JPH01200101A - Double floor type fluidized bed boiler - Google Patents

Abstract

PURPOSE:To recover heat from a fluid medium with high efficiency, by a method wherein two revolving flow type fluidized boilers are provided, the heat recovering part of the one furnace forms a liquid heater to generate steam of a steam drum, and the heat recovering part of the other furnace forms a steam superheater and/or steam reheater. CONSTITUTION:In a right fluidized bed boiler 1 of a steam drum 19, a pressure controller 31 outputs a control signal according to 8 deviation between the steam pressure of a steam outlet pipe 14 detected by a pressure detector 23 and a set value. A signal from a steam flow rate detector 14a is computed by a computer 34 to add it, and the number of revolutions of a motor 16 of a combustion substance feed device 18 is variably controlled. A control signal from a pressure controller 31 is compared with temperature in a fluidized bed, detected by a temperature detector 25, by means of a comparator 32, according to a difference therebetween, a diffusing air flow controller 33 opens and closes a valve 11a, and controls a heat recovery amount of a heat recovery part 9. Meanwhile, a left boiler 1' performs similar control by means of a steam temperature controller 31' serving as a main control system. This constitution prevents increase of a pressure in the steam drum to an excessively high value, and enables the feed of steam having a desired temperature.

Description

[Detailed Description of the Invention] [Industrial Application Field] The present invention provides a plurality of swirl flow type fluidized bed boilers 2, and the heat recovery section of each boiler is independently connected to a steam generation section, a steam heating section, and a steam heating section. /Or relates to a double-bed swirling flow type fluidized bed boiler used as a steam reheating section〇 [Technical Background of the Invention] The present inventors previously reported that We have been conducting extensive research on a method for recovering heat from the fluidized medium in a fluidized bed incinerator, and found that a reflective partition was installed inside the furnace in place of the reflective wall that conventionally formed part of the furnace wall. Provided independently, a heat recovery chamber is formed between the back surface of the reflective partition and the furnace wall, a moving layer is formed by a heating medium from a fluidized bed in the heat recovery chamber, and a heat-receiving fluid is heated in the heat recovery chamber. By arranging a heat transfer surface for
We discovered a way to efficiently recover heat from a fluidized medium without causing wear on the heat transfer surface, and to control the amount of heat recovery, and filed a patent application (Japanese Patent Application No. 62-9057).
0 In addition, in conventional incinerators, when the amount of combustibles increases or the calorific value of the combustibles increases, the flow The fluidized medium was cooled by injecting water into the medium, but as mentioned above, it has become possible to efficiently recover heat from the fluidized medium by providing a heat recovery chamber in the furnace. By collecting it, the fluidized medium can be cooled, making it possible to use it, for example, in the combustion section of a coal boiler.

Furthermore, since the heat recovery section is separated from the combustion section, and the combustion section is a swirling fluidized bed, it has become possible to burn combustible materials containing incombustibles exclusively and to co-combust them with coal, etc. In other words, it has become possible to use any combustible material as fuel.

Below, we will explain a swirl type fluidized bed boiler with a heat recovery chamber inside the furnace based on the meat surface.0 Figure 5 shows an example of an FC fluidized bed boiler with a heat recovery chamber inside the furnace. Is there a heat recovery chamber in the fluidized bed furnace described in JP-A-57-124608? The setting is a friend.

In FIG. 5, at the bottom of the furnace 51, the fluidizing gas introduced from the fluidizing gas introduction pipe 53 by the blower 57 is dispersed and
52, this dispersion plate 52 has both edges lower than the center, and is formed into a chevron-shaped surface (roof-like shape) that is almost symmetrical with respect to the center line of the furnace 51. The fluidizing gas sent from the air chamber is 54.55%
The flow rate of the fluidizing gas ejected from the air chambers 54 and 56 on both side edges is determined by the flow rate of the fluidizing medium in F51.
The velocity of the fluidizing gas ejected from the central air chamber 55 is selected to be smaller than the former.

The upper part of the air chamber 54% 56 at both edges blocks the upward flow path of the fluidizing gas and directs the fluidizing gas ejected from the air chamber 54% 56 toward the center of the furnace 51. A plate-shaped reflective partition 58 whose upper part is folded inward is provided as a reflecting wall, and due to the difference in lxt velocity between this reflective partition 58 and the ejected fluidizing gas, a swirling flow in the direction shown by the arrow in the figure is generated. occurs. - A heat recovery chamber 59 is formed between the back surface of the reflective partition 58 and the furnace wall, and is configured such that a part of the fluid medium passes over the top of the reflective partition 58 and enters the heat recovery chamber 59 during operation. ing.

