the section are installed in two rows. The upper row is a hot part of the rotor, made of distinguishing and corrugated sheets, 0.7 mm thick. The lower series of sections is a cold part of the rotor and is made of distinguishing direct sheets, 1.2 mm thick. The cold part is more susceptible to corrosion and can be easily replaced. Inside the hub of the rotor passes a hollow tree, having a flange on the bottom, which relies the rotor, the hub is attached to the flange with studs. RVP has two covers - the upper and lower, they have sealing plates. 9 The heat exchange process is carried out by heating the rotor packing in the gas stream and its cooling in the air flow. The sequential movement of the heated gas flow to the air is carried out due to the rotation of the rotor with a frequency of 2 turns per minute. At each moment of time, from 24 sectors of the rotor 13 sectors included in the gas tract, 9 sectors - in the air tract, two sectors are turned off and overlapped with sealing plates. In the air heater, the principle of counterflow is carried out: the air is entered from the outlet side and is removed from the part side of the gases. The air heater is designed for heating air from 30 to 280 ° C when the gases are cooling from 331 ° C to 151 ° C when working on fuel oil. The advantage of regenerative air heaters is their compactness and a small mass, the main disadvantage is a significant air punch from the air side into the gas (regulatory air suppression 0.2-0.25). The frame of the boiler The boiler frame consists of steel columns associated with horizontal beams, farms and disconsets, and serves to perceive loads from the weight of the drum, all surfaces of heating, condensate installation, irrigation, insulation and maintenance sites. The frame of the boiler is made by welded from profile rental and sheet steel. The columns of the frame are attached to the underground reinforced concrete foundation of the boiler, the base (shoe) columns are poured with concrete. Cutting Camera icing consists of refractory concrete, collateral plates and sealing magnesiac coating. Claiming thickness 260 mm. It is installed in the form of shields that are attached to the boiler frame. Ceiling icon consists of panels, 280 mm thick, freely lying on the pipes of the steamer. The structure of the panels: a layer of refractory concrete 50 mm thick, a layer of thermal insulation concrete with a thickness of 85 mm, three layers of constructive slabs, a total thickness of 125 mm and a layer of sealing magnesial coating, a thickness of 20 mm applied to metal grid. The irrigation of the rotary chamber and the convective mines are attached on the shields, which in turn are attached to the boiler frame. The overall thickness of the rotary chamber is 380 mm: refractory concrete - 80 mm, thermal insulation concrete - 135 mm and four layers of context plates of 40 mm. The convection of the convective steamer consists of one layer of thermal insulation concrete with a thickness of 155 mm, a layer of refractory concrete - 80 mm and four layers of collateral plates - 165 mm. Between the plates is a layer of suspended mass10 ticks 2 ÷ 2.5 mm thick. The watelling of the water economizer with a thickness of 260 mm, consists of refractory and thermal insulating concrete and three layers of collateral plates. Safety measures The operation of boiler units should be carried out in accordance with the existing "rules of the device and the safe operation of steam and water boilers" approved by Rostechnadzor and " Technical requirements According to the explosion safety of boiler installations operating on fuel oil and natural gas, "as well as operating" safety regulations for servicing the heat-power equipment of power plants ". Bibliographic list 1. Instructions for the operation of the energy boiler TGM-84 CHP VAZ. 2. Maclar M.V. Modern boiler aggregates TKZ. M.: Energia, 1978. 3. Kovalev A.P., Leleev N.S., Vilensky T.V. Steam generators: Tutorial for universities. M.: Energoatomizdat, 1985. 11 Design and work of the Boiler TGM-84 Compiler Kalmykov Maxim Vitalevich Editor N.V. In the e p and n and n and technical editor of G.N. W and H L to about and signed in print 06/20/06. Format 60 × 84 1/12. Offset paper. Print offset. Usl.l. 1.39. Sl.Kr.-Ott. 1.39. Ud. l. 1.25 Circulation 100. S. - 171. ____________________________________________________________________________________________________ educational institution Higher vocational education "Samara State Technical University" 432100. G. Samara, ul. Young Guard, 244. Main Corps 12
Students, graduate students, young scientists who use the knowledge base in their studies and work will be very grateful to you.
Federal Agency for Education
State educational institution
higher professional education
"Ural State Technical University - UPI
Name of the first president of Russia B.N. Yeltsin "-
branch in Mizhneuralsk
Specialty: 140101
Group: TPP -441
Course project
Thermal Calculation of the Boiler Aggregate TGM - 96
Under the discipline "Boiler installations of the TPP"
Teacher
Dalkova Nina Pavlovna
Kashurin Anton Vadimovich
mr. Sredneuralsk
1. On the course project
2. a brief description of And the parameters of the boiler TGM-96
3. Outlet air coefficients, volumes and enthalpy products combustion
4. The thermal calculation of the boiler unit:
4.1 Thermal balance and calculation of fuel
4.2 Regenerative air heater
but. Cold
b. Hot part
4.4 Weekend Shirm
4.4 Input Shirma
Bibliography
1. Task for a course project
For the calculation, the drum boiler unit TGM - 96 is accepted.
Task source data
Parameters of the boiler TGM - 96
· Step-view of the boiler - 485 t / h
· Pressure overheated steam at the outlet of the boiler - 140 kgf / cm 2
· Preheated paragraph temperature - 560 єС
· Operating pressure in the boiler drum - 156 kgf / cm 2
· Nutrient temperature on the entrance to the boiler - 230 ° C
· Pressure of nutrient water to the entrance to the boiler - 200 kgf / cm 2
· Cold air temperature at the entrance to RVP - 30 ° C
2 . Description of the thermal circuit
Nutrient boiler is condensate turbines. Which is condensate pump sequentially through the main ejector, the ejector of the seals, the gland heater, PND-1, PND-2, PND-3 and PND-4 is heated to a temperature of 140-150 ° C and is fed to Deaarators 6 at. In Deaaerators, separation of gases dissolved in condensate (deaeration) and additional heating to a temperature of about 160-170 ° C. The condensate from deaerators is signed by the sickness of nutritional pumps, after which the pressure is raised to 180-200 kgf / sm and nutrient water through the PVD-5, PVD-6, and PVD-7 adjusted to a temperature of 225-235 ° C. Power knot boiler. Behind the power regulator of the boiler pressure sits up to 165 kgf / sm and is served in a water economizer.
Nutrient water through 4 chambers D 219x26 mm enters the suspended pipes D 42x4.5 mm of Article 20, located in a step of 83 mm in 2 rows in each half of the gas plant. The output chambers of the suspended pipes are located inside the gas pipe, are suspended with 16 pipes D 108x11 mm Article 20 of the chambers of water 12 pipes D 108x11 mm are supplied to 4 condensers and further to the wall economizer panel. At the same time, the streams are transferred on one side to another. The panels are made of pipes D28x3.5 mm of Article 20 and shielded side walls and a skattop camera.
Water passes two parallel streams through the upper and lower panels, sent to the input cameras of the convective economize.
The convective economizer consists of the upper and lower packets, the lower part is made in the form of coils from the pipes with a diameter of 28x3.5 mm. 20, located in a checker, in 80x56 mm increments. It consists of 2 parts located in the right and left risks. Each part consists of 4 blocks (2 upper and 2nge). The movement of water and flue gases in a convective economizer is counter-flow. When working on gas, the economizer has 15% of boiling. The separation of the steam generated in the economiser (the economizer has 15% of boiling when working on gas) occurs in a special paore separation box with labyrinth hydrotherap. Through the hole in the box, the constant amount of nutrient water, regardless of the load, together with the ferry is supplied to the volume of the drum under flushing shields. Resetting water from flushing panels is carried out using drain boxes.