This tilted reflective partition is designed so that the fluidized gas ejects most violently near the top of the reflective partition, and therefore flows! - Karabuki! ! The fluid medium can easily pass over the upper end of the reflective partition and enter the heat recovery chamber.

In addition, at a level higher than the bottom of the furnace at the lower part of the heat recovery chamber 59, there is provided an aeration system [62] that introduces gas from the blower 60 through the air diffuser @62' of the heat recovery chamber 59.
An opening 63 is provided near where the heat recovery chamber 59 is installed, and the fluidized medium that has entered the heat recovery chamber 59 is maintained as a fixed layer depending on the operating conditions, or is continuously or intermittently formed as a moving layer or a weak fluid 18k. The air then settles down, slips through the air diffuser, and circulates from below to the combustion section.

The amount of sedimentation is controlled to some extent by the amount of air diffused into the heat recovery chamber and the amount of fluidized gas in the combustion section. That is, the amount Gl of the fluidized medium entering the heat recovery chamber 59 is determined by the amount of fluidizing gas ejected from the dispersion plate 52, especially the air chambers 54 and 56 at the ends, in order to completely fluidize the combustion section, as shown in FIG. If you increase t of the fluidizing gas ejected from the t, it will increase. Furthermore, as shown in Fig. 9, when the air blowing into the heat recovery chamber is changed within the range of 0 to less than 1 Gmf, the amount of fluidized medium that settles in the heat recovery chamber changes approximately proportionally, and the Collection chamber air volume is I
In the case of a fluidized bed of Gmf or more, it becomes almost constant. The amount of fluidized medium that becomes constant is the amount of fluidized medium that enters the heat recovery chamber G
Almost equal to 1. In addition, the amount of fluidized medium that completely settles in the heat recovery chamber is G! The following amount will be obtained depending on: The amount of settling of the fluidized medium that settles inside the heat recovery chamber 59 can be controlled by adjusting these air volumes. In the heat recovery chamber, flow or high-speed flow or I! In order to maintain Gs' that is effective for suppressing overheating of the fluidized medium and recovering heat without blowing it upwards due to #j flow, the falling fluidized medium should be kept as close as possible to the vicinity where the gas flow ejected from the fluidized bed combustion section is at its maximum. It is necessary to introduce the heat recovery chamber into the heat recovery chamber.In this ninth step, the reflective partition protruded on the side of the combustion section has the function of accelerating the rising gas flow of the combustion section and the function of protruding to receive the fluidized medium. It has an optimal shape.

As shown in FIG. 6, inside the heat recovery N59, a heat transfer tube 65 through which heat-receiving fluid passes is disposed inside the heat recovery tube 65, which is connected to a waste heat boiler 67 through a pipe 64, and exchanges heat with a fluidized medium moving downward through the heat recovery chamber. In order to do this, heat is recovered from the body. The heat transfer coefficient in the heat recovery section changes greatly and gently as shown in an example shown in FIG. 29 when the heat recovery chamber diffuser air pressure is changed from 0 to 2 Gmf. Note 5.
Figure @29 is an aeration device based on the principle shown in Figure 21, and the fluidized medium has an average particle diameter t2 type at a temperature of around 850°C.

As mentioned above, the ninth step in controlling the heat recovery t is to control the flow rate of the fluidized medium and at the same time control the heat transfer coefficient. When the diffuser air volume is increased, the heat transfer coefficient increases at the same time as the fluidized medium circulation volume increases, and as a synergistic effect, heat recovery
- increases significantly 0 This relationship is shown in Figure 4 b
Ru. Considering the temperature of the fluidized medium in the fluidized bed, this has the effect of preventing the temperature of the fluidized medium from rising above a predetermined temperature in summer.

Various devices can be considered as means for introducing gas into the heat recovery chamber 59, but generally a method is adopted in which the air diffuser lk is installed horizontally as shown in FIG. In FIG. 10, theory 8A is simplified and the circulation of the fluidized medium with the combustion section is ignored and the phenomenon of the moving bed is omitted in order to clarify the partial fluidization. In this case, if the openings for discharging gas are uniformly provided over the entire hearth surface, the amount of gas supplied per unit area will be uniform over the entire hearth surface regardless of the gas supply to the diffuser. When the amount of gas supplied to the diffuser is gradually increased, the fluidized medium in the heat recovery chamber changes from a fixed bed to a fluidized bed when the amount of gas supplied is called the minimum fluidization speed Gmf.

Considering the heat transfer lid in the heat recovery chamber in this simple case, in the heat recovery chamber according to the present invention, the heat transfer body i! between the heat transfer surface and the fluid medium! Since x changes rapidly near the fluidization mass velocity I Gmf of the supplied gas,
At this point in time, the heat transfer coefficient on the surface in contact with the fluidized medium changes significantly, and the total heat transfer wrinkles in the heat recovery chamber also change rapidly.