A steam-cutting mixture from the screens via steaming pipes enters the distributing boxes, and then into vertical separation cyclones, where primary separation occurs. In the pure compartment, 32 double and 7 single cyclones were installed, in the salt 8 - to 4 for each side. In order to avoid couples from cyclones in lower pipes under all cyclones, a box is installed. The water separated in cyclones flows down into the water volume of the drum, and the pairs along with some moisture rises upwards, passing by the reflective cover of the cyclone enters the flushing device, which consists of horizontal hole shields to which 50% of nutrient water is supplied. Couple passing through the layer of the washing device gives it the main amount of silicon salts contained in it. After the washing device, the pairs passes through the louvre separator and is additionally cleaned from moisture droplets, and then through a hole ceiling shield, leveling the velocity field in the steam space of the drum, enters the steamer.
All separation elements are collapsed and fastened with wedges that are grabbed by welding to the details of separation.
The average water level in the drum below the middle of the average watercase glass is 50 mm and 200 mm below the geometric center of the drum. The upper permissible level + 100mm, the lower permissible - 175 mm on the water glass.
For heating the body of the drum during extracts and disconnecting when the boiler is stopped, a special device for the UTE project is mounted. Couples in this device are served from a nearby working boiler.
The saturated pairs of drums with a temperature of 343 ° C enters in 6 panels of the radiation superheater and heated to a temperature of 430 ° C, after which it is heated to 460-470 ° C in 6 panels of the ceiling steamer.
In the first steamer, the temperature of the pair decreases to 360-380 ° C. Before the first steamers, the steam stream is divided into two streams, and after them to level the temperature scan, the left stream of the pair is transferred to right side, and right - in the left. After the transfer, each flow pair enters 5 input cold shirms, behind them in 5 outlet cold shirm. In these shirms, steam moves countercurrent. Next, the direct flow of the pairs enters the 5 hot input shirms, behind them in 5 weekend hot shirm. Cold shirms are located with book boilers, hot - in the center. Steam temperature in Shirmah 520-530 ° C.
Further, 12 steam steamed pipes D 159x18 mm Article 12x1mf pairs enters the input package of convective steamer, where it is heated to 540-545 ° C. In the event of an increase in temperature, the second injection enters the operation. Next, through the bypass pipeline D 325x50 st. The 12x1mf enters the Output Package of the CAT, where the temperature increase is 10-15 ° C. After him, the pairs enters the output collector of the CAT, which towards the front of the boiler goes to the main steam line, and in the rear section, 2 main workflows of safety valves are mounted.
To remove salts dissolved in boiler water, produce a continuous blowing from the boiler drum, the regulation of the continuous purge value is carried out on the task of the head of the shift of Himsch. To remove the sludge from the lower collectors, the screens produce a periodic blowing of the lower points. To prevent education in the Calcium scale boiler to produce phosphating of boiler water.
The amount of phosphate administered is regulated by a senior machinist on the task of the head of the shift of Himsech. To bind free oxygen and the formation of the passivating (protective) film on the inner surfaces of the boiler pipes, to dosing hydrazine into nutrient water, maintaining its excess 20-60 μg / kg. The dosing of hydrazine into nutrient water produces a turbine branch personnel on the task of the head of the shift of Himsech.
To utilize the heat of continuous purging boilers P Och. 2 sequentially included continuous purge expansion enabled.
Expander 1 tbsp. It has a volume of 5000 liters and is designed for a pressure of 8 at a temperature of 170 ° C, the parameter is directed to the collector of heating steam 6 at, the separation through the condensing pot into the expander P Och.
Expander PA. It has a volume of 7,500 liters and is designed for a pressure of 1.5 at the temperature of the medium of 127 ° C, you are sent to the NDU and is connected in parallel to the strip of drainage expander and the pipeline of the reduced pair of rabid row. The expander's separator is directed through the hydraulic table with a height of 8 m in the sewer. Submission of drainage expanders PA. The scheme is prohibited! For emergency plum from boilers. and purging the lower points of these boilers in KTC-1 2 parallel to the extender of 7500 liters each and calculated pressure of 1.5 ATA are installed. The disparal of each periodic purge expander according to the pipelines with a diameter of 700 mm without shut-off reinforcement is directed to the atmosphere and is removed on the roof of the boiler shop. The separation of the steam generated in the economiser (the economizer has 15% of boiling when working on gas) occurs in a special paore separation box with labyrinth hydrotherap. Through the hole in the box, the constant amount of nutrient water, regardless of the load, together with the ferry is supplied to the volume of the drum under flushing shields. Reset water with flushing shields is carried out using drain boxes
3 . Outlet air coefficients, volumes and enthalpyproducts combustion
Calculated Gaseous Fuel Characteristics (Table II)
Output of air excess aircraft:
· Outlet air coefficient at the outlet of the furnace:
t \u003d 1.0 +? T \u003d 1.0 + 0.05 \u003d 1.05
·? Excess air coefficient for PPC:
PPP \u003d T +? PPP \u003d 1.05 + 0.03 \u003d 1.08
· Excess air coefficient for IE:
WE \u003d PPP +? VE \u003d 1.08 + 0.02 \u003d 1,10
· Excess air coefficient for RVP:
RVP \u003d WE +? RVP \u003d 1,10 + 0.2 \u003d 1.30
Characteristics of combustion products
|
The calculated value |
Dimension |
V ° \u003d9,5 2 |
V ° H2O= 2 , 10 |
V ° N2. = 7 , 6 0 |
V. Ro2.=1, 04 |
V ° g \u003d 10, 73 |
|
|
G a z o x o d s |
|||||||
|
Flak |
Wow Gaza |
||||||
|
Outlet air coefficient ,? ? |
|||||||
|
Outlet air coefficient, medium? cf. |
|||||||
|
V h2o \u003d v ° h2o + 0,0161 * (? -1) * v ° |
|||||||
|
V r \u003d v ro2 + v ° n2 + v h2o + (? -1) * v ° |
|||||||
|
r RO2 \u003d V RO2 / V g |
|||||||
|
r h2o \u003d v h2o / v g |
|||||||
|
rn \u003d R RO2 + R H 2O |
· Theoretical air
V ° \u003d 0.0476 (0.5Co + 0.575n 2 O + 1.5H 2 S + y (M + N / 4) C M H n - O P)
· Theoretical volume of nitrogen
· Theoretical volume of water vapor
· Volume of trochaty gases
Enhaulpia products of combustion (J - table).
|
J ° g, kcal / nmі |
J ° B, kcal / nmі |
J \u003d j ° g + (? - 1) * j ° in, kcal / nmі |
|||||||||||
|
Flak |
Gaze |
||||||||||||
|
1, 09 |
1,2 0 |
1,3 0 |
|||||||||||
4.teplobo Calculation of the boiler unit
4.1 Thermal balance and calculation of fuel
|
The calculated value |
Denotation |
The size-nosta |
Formula or justification |
Payment |
|
|
Thermal Balance |
|||||
|
Placed heat fuel |
|||||
|
The temperature of the outgoing gases |
|||||
|
Enthalpy |
By j - ?? Table |
||||
|
Cold air temperature |
|||||
|
Enthalpy |
By j - ?? Table |
||||
|
Losses of heat: |
|||||
|
From mechanical unimportant |
|||||
|
from chemical unimportant |
Table 4. |
||||
|
with outgoing gases |
(J.? Wow * J ° KH) / Q p |
(533-1,30*90,3)*100/8550=4,9 |
|||
|
environmental |
|||||
|
The sum of thermal loss |
|||||
|
Efficiency coefficient of the boiler unit (gross) |
|||||
|
Overheated Para consumption |
|||||
|
Pressure superheated steam behind boiler unit |
|||||
|
The temperature of the superheated steam behind the boiler unit |
|||||
|
Enthalpy |
Table XXVI (N.M.STR.221) |
||||
|
Pressure of nutrient water |
|||||
|
Nourishing water temperature |
|||||
|
Enthalpy |
Table XXVII (N.M.STR.222) |
||||
|
Flow water consumption |
0,01*500*10 3 =5,0*10 3 |
||||
|
Purpose water temperature |
t n at r b \u003d 156 kgf / cm 2 |
||||
|
Enthalpy of purge water |
ipr.v \u003d i? Kip |
Table XX1II (N.M.STR.205) |
|||
|
The calculated value |
Denotype |
Dimension |
Formula or justification |
Payment |
4.2 Reghe.unprofitable air heater
|
The calculated value |
Denotation |
Dimension |
Formula or justification |
Payment |
|
|
Rotor diameter |
According to constructive data |
||||
|
The number of aircraft on the body |
According to constructive data |
||||
|
Number of sectors |
According to constructive data |
24 (13 gas, 9 air and 2 dividing) |
|||
|
Surface shares, washed gases and air |
|||||
|
Cold |
|||||
|
Equivalent diameter |
p.42 (norm.m.) |
||||
|
Sheet thickness |
According to constructive data (smooth corrugated sheet) |
||||
|
0,785 * DVN 2 * xg * cr * |
0,785*5,4 2 *0,542*0,8*0,81*3=26,98 |
||||
|
0,785 * DVN 2 * KR * * |
0,785*5,4 2 *0,375*0,8*0,81*3=18,7 |
||||
|
Putting height |
According to constructive data |
||||
|
The surface of heating |
According to constructive data |
||||
|
Air temperature at the entrance |
|||||
|
Enthalpy air at the entrance |
By J-? Table |
||||
|
The ratio of air expenditures at the outlet of the cold part to theoretical |
|||||
|
Suk air |
|||||
|
Outlet air temperature (intermediate) |
Adopted pre- |
||||
|
Enthalpy air at the exit |
By J-? Table |
||||
|
(in"HF + ?? HF) (J ° Pr-j ° KH) |
(1,15+0,1)*(201,67 -90,3)=139 |
||||
|
Gas temperature at the exit |
|||||
|
The calculated value |
Denotation |
Dimension |
Formula or justification |
Payment |
|
|
Enthalpy gases at the exit |
By J-? Table |
||||
|
Enthalpy gases at the entrance |
JF + QB / C - ?? HF * J ° |
533+139 / 0,998-0,1*90,3=663 |
|||
|
Gas temperature at the entrance |
By J-? Table |
||||
|
Average temperature |
|||||
|
Medium temperature pressure |
|||||
|
The average temperature of the wall |
(xg *? cf + x * TSR) / (xg + yd) |
(0,542*140+0,375*49)/(0,542+0,375)= 109 |
|||
|
Average velocity gases |
(BP * Vg * (? Cf + 273)) / |
(37047*12,6747*(140+273))/(29*3600*273)=6,9 |
|||
|
Average air speed |
(BP * Vє * (in "HF + HF / 2) * (TSR + 273)) / |
(37047*9,52*(1,15+0,1)*(49+273))/ (3600*273*20,07)=7,3 |
|||
|
kcal / (m 2 * h * * hail) |
Nomogram 18 CH * SF * SY *? N |
0,9*1,24*1,0*28,3=31,6 |
|||
|
kcal / (m 2 * h * * hail) |
Nomogram 18 CN * C "F * SY *? N |
0,9*1,16*1,0*29,5=30,8 |
|||
|
Coefficient of use |
|||||
|
The heat transfer coefficient |
kcal / (m 2 * h * * hail) |
0,85/(1/(0,542*31,6)+1/(0,375*30,8))=5,86 |
|||
|
Heat-perception of the cold part (according to the heat transfer equation) |
5,86*9750*91/37047=140 |
||||
|
The ratio of heat-perceptions |
(140/ 139)*100=100,7 |
||||
|
|
|||||
|
The calculated value |
Denotation |
Dimension |
Formula or justification |
Payment |
|
|
Hot part |
|||||
|
Equivalent diameter |
p.42 (norm.m.) |
||||
|
Sheet thickness |
According to constructive data |
||||
|
Live cross section for gases and air |
0,785 * DVN 2 * xg * cr * cl * n |
0,785*5,4 2 *0,542*0,897*0,89*3=29,7 |
|||
|
0,785 * DVN 2 * KR * KR * CL * N |
0,785*5,4 2 *0,375*0,897*0,89*3=20,6 |
||||
|
Putting height |
According to constructive data |
||||
|
The surface of heating |
According to constructive data |
||||
|
The air temperature at the entrance (intermediate) |
Adopted pre-(in the cold part) |
||||
|
Enthalpy air at the entrance |
By J-? Table |
||||
|
Suk air |
|||||
|
The ratio of air costs at the outlet of the hot-part to theoretical |
|||||
|
Outlet air temperature |
Adopted pre- |
||||
|
Enthalpy air at the exit |
By J-? Table |
||||
|
Leap-grade stage (balance) |
(in "GC + ?? GC / 2) * * (J ° GW-J ° |
(1,15+0,1)*(806- 201,67)=755 |
|||
|
Gas temperature at the exit |
From cold |
||||
|
Enthalpy gases at the exit |
By J-? Table |
||||
|
Enthalpy gases at the entrance |
J? HF + QB / C - ?? GC * |
663+755/0,998-0,1*201,67=1400 |
|||
|
Gas temperature at the entrance |
By J-? Table |
||||
|
The average temperature of gases |
(? "VP + ?? HF) / 2 |
(330 + 159)/2=245 |
|||
|
Average temperature |
|||||
|
Medium temperature pressure |
|||||
|
The average temperature of the wall |
(xg *? cf + x * ts) |
(0,542*245+0,375*164)/(0,542+0,375)=212 |
|||
|
Average velocity gases |
(BP * Vg * (? Cf + 273)) |
(37047*12,7*(245 +273)/29,7*3600*273 =8,3 |
|||
|
The calculated value |
Denotation |
Dimension |
Formula or justification |
Payment |
|
|
Average air speed |
(BP * Vє * (in "VP + ?? GC * (TSR + 273)) / (3600 ** 273 * FB) |
(37047*9,52(1,15+0,1)(164+273)/ /3600*20,6*273=9,5 |
|||
|
The heat transfer coefficient from gases to the wall |
kcal / (m 2 * h * * hail) |
Nomogram 18 CH * SF * SY *? N |
1,6*1,0*1,07*32,5=54,5 |
||
|
The heat transfer coefficient from the wall to the air |
kcal / (m 2 * h * * hail) |
Nomogram 18 CN * C "F * SY *? N |
1,6*0,97*1,0*36,5=56,6 |
||
|
Coefficient of use |
|||||
|
Heat transfer coefficient |
kcal / (m 2 * h * * hail) |
o / (1 / (xg *? GK) + 1 / (Hins *? VK)) |
0,85/ (1/(0,542*59,5)+1/0,375*58,2))=9,6 |
||
|
Heat-perception of the hot part (according to the heat transfer equation) |
9,6*36450*81/37047=765 |
||||
|
The ratio of heat-perceptions |
765/755*100=101,3 |