Under such circumstances, if the transfer flp4t is completely controlled by the gas supply to the diffuser, the fluidization mass velocity is substantially in the vicinity of I Gmf and the amount of heat transfer is large,
This results in stepwise control that selects either a state where the fluidization mass velocity is lower than I Gmf and the amount of heat transfer is small, or a state where the gas supply to the diffuser is stopped and the amount of heat transfer is extremely small. .

On the other hand, by installing the diffuser vIt at an angle as shown in FIG. 17, by changing the opening diameter of the gas outlet to the heat recovery chamber 59 of the diffuser depending on the location, Even if is the same, the gas pressure drop is changed by changing its density.Then, the amount of gas flowing into the heat recovery chamber is 19 J! Not only will this condition occur, but the amount of gas supplied to the diffuser may also vary.
This situation will be exacerbated.

For example, if the amount of gas supplied to the aeration device is gradually increased, the increase IK in the amount of gas supplied to the fluidized medium layer from the gas outlet (opening) with relatively small pressure loss through gas flow will become relatively large. , conversely, an increase in the amount of gas supplied to the fluidized medium layer from the gas outlet (opening) with relatively large gas flow pressure loss''4
is relatively small.

For this reason, only the fluidized medium layer above the gas inlet, where the pressure drop during gas flow is relatively small, becomes a fluidized bed, and the rest remains as a fixed bed, or conversely, the gas is introduced, where the pressure loss during gas flow is relatively large. A situation arises in which only the fluidized medium layer near the mouth is a fixed bed and the rest is a fluidized bed.

In other words, as the amount of gas supplied to the diffuser increases, the IA
1. From a fixed bed state in which the fluidized medium bed in the heat recovery chamber has no grooves at the fluidized mass velocity I Gmf of the introduced gas, to a fluidized bed state in which a part of the fluidized media bed is formed at a fluidized mass velocity I Gmf or more, The other becomes a fixed layer, and the ratio of the hearth area occupied by these two gradually changes! The portion in the 1E17 layer state increases, and finally the entire fluidized medium layer shifts to the fluidized bed state.

As a result, regarding the amount of heat transferred in the heat recovery chamber,
As the amount of gas supplied to the air diffuser increases, from a state where the amount of heat transferred is initially less than the fluidized mass velocity I Gmf blown into the heat recovery chamber, a part of the fluidized mass velocity I Gm is blown into the heat recovery chamber.
In the state where the amount of heat transfer is larger than f, and the other part is I Gmf, the ungrooved heat transfer lid remains small, and the area ratio of the heat transfer surface in both states gradually increases in the area where the amount of heat transfer is large, Eventually, the entire system shifts to a state where the amount of heat transfer is greater than the fluidization mass velocity I Gmf. Since the total amount of heat transfer in the heat recovery chamber is the sum of the heat transfer lids in these valleys, the amount of heat transfer will show a gentle increase or decrease based on the increase or decrease in the gas supply to the diffuser. This makes it easy to continuously control.

Examples of this air diffuser are shown in Figures 19, 20, and 2.
Shown in Figure 1.

Figure g/JJ19 shows the opening diameter of a diffuser pipe installed horizontally!
This is an example in which a plurality of gas ejection ports A are provided, and the resistance when gas passes through the ejection ports is different, and the amount of gas passing through the six ejection ports is different. That is, if the opening diameter of the ejection port is A)B)C as shown in FIG. 19, then the gas passage 11 will be A)B>C.

Figure 20 shows that diffuser pipes with jet ports with the same opening diameter are installed at an angle and are proportional. The gas passage jetted from the nozzle is different. That is, if the ejection ports are A%B and C in descending order of the depth of the fluidized medium layer,
The gas flow position is A(B(C).

Fig. 21 shows an example in which the diffuser W' is installed at an angle with jet ports having different opening diameters. The opening diameter of the jet nozzle located in the shallow part is made small to correct the difference in gas passing pressure loss due to the depth of the fluid medium no. by adjusting the opening diameter.

That is, by setting the opening diameter to A)B)C, the gas passage through the valley opening at any design point ii'1A=B
= c, and in this case, below the design point, the gas passage 1 is A(B(C), and above the design point, the gas passage In-A>
B>C can be satisfied.

This previously proposed invention is based on the flow 1-
The main combustion section of the fluidized bed (fluidized swirl 1
Heat recovery t'? r:
steplessly and over an order of magnitude larger range, easily by blowing air t (diffusion 1!t) into the fluidized medium of the circulating layer section.
In view of this, steam is passed through a heat transfer tube inserted in the circulation layer section (PP4 recovery section) to form a steam superheating tube, and the outlet side temperature of the steam is detected, and based on the outlet temperature, the circulation layer section The temperature of the superheated steam obtained by adjusting the opening degree of the damper at the node tX of the supply air to the diffuser pipe is controlled to a predetermined temperature.