||||
|
QT and QB values \u200b\u200bdiffer in less than 2%. |
vP \u003d 330 ° C TGV \u003d 260 ° C
Јvp \u003d 1400 kcal / nm 3 ј cart \u003d 806 kcal / nm 3
hF \u003d 159 ° C TPR \u003d 67 ° C
Јkhch \u003d 663 kcal / nm 3
ЈPR \u003d 20167 kcal / nm 3
wow \u003d 120 ° C TXV \u003d 30 ° С
ЈХВ \u003d 90,3кал / nm 3
Јhu \u003d 533 kcal / nm 3
4.3 Flak
|
The calculated value |
Designation |
Dimension |
Formula or justification |
Payment |
|
|
Diameter and thickness of screen pipes |
According to constructive data |
||||
|
According to constructive data |
|||||
|
The total surface of the walls of the furnace |
According to constructive data |
||||
|
The volume of the furnace |
According to constructive data |
||||
|
3,6*1635/1022=5,76 |
|||||
|
Excess air coefficient in the furnace |
|||||
|
Air shocks in the firebox of the boiler |
|||||
|
The temperature of hot air |
At the calculation of the aircraft hedgehog |
||||
|
Enhaulpia hot air |
By J-? Table |
||||
|
Air-powered heat |
(? T - ?? T) * J ° gv + + ?? T * J ° |
(1,05-0,05)*806+0,05*90,3= 811,0 |
|||
|
Useful heat dissipation in the furnace |
Q p p * (100-Q 3) / 100 + QB |
(8550*(100-0,5)/100)+811 =9318 |
|||
|
Theoretical combustion temperature |
By J-? Table |
||||
|
The relative position of the maximum temperature in the height of the furnace |
xt \u003d XG \u003d HG / HT |
||||
|
Coefficient |
p.16 0.54 - 0.2 * HT |
0,54 - 0,2*0,143=0,511 |
|||
|
Adopted pre- |
|||||
|
By J-? Table |
|||||
|
The average total heat of combustion products |
kcal / (Nm_ * Hrad) |
(QT.- J? T) * (1 + Czech) |
(9318 -5 018 )*(1+0,1) (2084-1200) =5,35 |
||
|
Composition |
m * kgf / sm |
1,0*0,2798*5,35=1,5 |
|||
|
The coefficient of weakening rays in trotham gases |
1 / (m ** kgf / / cm 2) |
Nomogram 3. |
|||
|
Optical thickness |
0,38*0,2798*1,0*5,35=0,57 |
||||
|
The calculated value |
Designation |
Dimension |
Formula or justification |
Payment |
|
|
The degree of blackness of torch |
Nomogram 2. |
||||
|
The coefficient of thermal efficiency of smooth-paper screens |
schire \u003d x * w Sheek \u003d w at x \u003d 1 to table. 6-2. |
||||
|
The degree of black chamber |
Nomogram 6. |
||||
|
Gas temperature at the outlet of the furnace |
TA / [M * \u200b\u200b((4.9 * 10 -8 * * Schire * Fst * AT * TAI) / (C * BP * VSSR)) 0,6 +1] -273 |
(2084+273)/-273=1238 |
|||
|
Enthalpy gases at the exit of firebox |
By J-? Table |
||||
|
The amount of heat perceived in the furnace |
0,998*(9318-5197)=4113 |
||||
|
The average thermal load of the radiation surface of heating |
BP * Q t l / nl |
37047*4113/ 903=168742 |
|||
|
Heat blocks of flue volume |
BP * Q r / VT |
37047*8550/1635=193732 |
4.4 Hotshirma
|
The calculated value |
Tombo- back- nie |
Dimension |
Formula or justification |
Payment |
|
|
Diameter and pipe thickness |
According to the drawings |
||||
|
According to the drawings |
|||||
|
Number of shirm. |
According to the drawings |
||||
|
Middle step between shirms |
According to the drawings |
||||
|
Longitudinal Step |
According to the drawings |
||||
|
Relative transverse step |
|||||
|
Relative longitudinal step |
|||||
|
The surface of the heating is shirm |
According to constructive data |
||||
|
Additional surface of heating in the area of \u200b\u200bhot shirm |
According to the drawings |
6,65*14,7/2= 48,9 |
|||
|
The surface of the input window |
According to the drawings |
(2,5+5,38)*14,7=113,5 |
|||
|
NVH * (NSHI / (NSHI + HDPI)) |
113,5*624/(624+48,9)=105,3 |
||||
|
N Vh - n lsi |
|||||
|
Gases |
According to constructive data |
||||
|
Live cross section |
According to constructive data |
||||
|
Effective emitting layer thickness |
1.8 / (1 / a + 1 / in + 1 / s) |
||||
|
Gas temperature at the entrance |
At the calculation of the furnace |
||||
|
Enthalpy |
By J-? Table |
||||
|
Coefficient |
|||||
|
Coefficient |
kcal / (m 2 h) |
b * Z * Q l |
0,6*1,35*168742=136681 |
||
|
Radiant heat perceived by the plane of the input section of hot shirm |
(Q LSH * N V) / (BP / 2) |
(136681*113,5)/ 37047*0,5=838 |
|||
|
The calculated value |
Most |
Dimension |
Formula or justification |
Payment |
|
|
Gas temperature at the exit from Shirm I and ?? Steps |
Adopted pre- |
||||
|
By J-? Table |
|||||
|
The average temperature of gases is swirms |
(1238+1100)/2=1069 |
||||
|
Composition |
m * kgf / sm |
1,0*0,2798*0,892=0,25 |
|||
|
Nomogram 3. |
|||||
|
Optical thickness |
1,11*0,2798*1,0*0,892=0,28 |
||||
|
Nomogram 2. |
|||||
|
v ((y / s1) і + 1) -th / s1 |
|||||
|
(QL? (1-a) ?? Ц Ш) / in + + (4.9 * 10 -8 a * evil * T CP 4 * OP) / BP * 0.5 |
(838 *(1-0,245)*0,065)/0,6+(4,9*10 -8 * *0,245*(89,8*)*(1069+273) 4 *0,7)/ 37047*0,5)= 201 |
||||
|
The heat obtained by radiation from the stoves of the Schirma Stage I |
Q lsi + add |
Q L W - Q l |
|||
|
Q t l - Q l w |
|||||
|
(QEK? BP) / D |
(3912*37047)/490000=296 |
||||
|
The amount of radiant heat perceived from the stamp of shirms |
QLSHI + additional * NLS I / (NLS I + NL Dop I) |
637*89,8/(89,8+23,7)= 504 |
|||
|
Q LSH I + additional * n d additional i / (N LSH I + N LE Dop I) |
637*23,7/(89,8+23,7)= 133 |
||||
|
0,998*(5197-3650)= 1544 |
|||||
|
Including: |
|||||
|
actually shirm |
Adopted pre- |
||||
|
additional surfaces |
Adopted pre- |
||||
|
Adopted pre- |
|||||
|
Enthapia there |
|||||
|
The calculated value |
Most |
Dimension |
Formula or justification |
Payment |
|
|
(QBS + QLSh) * BP |
(1092 + 27 2 ,0 )* 3 7047 *0,5 |
||||
|
Enthalpy couple at the exit |
747,8 +68,1=815,9 |
||||
|
Temperature there |
Table XXV. |
||||
|
The average temperature of the para |
(440+536)/2= 488 |
||||
|
Temperature pressure |
|||||
|
Average velocity gases |
|||||
|
52*0,985*0,6*1,0=30,7 |
|||||
|
Pollution coefficient |
m 2 h hail / / kcal |
||||
|
488+(0,0*(1063+275)*33460/624)= |
|||||
|
220*0,245*0,985=53,1 |
|||||
|
Coefficient of use |
|||||
|
The heat transfer coefficient from gases to the wall |
((30,7*3,14*0,042/2*0,0475*0,98)+53,1) *0,85= 76,6 |
||||
|
Heat transfer coefficient |
76,6/ (1+ (1+504/1480)*0,0*76,6)=76,6 |
||||
|
k? NSHI ?? T / BP * 0.5 |
76,6*624*581/37047*0,5=1499 |
||||
|
The ratio of heat-perceptions |
(Q tsh / q bsh) ?? 100 |
(1499/1480)*100=101,3 |
|||
|
Adopted pre- |
|||||
|
k? Ndopi? (? Wed? - T) / BR |
76,6*48,9*(1069-410)/37047=66,7 |
||||
|
The ratio of heat-perceptions |
Q T add / q b extra |
(Q T add / q b extra) ?? 100 |
(66,7/64)*100=104,2 |
ValuesQ.tSH I.Q.
butQ.t Dop I.Q.
4.4 Cold shirma
|
The calculated value |
Most |
Dimension |
Formula or justification |
Payment |
|
|
Diameter and pipe thickness |
According to the drawings |
||||
|
The number of parallel pipes |
According to the drawings |
||||
|
Number of shirm. |
According to the drawings |
||||
|
Middle step between shirms |
According to the drawings |
||||
|
Longitudinal Step |
According to the drawings |
||||
|
Relative transverse step |
|||||
|
Relative longitudinal step |
|||||
|
The surface of the heating is shirm |
According to constructive data |
||||
|
Additional surface of heating in the Schirm region |
According to the drawings |
(14,7/2*6,65)+(2*6,65*4,64)=110,6 |
|||
|
The surface of the input window |
According to the drawings |
(2,5+3,5)*14,7=87,9 |
|||
|
Running Surface Shirm |
NVH * (NSHI / (NSHI + HDPI)) |
87,9*624/(624+110,6)=74,7 |
|||
|
Additional empty surface |
N Vh - n lsi |
||||
|
Gases |
According to constructive data |
||||
|
Live cross section |
According to constructive data |
||||
|
Effective emitting layer thickness |
1.8 / (1 / a + 1 / in + 1 / s) |
1,8/(1/5,28+1/0,7+1/2,495)=0,892 |
|||
|
Gas temperature at the outlet of cold |
At the rate of hot |
||||
|
Enthalpy |
By J-? Table |
||||
|
Coefficient |
|||||
|
Coefficient |
kcal / (m 2 h) |
b * Z * Q l |
0,6*1,35*168742=136681 |
||
|
Radiant heat perceived by the plane of the input section of the SwIRM |
(Q LSH * n Vh) / (BP * 0,5) |
(136681*87,9)/ 37047*0,5=648,6 |
|||
|
Correction coefficient for radiation taking into account for shirms |
|||||
|
The calculated value |
Most |
Dimension |
Formula or justification |
Payment |
|
|
Gas temperature at the entrance to cold screen |
At the rate of hot |
||||
|
Enthalpy of gases at the exit from shirm when the temperature accepted |
By J- Table |
||||
|
The average gases temperature in Shirmah? Art. |
(1238+900)/2=1069 |
||||
|
Composition |
m * kgf / sm |
1,0*0,2798*0,892=0,25 |
|||
|
Ray weakening coefficient: Treatomic Gas |
Nomogram 3. |
||||
|
Optical thickness |
1,11*0,2798*1,0*0,892=0,28 |
||||
|
Gas black degree in shirms |
Nomogram 2. |
||||
|
Corner coefficient from the input on the output section Shirm |
v ((1 / s 1) І + 1) -1 / s 1 |
v ((5.4 / 0.7) І + 1) -5.4 / 0.7 \u003d 0.065 |
|||
|
Heat of radiation from firebox to input widths |
(Q added? (1-a) ?? CCS) / B + (4.9 * 10 -8 * a * evil * (TCP) 4 * OP) / BP |
(648,6 *(1-0,245)*0,065)/0,6+(4,9*10 -8 * *0,245*(80,3*)*(1069+273)4 *0,7)/ 37047*0,5)= 171,2 |
|||
|
The heat obtained by the radiation from the firebox with cold screen |
Qlov VKh - QL |
648,6 -171,2= 477,4 |
|||
|
Heatshop heat screens |
QTL - QL |
4113 -171,2=3942 |
|||
|
Environment Environment in Screens |
(QEK? BP) / D |
(3942*37047)/490000=298 |
|||
|
The amount of radiant heat perceived from the furnishes input swirms |
QLSHI + additional * NLS I / (NLS I + NL Dop I) |
477,4*74,7/(74,7+13,2)= 406,0 |
|||
|
The same additional surfaces |
QLS I + Ext * NL Dop I / (NLSHI + NL Dop I) |
477,4*13,2/(74,7+13,2)= 71,7 |
|||
|
Heat-perception Shirm I Steps and additional balances on balance |
c * (ј "-ј" ") |
0,998*(5197-3650)=1544 |
|||
|
The calculated value |
Most |
Dimension |
Formula or justification |
Payment |
|
|
Including: |
|||||
|
actually shirm |
Adopted pre- |
||||
|
additional surfaces |
Adopted pre- |
||||
|
Couple temperature at the output from the Input Shirm |
From the settlement of the weekend |
||||
|
Enthapia there |
Table XXVI |
||||
|
The increase in enthalpy couple in shirms |
(QBS + QLSh) * BP |
((1440+406,0)* 37047) / ((490*10 3)=69,8 |
|||
|
Enthalpy couple at the entrance to the input screen |
747,8 - 69,8 = 678,0 |
||||
|
Steam temperature at the entrance to the screen |
Table XXVI (P \u003d 150kgs / cm 2) |
||||
|
The average temperature of the para |
|||||
|
Temperature pressure |
1069 - 405=664,0 |
||||
|
Average velocity gases |
In r? V g? (? cf + 273) / 3600 * 273 * FG |
37047*11,2237*(1069+273)/(3600*273*74,8 =7,6 |
|||
|
Coefficient of heat transfer convection |
52,0*0,985*0,6*1,0=30,7 |
||||
|
Pollution coefficient |
m 2 h hail / / kcal |
||||
|
The temperature of the outer surface of the pollution |
t cf + (e? (Q BSH + Q LSH) * BP / NSHI) |
405+(0,0*(600+89,8)*33460/624)= |
|||
|
The heat transfer coefficient radiation |
210*0,245*0,96=49,4 |
||||
|
Coefficient of use |
|||||
|
The heat transfer coefficient from gases to the wall |
(? K? P * D / (2 * S 2? X) +? L) ?? ? |
((30,7*3,14*0,042/2*0,0475*0,98)+49,4) *0,85= 63,4 |
|||
|
Heat transfer coefficient |
1 / (1+ (1+ Q LSH / Q BSH) ?? ???? 1) |
63,4/(1+ (1+89,8/1440)*0,0*65,5)=63,4 |
|||
|
Heat-perception of shirm on the heat transfer equation |
k? NShi ?? T / BP |
63,4*624*664/37047*0,5=1418 |
|||
|
The ratio of heat-perceptions |
(Q tsh / q bsh) ?? 100 |
(1418/1420)*100=99,9 |
|||
|
Average pair temperature in additional surfaces |
Adopted pre- |
||||
|
The calculated value |
Most |
Dimension |
Formula or justification |
Payment |
|
|
Heat-perception of additional surfaces according to the heat transfer equation |
k? Ndopi? (? Wed? - T) / BR |
63,4*110,6*(1069-360)/37047=134,2 |
|||
|
The ratio of heat-perceptions |
Q T add / q b extra |
(Q T add / q b extra) ?? 100 |
(134,2/124)*100=108,2 |
ValuesQ.tSH I.Q.bSh differ by no more than 2%,
butQ.t Dop I.Q.b extra - less than 10%, which is permissible.
Bibliography
Thermal calculation of boiler aggregates. Regulatory method. M.: Energy, 1973, 295 p.
Rivka S.L., Aleksandrov A. A. Tables of thermodynamic properties of water and water vapor. M.: Energia, 1975
Fadyushina M.P. Thermal calculation of boiler aggregates: guidelines for the implementation of the course project on the discipline "Boiler installations and steam generators" for students full-time learning Specialties 0305 - thermal electric stations. Sverdlovsk: UPI. Kirov, 1988, 38 s.
Fadyushina M.P. Thermal calculation of boiler aggregates. Guidelines for the implementation of the course project on the discipline "Boiler installations and steam generators". Sverdlovsk, 1988, 46 s.