That is, when the steam outlet temperature changes to a lower side than the set value, the damper is opened and the diffuser gas tv in the heat recovery chamber of the inserted part before the steam is superheated is increased to increase the amount of heat transfer. The temperature at the outlet side is increased, and when the temperature changes to a higher side than the set value, the opposite is done. By doing so, the superheated steam temperature easily becomes close to the set temperature.

These air diffusers [-gas t supplied to the air diffusers using
FIGS. 22, 23, and 24 show the amount IN of gas blown out from each outlet into the fluidized medium layer when changing the amount of gas.

Figure 22 is a diagram using the air diffuser shown in Figure 19, Figure 23 is a diagram using the air diffuser IIL as shown in Figure 20, and Figure 24 is the same as Figure 21. It is a diagram when using the air diffuser itt as shown in FIG.

In FIGS. 22, 23, and 24, the horizontal axis shows the mass velocity t1 of the gas blown out from the outlet B. The vertical shelf shows the mass velocity t1 of the gas blown out from each outlet.

From these figures, even if the mass velocity of gas blown out from nozzle B is less than I Gmf, if the mass velocity of gas blown out from other nozzles is greater than I Gmf, or nozzle B is also blown out. The mass velocity of the gas is I Gm
It is clear that even if the gas velocity is greater than f, the mass velocity of the gas blown out from other nozzles may be less than I Gmf. The relationship between the mass velocity of gas blown out from each nozzle shown in Figures 23 and 24. The horizontal axis shows the nozzle, and the vertical axis shows the mass velocity of gas blown out from each nozzle. Figure 25 is a diagram corresponding to the case where the air diffuser as shown in FIG. 19 is installed. % FIG. 26 is a view corresponding to the case where the air diffuser l' as shown in FIG. 20 is installed.

FIG. 27 is a diagram corresponding to the case where a diffuser as shown in FIG. 21 is provided.

In these figures, each plot under the same supply gas to the diffuser is connected by a polygonal line.

In this way, when the gas mass velocities differ depending on each ejection port, the total heat transfer t is the product of the heat transfer area in the region corresponding to each ejection port and the heat transfer coefficient according to each fLwJ mass velocity. It becomes peace. For example, in Figures 25 to 27, the gas t supplied to the diffuser at which the fluidization wave velocity becomes I Gmf differs depending on the ejection port. No change occurs. When the amount of gas supplied to the diffuser is increased, the heat transfer surface in the area corresponding to each nozzle will gradually change to a heat transfer surface at I Gmf. Moreover, when the amount of supplied i11 direction is decreased, the opposite phenomenon occurs. Therefore, when using either of the examples 3') shown in FIGS. 19 to 21, the characteristics of the increase and decrease in the amount of heat transfer with respect to the increase and decrease in the amount of gas supplied to the diffuser are gentle as described above. It can be done. In the case of proportionality as shown in FIG. 21, for example, as shown in FIG. 24, the design can be such that the amount of gas blown out from each nozzle at a mass velocity of 2 Gmf becomes uniform.

By doing this, as shown in Fig. 4, the area where the mass velocity is 2 Gmf or more, that is, the area where the amount of heat transfer becomes negative and the wear rate of the heat transfer surface increases rapidly depending on the mass velocity. It can be designed so that the operating point where the
The jet nozzle A in the figure and the jet nozzle C in FIG. 23 are 2 Gmf or more, but in the example shown in FIG.
If it is 2 Gmf, all other nozzles will also have uniform gas flow wrinkles of 2 Gmf. In other words, the wear rate of all the heat transfer surfaces of the heat recovery chamber is small, and it is possible to obtain the heat recovery box with the lowest potency.

Note that the matching point for the amount of gas passing can be easily designed based on the diameter of the jet port, the density of the jet port, the depth from the surface of the sand in the heat recovery chamber to the nozzle, etc.

For this reason, as shown in Fig. 21, the diffuser is installed diagonally, and the outlet at a deep position is
It is preferable to increase the nozzle density 〇The relationship between the supply gas mass velocity and the heat transfer surface when used on a diffuser like this ↓ is that the diffuser is installed horizontally and the openings of the nozzles are uniform. FIG. 28 shows a comparison with a case in which it is provided so that

In %@28, the curve y shows the case where the air diffuser having a uniform outlet metal is installed horizontally, and the curve X shows the case where the air diffuser as shown in FIG. 21 is installed.

From the curve shown in Figure 28, by installing the diffuser a diagonally and increasing the opening diameter of the nozzle closer to the gas introduction part, the characteristics of increase and decrease in the heat transfer surface due to increase and decrease in the amount of supplied gas can be controlled. Slope (curve X)% Therefore, supply gas Jl@:1
It is clear that by adjusting i11, the amount of heat transfer can be easily and continuously controlled.

In addition to this disproportional effect on flow.

As in the present invention, in a 1 m layer that descends in a shearing manner due to the action of the fluidized medium G1 flowing in from the combustion section by blowing gas, the average diffused gas area i, 50 to f
Below the front and back, the effect of moving JfI of 11% makes it even more gradual.

That is, the heat transfer coefficient below I0~f is several times larger than that of the solid foot layer and increases in proportion to the amount of diffused gas, and even when the amount of diffused gas exceeds 10~f'i, the heat transfer coefficient The effect of this makes it difficult to liquefy. As a result of the two-dimensional fluidization at 1~f and 50~f, the grooves in Figure 29 are 0~2 Gmf.
The relationship between the heat transfer coefficient and the average amount of gas diffused in the heat recovery chamber can be obtained.

The amount of heat recovery can be rapidly controlled by the amount of air diffused in the heat recovery chamber, as will be described later.

Next, the relationship between the height of the fluidized bed and the amount of circulating fluidized medium will be explained in more detail.

Flow) - When the surface is lower than or at the same position as the top of the reflective partition, the gas flow that rises downward along the reflective partition is given direction by the reflective partition and ejects from the fluidized bed along the reflective partition. However, along with this, the flow 11tJJ medium is also given direction and ejects mainly on the flow # surface near the reflective partition.

The ejected gas flow differs from inside the flow 1-, where the fluid medium filled in the flow path circle disappears and the cross section of the flow path widens rapidly, so the jet also becomes agitated and becomes a gentle flow with a flow velocity of 1 m/sec or less. The fluid medium that was evacuated upwards and thus entrained must have a particle size of 1 ms+ to be carried by the flow velocity.
It licks back and forth and falls without losing kinetic energy due to gravity and the friction with the exhaust gas. Due to inertia, some of the particles will jump over the combustion section and into the heat recovery section. However, the flight distance of the fluidized medium ejected from the fluidized bed surface is 1 to 1 due to the relationship with the particle size or specific gravity. Only when the width of the furnace is 1 to 2 m or less can the amount of fluidized medium necessary for heat recovery and prevention of overheating of the fluidized medium in the heat recovery chamber be secured.

By the way, when the surface of the fluidized bed is above the top of the reflective partition, the higher the R,m layer height, the more the fluidized gas gathered by the partition will be blown up almost directly above the top of the reflective partition. As the gas ejection direction changes, the fluidized medium is blown up from the surface of the fluidized bed mainly near the top of the reflective partition as shown by arrow a in Figure 5, and then falls down, making it easy to damage the reflective partition. In other words, a large amount of heat will enter the back side of the engine, that is, the heat recovery chamber.

In other words, the larger the flow l-height, the closer the directionality of the ejected ia medium due to the reflective partition is to the directly upward direction, and as the height of the fluidized bed increases, more fluid medium enters the heat recovery chamber, resulting in an increase in the flow rate. The ratio is the joist whose distance from the top of the reflective partition to the height of the fluidized bed is small.

In FIG. 5, 66 is a combustion material inlet provided at the top of the furnace 51, and 67 is an air/water drum provided near the exhaust gas outlet 68, which forms a circular path with the heat transfer w65 in the heat recovery chamber 59. ing. 9, 69 is an incombustible material discharge port connected to the outside of both side edges of the distribution plate 520 at the bottom of the furnace 51, and 70 is a screw conveyor having a screw 71 disposed in a reverse thread direction.

The combustible material F introduced into the υ furnace 51 through the combustible material inlet 66 is combusted while flowing together with the fluidized medium swirled by the fluidizing gas. At this time, the fluid medium near the upper center of the air chamber 55 does not move violently up and down, but forms a downward movement 1if in a weak flowing or moving state.

The width of this moving layer is narrow at the top, but becomes slightly wider at the bottom due to the effect of the slope of the dispersion plate 52, and a part of the bottom is above the air chambers 54 and 56 on both side edges. Since the inner air chamber reaches the inner air chamber, it is blown up by the injection of fluidizing gas at a large mass velocity. Then, part of the fluid medium at the hem is removed, so Iil# directly above the air chamber 55 descends under its own weight.