Characteristics of the TP-23 boiler, its design, thermal balance. Calculation of air enthalpy and fuel combustion products. The thermal balance of the boiler unit and its efficiency. Calculation of heat exchange in the furnace, calibration thermal calculation of the Feston.
course work, added 04/15/2011
Constructive characteristics of the boiler unit, the diagram of the cooler, the wiring gas and the rotary chamber. Elementary composition and heat combustion of fuel. Determination of volume and partial pressure of combustion products. Thermal calculation of the boiler.
course work, added 05.08.2012
Thermal scheme of the boiler unit E-50-14-194. Calculation of the enthalpy of gases and air. The calibration of the furnace chamber, a boiler beam, a superheater. Distribution of heat-bypatic tracting paths. Thermal balance of the air heater.
course work, added 11.03.2015
Estimated fuel characteristics. Calculation of air and combustion products, efficiency, heat chamber, festoon, steps, and an economy meter, an air heater. The thermal balance of the boiler unit. Calculation of enthalpium on gas powders.
course work, added 01/27/2016
Recalculation of the amount of heat for steam boiler. Calculation of the amount of air required for combustion, full combustion products. The composition of combustion products. Thermal balance of the boiler unit, efficiency.
examination, added 08.12.2014
Description of the GM-50-1 boiler unit, gas and steaming path. Calculation of volumes and enthalpies of air and combustion products for the specified fuel. Determination of balance parameters, furnaces, fester of the boiler unit, the principles of heat distribution.
course work, added 30.03.2015
Description of the design I. technical characteristics Boiler aggregate de-10-14gm. Calculation of theoretical consumption of air and volumes of combustion products. Determination of an excess air coefficient and sucks on gas powders. Check the thermal balance of the boiler.
course work, added 01/23/2014
Characteristics of the boiler de-10-14gm. Calculation of the volume of combustion products, volume fractions of trochatomic gases. The excess air coefficient. The heat balance of the boiler unit and determining fuel consumption. Calculation of heat exchange in the furnace, water economizer.
coursework, added 12/20/2015
Calculation of volumes and enthalpy of air and combustion products. Calculated thermal balance and fuel consumption of a boiler unit. Checking the combustion chamber. Convective heating surfaces. Calculation of a water economizer. Consumption of combustion products.
course work, added 04/11/2012
Fuel types, its composition and heat engineering characteristics. Calculation of air volume when burning solid, liquid and gaseous fuels. Determination of the coefficient of excess air in the composition of flue gases. Material and thermal balance of the boiler unit.
The temperature of the outgoing gases: when working on fuel oil 141 on gas 130 efficiency on fuel oil 912 on gas 9140. In the back wall, slots are placed to enter the recycling flue gases.3. Excess air coefficients in the gas path of the boiler. Excess air exhaust air coefficients. . Excess air coefficients: at the outlet of the furnace after the shirm steamer after the PPP1 after the PPC2 after the EK1 after EK2 in the outgoing gases; Selecting the calculated temperatures The recommended temperature of the outgoing gases for fuel oil ...
If this job does not come up at the bottom of the page there is a list of similar works. You can also use the Search button.
1. Thermal calculation of the boiler TGM-94
1.1 Description of the boiler
Steam generator TGM-94 for block 150 MW per capacity 140 kg / s, pressure 14MN /, overheating, promineragrev, hot air temperature. Estimated fuel: natural gas and fuel oil. The temperature of the outgoing gases: when working on fuel oil 141, on gas 130, efficiency on fuel oil 91.2, on gas 91.40%.
The steam generator is designed for areas with minimal atmospheric air temperature - and has a P - shaped open layout. All elements of the aggregate are made drainaged. The frame turned out to be rather complicated and difficult due to the presence of local shelters, as well as due to the accounting of wind load and seismicity in 8 points. Local shelters (boxes) are made of light-type asbanene materials. Open pipelines are covered with aluminum trim.
The equipment of the block is designed so that the air heater is located from the front of the steam generator, and the turbine is rear. At the same time, gas ducts are somewhat extended, but the air ducts are conveniently combined, steam pipelines are also shortened, especially when placing the output reservoirs behind the steam generator. All elements of the unit are designed for block factory manufacturer, with a maximum weight of a block of 35 tons, except the drum that has 100t.
The front wall of the furnace is shielded by the evaporating and overheater panels, seven panels of the superheater are placed on the wall. bent pipes By going around the burners, and between them evaporative panels from straight pipes.
Gibbs bypassing the burners allow you to compensate for the difference in thermal elongations and cook with each other the lower cameras of all front panels located coaxially. Horizontal furnace ceiling is shielded with overheating tubes. The middle panels of the side screens are included in the second stage of evaporation. Salt compartments are placed on the ends of the drum and have a total capacity of 12%.
In the back wall, slots are placed to enter recycling flue gases.
On the front wall installed in 4 tiers of 28 gas-dashed burners. There are three top rows on the fuel oil, there are three lower gas on gas. In order to reduce the excess air in the furnace, an individual air supply to each burner is provided. The volume of the furnace 2070; The volumetric density of the heat generation of the combustion chamber depends on the type of fuel: for gasQ / V. \u003d 220, for fuel oil 260 kW /, thermal flux density cross section Fires for gasQ / F. \u003d 4.5, for fuel oil 5.3 MW /. Cutting the aggregate shield with reference to the frame. Iron icon - bubble and moved along with the screen; Ceiling irrigation is made of panels lying on the ceiling steamer pipes. The seam between the moving and fixed surveillance of the furnace is made in the form of a hydraulic circuit.
Circuit circulation
The nutrient water of the boiler, passing the capacitor, the economizer enters the drum. About 50% of the nutrient water is supplied to the barbage-wash device, the rest of the washing device is sent to the bottom of the drum. From the drum, it enters the on-screen pipes of the pure compartment and then in the form of a steam mixture enters the drum into the internal-accessed cyclones, where the primary separation of water from steam occurs.
Part of the drum boiler water enters remote cyclones, which is a purge water of 1 stage and nutrient water 2 steps.
Couples of the pure compartment goes into a bubble-washing device, there are pairs of salt compartments from remote cyclones.
Couples passing through a layer of nutrient water is cleaned from the main amount of salts contained in it.
After the washing device, the saturated pair passes through the plate separator and a hole-leaf, cleaning from moisture, and heads along the steamed pipes into the steamer and further on the turbine. The part of the saturated pair is discharged into capacitors to obtain their own condensate, for injection into the steelectricel.
Continuous purge is carried out from remote cyclones in the saline compartment 2 steps of evaporation.
Condensation set (2 pcs.) Are accommodated in the side walls of the heat chamber and consists of two capacitors, a collector and pair supply pipes and condensate.
Steamers are located along the steam.
Radiation (wall) - shielding front wall of the furnace.
Ceiling - shielding ceiling of the boiler.
Shirm - located in the gas duct connecting the furnace with a convective shaft.
Convective - posted in a convective mine.
1.2 Original data
Air volume and combustion products, /:
1.3 Excess air coefficients in the gas tract of the boiler
Outlet air coefficients at the exit of the furnace excluding recirculation :.
Cold air supplies in the furnaces and heat boilers are missing.
Air excess coefficients:
On the outlet of the firebox
After the shirm steamer
After gearbox1
After gearbox2.
After ek1
After ek2.
In the outgoing gases;
Selection of estimated temperatures
130 ÷ 140 \u003d 140.
Air temperature at the air heater
for regenerative air heater:
0.5 (+) - 5;
Air heating temperature 250-300 \u003d 300.
Minimum temperature pressure behind the economizer :.
The minimum temperature pressure in front of the air heater :.
Last air heating in one stage of the VP:.
The ratio of water equivalents:, in drawing.