Above this layer, the fluidized medium from the fluidized bed is replenished and deposited as described later, and by repeating this, the fluidized medium above the air chamber 55 forms a moving layer that gradually and continuously descends. 0 The fluidized medium that has moved above the air chambers 54 and 56 is blown upward, but it hits the reflective partition 5B and is reflected and turned into the furnace 51.
fL is rotated toward the center of
A part of the moving medium passes over the top of the reflective partition 58 and enters the heat recovery chamber 5.
Enter 9 yen. If the sedimentation speed of the fluidized medium deposited in the heat recovery chamber 59 is slow, an angle of repose is formed in the upper part of the heat recovery chamber, and the excess fluidized medium falls from the upper part of the reflective partition to the combustion section. Heat recovery chamber 59 The fluid medium that has entered the circle is transferred to the air diffuser IL.
A circulating layer of the fluidized medium is formed, which gradually descends while moving without flowing or sliding down due to the gas blown from the 62, and after heat exchange with the heat transfer surface, reflection occurs. It is returned to the combustion section through the opening 63 at the lower end of the partition.

The mass velocity of the diffused gas introduced from the diffuser 62 in the heat recovery chamber 59 is 0 to 30 mf, preferably 15 to 2 mf.
It is selected from values within the range of Gmf.

The reason for the seventh reason is that, as shown in FIG. 4, (when the diameter is 30 mf or less, the heat transfer coefficient is large and the wear rate is small.

Further, the mass velocity of the diffused gas in the heat recovery chamber 59 is set from 0 to I.
When Gmf is changed, the settling velocity of the moving layer in the heat recovery chamber changes dramatically as shown in FIG. 9, and the required amount of high-temperature medium can be arbitrarily controlled. However, R
When heat is recovered from the fluidizing medium, the flow rate decreases and good combustion is no longer possible.If the fluidizing gas t in this part is set to 0, the heat recovery from the fluidizing medium may be stopped and the operation performed. can. In addition, the heat recovery section is filtered outside the main combustion area of the furnace 51 yen. kfi #) Since the heat exchanger tube 65 does not have strong corrosive properties like the returning atmosphere, it is less susceptible to corrosion than the conventional one, and as mentioned above, the flow velocity is low in this part. , wear of the heat exchanger tubes 65 is also extremely small.

In the range of the mass velocity of the fluidizing gas from 15 to 2 Gmf, the gas velocity is actually extremely low at a fluidizing medium temperature of, for example, 800°C, depending on the particle size of the fluidizing medium, α1 to 14 m/s (superficial velocity of It's speed.

If there is a non-combustible material with a diameter larger than the fluidized medium in the combustion material, the combustion residue is discharged from the screw conveyor 70 at the bottom of f along with a part of the fluidized medium.

In addition, the heat transfer inside the heat recovery chamber 59 is conducted between the fluidized medium and the heat transfer w65.
In addition to heat transfer through direct contact with the gas, there is also heat transfer through the medium of gas, which rises while vibrating violently and irregularly due to the flow of the fluid medium. In the latter case, in contrast to the normal gas-solid contact state, there is almost no boundary layer on the solid surface that impedes heat transfer, and the fluidized medium is well stirred by the flow, so it is stationary. Unlike a medium, heat transfer in powder can be ignored, and it has seven extremely large heat transfer properties.

Therefore, in the heat recovery chamber of the present invention, compared to normal heat recovery from combustion gas, the heat transfer coefficient can be nearly 10 times Fi at the maximum.

In this way, the heat transfer phenomenon between the fluidized medium and the heat transfer surface largely depends on the amount of blown gas, and the amount of fluidized medium circulation can also be adjusted by adjusting the amount of gas introduced from the diffuser 62. By making the heat recovery chamber 59 using the moving bed independent from the main combustion chamber in the furnace, it is possible to provide a fluidized bed heat recovery device that is compact, has a large turndown ratio, and is easy to control.

In boilers that use combustible materials with a slow burning rate such as coal or petroleum coke as fuel, even if you want to change the evaporation rate suddenly, it is often only possible to change it at a rate commensurate with the burning rate. - Membrane fluidized bed In the boiler, although the combustion rate itself has been improved, it is still worse because heat is recovered through the flow N1.

However, in the method described in connection with FIG. 5, the heat transfer a in the heat recovery chamber can be instantaneously changed from several times to several minutes by changing the gas diffusion t. Therefore, although a change in the amount of heat input to the fluidized bed due to a change in the combustion material supply liquid depends on the combustion rate and causes a time delay, the heat recovery section from the fluidized medium in the heat recovery chamber of the present invention is It can be rapidly changed in an air chamber, and the difference between the heat input wrinkle and the heat recovery rate can be treated as a temporary temperature change in the temperature of the fluidized medium due to the sensible heat storage capacity of the fluidized medium that forms the fluidized bed. It can be absorbed. As a result, heat can be used without waste, and it is possible to control the amount of evaporation with a high degree of followability, which was not possible with conventional coal-fired boilers.