Medium excess air in the steps of the VP:
300;
140;
Calculate the volume of gas taken by recycling, fuel
The proportion of hot air recycling on the entrance to the air heater;
1,35/10,45=0,129.
The average excess of air in the stage of the air heater:
1,02-0+0,5∙0+0,129=1,149.
The ratio of water equivalents:
1.4 Calculation of air and combustion products
When burning fuel oil, the calculation of theoretical volumes of air and combustion products is made on the basis of the percentage composition of the working mass:
theoretical air volume:
Theoretical air volumes:
The actual volumes of combustion products in the excess of air in the risks are determined by the formula:
The results are shown in Table 1.1.
|
Value |
Flak shirm |
PPP1 |
KPP2. |
Ek1 |
Ek2. |
RVP |
|
1,02 |
1,02 |
1,02 |
1,02 |
1,02 |
1.02 |
|
|
1,02 |
1,02 |
1,02 |
1,02 |
1,02 |
1,02 |
|
|
|
1,453 |
1,453 |
1,453 |
1,453 |
1,453 |
1,453 |
|
10,492 |
10,492 |
10,492 |
10,492 |
10,492 |
10,492 |
|
|
0,15 |
0,15 |
0,15 |
0,15 |
0,15 |
0,15 |
|
|
0,138 |
0,138 |
0,138 |
0,138 |
0,138 |
0,138 |
|
|
0,288 |
0,288 |
0,288 |
0,288 |
0,288 |
0,288 |
Volume of water vapor:
Full gases:
Volume fraction of triat gases:
Volume fraction of water vapor:
Share of trucatomic gases and water vapor:
1.5 Enthalpia air and combustion products
The enthalpy of theoretical volumes of air and combustion products, in, at a calculated temperature, is determined by the formulas:
Enhaulpia combustion products in excess air
The results of the calculations are shown in Table 1.2.
Table 1.2.
Enhaulpia products of combustion
|
Surface heating |
Temperature over the surface |
||||
|
Machine camera |
2300 2100 1900 1700 1500 1300 1100 |
44096 ,3 39734,1 35606 31450 27339,2 23390,3 19428 16694,5 |
37254,3 33795,3 30179,6 26647,5 23355,7 19969,95 16782,70 13449,15 |
745,085 675,906 603,592 532,95 467,115 399,399 335,654 268,983 |
44827,3 40390,7 36179,6 32018,5 27798 23782,6 19757,9 15787,1 |
|
PPP1 |
1100 |
19422,26 15518,16 13609,4 11746,77 9950,31 |
16782,70 13449,15 11829,40 10241 8683,95 |
335,654 268,983 236,588 204,820 173,679 |
19757,9 15787,1 13846 11951,6 10124 |
|
KPP2. |
11746,77 9950,31 9066,87 |
10241 8683,95 7921,10 |
204,820 173,679 158,422 |
11951,6 10124 9225,3 |
|
|
Ek1 |
9950,31 9066,87 8193,30 |
8683,95 7921,10 7158,25 |
173,679 158,422 143,165 |
10124 9225,3 8336,5 |
|
|
Ek2. |
9066,87 8193,30 6469,46 4788,21 |
7921,10 7158,25 5663,90 4200,90 |
158,422 143,165 113,278 84,018 |
9225,3 8336,5 6582,7 4872,2 |
|
|
RVP |
4788,21 3151,52 1555,45 |
4200,90 2779,70 1379,40 |
84,018 55,594 27,588 |
4872,2 3207,1 1583 |
For
1.6 Efficiency and Warm Loss Factors
The efficiency coefficients of the projected steam boiler are determined from the return balance:
The loss of heat with outgoing gases depends on the selected gas temperature, leaving the steam boiler, and excess air and is determined by the formula:
We find enthalpy of outgoing gases when:
Cold air enthalpy at the calculated temperature:
Located heat of burning fuelkJ / kg, generally determined by the formula:
Warm loss with chemical fuel chemical=0,1%.
Then:.
Warm losses with mechanical non-fuel
Warm losses from outdoor cooling through the external surface of the boiler %, it is small and with the growth of the nominal productivity of the boiler kg / s, decreases: when
We get:
1.7 Thermal Balance and Fuel Consumption
Fuel consumption in, kg / s supplied to the steam chamber of the steam boiler, can be determined from the following balance:
Consumption of purge water from drum steam boiler, kg / s:
Where \u003d 2% - continuous boiler purge.
- enthalpy of superheated steam;
- enthalpy of boiling water in the drum;
- entalpy of nutritious water;
1.8 Calculation of heat exchange in the furnace
Floor chamber dimensions:
2070 .
Heat voltage of flue
Twiling screen, 6 gas-dashed burners in two tiers on the front of the boiler.
Thermal characteristics of the furnace chamber
Useful heat dissipation in the heat chamber (per 1 kg or 1fuel):
The heat of air consists of heat of hot air and a small share of the warmth of cold air suits from the outside:
In gas-metal furnaces working under the supervision, air supplies in the furnace are excluded=0. =0.
Adiabatic (calorimetric) Temperature of combustion products:
where
Let the table find the enthalpy of gases
Averaged gases heat capacity:
When calculating the boiler firebox temperatureyou can define directly using Table 2.3 data, according to a known value.
by interpolation in the zone of high temperatures of gases at a value, and taking
Then,
Gas temperature at the outlet of the furnace forD.<500 т/ч
From Table 2.2 we find the enthalpy of gases at the outlet of the furnace:
Specific heat treatment of the furnace, KJ / kg:
where - the coefficient of heat conservation, which takes into account the proportion of gas heat, perceived by the surface of heating:
Gas temperature at the outlet of the furnace:
where m \u003d 0.52-0.50 is the coefficient, taking into account the relative position of the torch kernel in the height of the furnace chamber;
At the location of the burner in two three rows, the average height is taken at the height, if the thermal production of the burners of all rows is the same, i.e. Where\u003d 0.05 with D \u003e 110 kg / s, m \u003d 0.52-0.50 ∙ 0.344 \u003d 0.364.
Coefficient of thermal efficiency of the screen:
Corner screen coefficient is determined:
1.1 - the relative pitch of the wall screen.
Conditional coefficient of surface pollution:
The degree of black:, when burning liquid fuel, the thermal radiation coefficient of the torch is:
The thermal radiation coefficient is the unlinking part of the torch:
Where p \u003d 0.1 MPa, and
The absolute temperature of the gases at the outlet of the furnace.
Complete proportion of triat gases.
The effective thickness of the radiated layer in the heat chamber, where the calculated volume of the cooler chamber is:, and the surface of the furnace with a double-screen screen:
where
Then I.
Receive
We accept in the first approximation equal
The average thermal voltage of the heating surface of the heat screens:
Where - complete radiation surface of the furnace.
1.9 Calculation of the surface of the boiler heating
Hydraulic resistance of superheated steam:
At the same time, the pressure in the drum:
Pressure of nutritional water in a wall-mounted superheater:
Pressure loss in Shirma:
Pressure loss in PPC:
1.9.1 Calculation of the Wall Steamer
Nutrient water pressure
Petroleum temperature,
Entalpy of nutritious water.
Heat-perception of radiation wall screens: where the average thermal voltage of the calculated on-screen surface, for the wall screen means
Corner screen coefficient:
So
Calculate the output parameters of the feed water:
At p \u003d 15.4 MPa.