The position of the incombustible material discharge port 69 is, for example, the lower opening 6 of the reflective partition 5B of the heat recovery chamber 59 as shown in the figure.
3 and both side edges of the air distribution plate in the furnace 51, but the present invention is not limited thereto.

In addition, the flow IJ prevents discharge of the fluidized medium from the heat recovery chamber 59 to the incombustible material discharge port 69 due to a short circuit, and effectively allows the medium after heat transfer to pass through the combustion chamber! In order to return to seven layers, it is also preferable to provide a partition 50, and this partition 5so is shown in FIGS. 10 and 1.
As shown in FIG.
It can also be formed using the furnace wall as shown in the example shown in the figure.

In FIG. 5, the air dispersion plate 52 has a chevron shape, and the air chambers have a royal air chamber (54, 55, 56).

Although the case has been described in which the mass velocity of the fluidizing gas ejected from the air chambers 54 and 56 is higher than the mass velocity of the fluidizing gas ejected from the air chamber 55, the mass velocity of the air blown into the lower part of the fluidized bed is the same. However, due to the action of the reflective partition, the air flow velocity in the part along the reflective partition is higher than that in the center, and it is possible to completely form a swirling flow in the fluidized bed, so that air is ejected from each air chamber. The mass velocity of the fluidizing gas may be the same, and for the same reason, the seventh
As shown, the air distribution plate 52 may be horizontal and may have a single air chamber 56'. Nine, in this case air chamber 5
6' may be divided into several chambers instead of one chamber.

When the air chamber is divided into several chambers, it is natural that each chamber may have a different velocity as explained with respect to the mass velocity 'kwJ5 diagram of the fluidizing gas.

Furthermore, when burning a combustible material such as coal that has few incombustible discharge ports, the noncombustible discharge port can be omitted as shown in FIG.

Next, another embodiment is shown in FIG. The swirling fluidized bed type heat recovery apparatus shown in FIG. 12 includes a swirling fluidized bed 2 shown in FIG.
two are provided in the same furnace, therefore, the heat recovery chamber 59 in the central part
is exactly the same except that it is provided between the back and rear surfaces of the reflective partition 58 in the central part 2') and that the lower partition of the heat recovery chamber 59 in the central part has the structure shown in FIG.

Next, further other embodiments are shown in FIGS. 13, 14, and 15.
It is shown in FIG.

In these embodiments, the only difference is mainly in the shape of the reflective partition 5B and its mounting. And the embodiment shown in FIG. 14 is 1') swirling fluidized bed'?
This is a drawing showing an actual example of a case where a heat recovery section is installed in a furnace with r:.

In addition, FIG. 14 is a diagram showing an example 7 in which the gas distribution plate 52 is made horizontal in the swirling flow type fluidized bed furnace shown in FIG. Therefore, its operation is similar to that described with reference to FIG. In FIG. 14, reference numeral 69' indicates a fluidized medium discharge nozzle.

In FIGS. 13, 14, 15, and 16, symbols 50 to 71 have the same meanings as explained in FIGS. The provided header 83.84 indicates a friend header provided in the furnace.

In the examples shown in Figures 13, 14, 15, and 16, the furnace wall is composed of a membrane outer wall. The water is branched from the headers 86 and 84 (example shown in Figure 16 only) provided, and reflective partitions 58 are attached to the lower diagonal portions of each membrane/wall partition. The torpedo groups shown in these drawings are bent at one or two places9 to absorb thermal expansion, and are fixed with upper and lower headers, so they can withstand intense movements of the fluid medium. The vertical part of the O primary water t80 that can withstand it is long enough to penetrate the top of the fluid medium, so incombustibles do not accumulate on the upper slope, and the passage resistance is small, making it non-combustible. To prevent clogging 1i-by objects, etc., torpedo 8
0 i! [The portions and the portions of the lower opening 63 of the heat recovery chamber 59 are preferably arranged in a staggered manner as shown in FIG.

Further, as shown in FIG. 17, it is preferable that the heat transfer w65 is similarly arranged in a staggered manner, and the air diffuser (air diffuser '#)
62 are preferably provided at the bottom of the heat recovery chamber along the back side of the reflective partition 58, as shown in FIGS. 13 to 16, instead of being arranged parallel to the heat transfer tubes at the bottom of the heat recovery chamber. .

By making the gas outlet in the part of the diffuser tube near the gas outlet large and gradually decreasing it toward the tip, it is possible to diffuse air more uniformly regardless of the depth of the fluidizing medium.