1.9.2 Calculation of radiation ceiling steamer
Input water parameters:
Heat-perception of radiation ceiling PP:
Heat-perception over the furnace: where the cream-visible surface of the heating of the ceiling screens of the furnace:
Heat-perception with horizontal gas duct:
Where the average specific thermal load in the horizontal gas duct area of \u200b\u200bthe gas plant then
Calculate the enthalpy couple: or
Then enthalpy at the exit of the furnace:
Injection 1:
1.10 Calculation of the heat-perception of shirms and other surfaces in the scope of shirms
1.10.1 Calculation of the Shirm Steamer 1
Input water parameters:
Output water parameters:
Injection 2:
1.10.2 Calculation of the Shirm Steamer 2
Input water parameters:
Output water parameters:
Heatshitus Shirm:
The heat obtained from the furnace with the plane of the input window of the SHIRM
Where
Heat, emitted from the firebox and shirm on the surfaces behind the shirms:
Where am correction factor
Angular coefficient from the input on the output section Shirm:
The average temperature of gases in Shirmah:
Heat from washing gases:
Defined heat-perception Shirm:
Wire Exchange Equation: where the surface of the heating is wide:
Averaged
where the temperature pressure of the forward-point:
Temperature contamination:
Heat transfer coefficient:
Coefficient of heat transfer from gases on the wall:
Gas velocity:
The heat transfer coefficient of gases convects to the surface:
Where amendment on the number of pipes in the course of gases.
And a correction to the layout of the beam.
1 - the coefficient that takes into account the influence and change of physical flow parameters.
Heat transfer coefficient of burning products:
Coefficient use:,
where
Then
The heat exchange equation for Shirma will look like this:
Receivedcompare with:
1.10.3 Calculation of suspended pipes in the Schirm region
The heat obtained by the surface of the tubular beam from the furnace:
Where heat-visible surface:
Heat exchange in pipes:
Gas velocity:
Where
The heat transfer coefficient of convection from gases to the surface:
So
Then
Heat, perceiving heated medium due to cooling of washing gases (Balance):
From this equation, we find enthalpy at the exit of the surface of the pipes:
where - the heat obtained by the surface of the radiation from the furnace;
Enthalpy at the entrance to the pipes at temperatures
Enthalpy determine the temperature of the working medium at the outlet of the suspended pipes
The average pair temperature in the suspended pipes:
Temperature wall
Coefficient, heat transfer from radiation of combustion products with not dusty gas flow:
Use ratio: where
Then:
The heat-perception of suspended pipes is found according to the heat transfer equation:
Compared from the value with
So The temperature of the working fluid at the outlet pipe output
1.10.4 Calculation of the Shirm Steamer 1
Gases at the entrance:
at the exit:
Heat obtained from firegram:
The radiation coefficient of the gas environment: where
Then:
The heat obtained by radiation from the furnace:
Heat from washing gases:
Temperature reference temperature:
Averaged Temperature Phoam:
Heat transfer coefficient:
where the heat transfer coefficient from gases to the wall:
Gas velocity:
We get:
The heat transfer coefficient of convects from the surface to the heated environment:
Then:
The heat exchange equation for Shirm:
Compare with:
So The temperature at the exit from the wiring superheater 2:
1.11 Driving a convective steamer
1.11.1 Calculation of convective steamer 1
Output parameters at the entrance:
Output Work Environment Parameters:
where
Heat, perceived by the working environment:
The enthalpy of gases at the exit from the heating surface is expressing from the heat equation given by the gases:
Heat exchange equation for PPC1:
Heat transfer coefficient:
The heat transfer coefficient of gases to the surface:
Gas velocity:
So
Determine the state of gases at the output:
taking into account the emission volume
Then:
Then the heat transfer coefficient from gases to the wall will be:
Steam speed on the convective superheater:
The heat transfer coefficient will be equal to:
Temperature reference temperature:
The heat exchange equation for the convective steamer:
Compare S.
Injection 3 (3).
1.11.2 Calculation of convective steamer 2
Output parameters at the entrance:
Output Work Environment Parameters:
Heat, perceived by the working environment:
Gas equation given by gases:
hence the enthalpy of gases at the outlet of the heating surface:
The heat exchange equation for PPC 2:.
Temperature reference temperature:
Coefficient of heat transfer: where the heat transfer coefficient from the gases to the wall: where
Gas velocity:
The coefficient, heat transfer of radiation of combustion products with a non-dusty gases:
Relief coefficient of the gas environment:
Determine the state of gases at the outlet of the furnace chamber by the formula:
Then:
So:
Then the heat transfer coefficient of convection from gases to the wall will be:
The heat transfer coefficient of convection from the surface to the heated environment:
Then:
The heat exchange equation will look at:
Compare S.
1.11.3 Calculation of suspended pipes in a convective mine
Heat, given by surface gazes:
Heat-perception of suspended pipes:where the calculated heat exchange surface:
Heat transfer coefficient
from here
on this enthalpy we find the temperature of the working medium at the outlet of the suspended pipes:
The temperature of the work environment at the entrance:
Temperature pressure: where
Then
It turned out that it means gas temperature after suspended pipes
1.12 Calculation of water economizer heat
1.12.1 Economic meter calculation (second stage)
Heat, given by gases:
where at
Enthalpy couple at the entrance:
- inlet pressure should
The enthalpy of the exit medium is located from the heat equation, a perceived working surface:
Heat exchange equation:
Heat transfer coefficient:
Heat transfer coefficient from gases to the wall: where
Gas velocity:
Then the heat transfer coefficient of convection from gases to the surface:
Relief coefficient of the gas environment:
Square heated surface:
Taking into account the emission volume
Then:
coefficient of use
Coefficient, heat transfer radiation products of combustion:
The heat transfer coefficient of gases to the wall:
Then
Temperature pressure:
Economyzer heat exchange (second stage):
Compare S.
so the temperature at the exit from the second level of the economize
1.12.2 Calculation of the economizer (first stage)
Working Environment Parameters:
Combusion Product Parameters:
Parameters perceived by the working medium:
From the equation for the heat of given gases, we find enthalpy at the exit:
In using Table 2 we find
Heat exchange equations:
Temperature reference temperature:
Gas velocity:
Coefficient of heat transfer from gases to the surface:
The coefficient, heat transfer of the radiation of combustion products with not dusty of gases:
Where the radiation coefficient of the gas environment: where the state of gases at the output:
then
Heat transfer coefficient:
Then the heat exchange equation will look like this:
So The temperature at the exit from the first stage of the economize:
1.13 Calculation of the regenerative air heater
1.13.1 Calculation of a hot package
Air perceived heat:
where at
for
The ratio of the average air temperature in the air heater to theoretically necessary:
From the equation for the heat of the given gases, we find enthalpy at the outlet of the hot part of the air heater:
Gas temperature at the outlet of the hot part in Table 2:
Average temperature:
The average temperature of gases:
Temperature pressure:
Average air speed:
The average velocity of gases:
The average temperature of the hot wall of the air heater:
The heat transfer coefficient of convection from the surface to the heated environment:
Heat transfer equation:
Heat exchange equation:
1.13.2 Calculation of the Cold Package
The proportion of air theoretically necessary in the cold part of the air heater:
Heat-perception of the cold part of the balance:
Enthalpy gases at the outlet of the air heater:
Average temperature:
The average temperature of gases:
Temperature pressure:
The temperature of the cold part of the air heater:
Average air speed:
The average velocity of gases:
The heat transfer coefficient of convection from gases to the surface:
Heat transfer equation:
Heat exchange equation:
1.14 Calculation of the PDA Steam Boiler
Efficiency:
Warm losses with outgoing gases:
where the enthalpy of cold air at the estimated temperature and
Then the efficiency will be equal to:
Inv. No.
Sub. and date
Torture. Inv. No.
Inv. No. Double.
Sub. and date
LIT.
Sheet
Sheets
FGBOU VPO "KGEU"
ITE, gr. KUB-1-09
DP 14050 2 .065.002 PZ
LIT.
№ DOCUM.
Change
Sub.
date
Bakhtin
Developed.
Fedosov
Prov.
T. K
Loktev
N. Keep.
Galitsky
Applied.
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
DP 14050 2 .065.002 PZ
Change
Sheet
№ DOCUM.
Signature
date
Sheet