The lower end of the reflective partition 58 is preferably located outside the end of the dispersion plate 52 in a region where the fluid medium is not in a rapid flow state. The reason for this is to prevent the heat recovery chamber from being affected by the intense fluidized bed and to facilitate control of the sedimentation rate of the fluidized medium within the heat recovery chamber.

Also, the purchasing speed of fluidized gas from the lower part of the moving bed in the combustion section is 15 x 50 m! , preferably 1 to z5Gmf, and
The amount blown from the lower part of the fluidized bed section is preferably 50 or less.

In addition, as shown in Figs. 15 and 14, when the combustible material is directly fed into the downward moving bed by the combustible material input device f166, the supply of powdered coal etc. to the combustible material has a scraping effect on the fluidized medium. This allows for continuous operation, less air leakage from the feeder, higher combustion efficiency of powdered coal, etc., and even when the operation is stopped, the IJ-
It is not necessary to close off the gap between the supply section and the furnace with a T-damper to prevent the heat inside the furnace from igniting the remaining combustible materials in the supply section and burning the supply section. do not have.

In addition, combustible materials including bulky items such as municipal waste and garbage are shown in Figure 5.
As shown in Fig. 7, Fig. 12, Fig. 15, and Fig. 16, it is installed in the ceiling and can be operated without difficulty by inputting it from the next installation inlet. In the case of combustion, it is preferable to introduce the material into the combustion section from a position higher than but lower than the surface of the fluidized bed on the side wall of the combustion section using a spreader such as a rotating blade. When used as a dedicated combustion furnace for solid fuel such as coal, the above-mentioned spreader alone may be used without providing a ceiling inlet, or the combustible materials including coarse materials are injected through the ceiling inlet, and the solid fuel is injected into the above-mentioned spreader. In the swirling FI-type fluidized bed boiler equipped with the heat recovery chamber described above, heat recovery can be controlled by controlling the airflow to the air diffuser. Therefore, as part of the utilization of this boiler, the present inventors further divided the heat recovery chamber and injected steam as a heat-receiving fluid into at least some of the heat transfer tubes in a part of the divided heat recovery chamber. The amount of gas supplied to the diffuser is adjusted based on the temperature on the downstream side of the heat recovery chamber of the steam, and the amount of gas supplied to other diffusers is adjusted based on the temperature of the fluidized bed. proposed a steam temperature raising device for a fluidized bed boiler that obtains superheated steam at a predetermined temperature and controls the fluidized NI temperature to a constant temperature by adjusting the amount of gas supplied to the steam device (Japanese Patent Application No. 159,707/1982) issue).

That is, this device will be explained based on Figure @50.

In FIG. 30, the bottom of the furnace 1 is equipped with a dispersion plate 2 for fluidizing gas introduced from the fluidizing gas inlet pipe 3 by the blower 7, and this dispersion plate 2 is shown in FIG. Like the furnace 1, it is formed into a roof shape that is almost symmetrical with respect to the center of the furnace 1.

The fluidizing gas sent from the blower 7 is sent to the air chamber 4,
The mass gas velocity of the fluidizing gas (mass gas velocity 1 is the fluidizing medium'
The minimum air volume required to fluidize the fluidized medium in the furnace 1 is set to a velocity sufficient to form a fluidized bed of the fluidized medium in the furnace 1, but the velocity Fi of the fluidizing gas ejected from the central portion 5 is smaller than the former. To be elected.

The upper part of the air chambers 4 and 6 at the inner edge blocks the upward flow path of the fluidizing gas, and reflects and diverts the fluidizing gas blown out from the air chambers 4 and 6 toward the center of the furnace 1. A reflecting wall partition 8 is provided, and the difference between this reflecting wall partition 8 and the mass velocity of the ejected fluidizing gas causes a swirling flow in the same direction as indicated by the arrow in FIG. - A part of the circulation of the fluidized medium (a heat recovery section 9.9' is formed between the reflective partition 8 and the furnace wall, and during operation, a part of the fluidized medium circulates over the upper end of the reflective partition 8). It enters the layer parts 9, 9'. Also, the circulation layer part 9
．． At a high level in the bottom area of the furnace at the bottom of 9', there is an aeration device 1 that introduces gas from the blower 10 through the introduction pipe 11°11'.
2.12' is provided at the f+ position along the back surface of the reflective partition, and on the introduction pipe 11.11' there is a next flow rate regulating damper 24°24' for controlling the diffused air t introduced into the diffuser. is provided. In addition, the air diffuser 12 of the circulation layer section 9, 9'
．． Openings 13 and 13' are provided in the vicinity of the 12'i installation, so that the fluidized medium that has entered the circulating bed portions 9, 9' is continuously formed on the moving bed and sedimented depending on the operating conditions. , and circulates through the openings 15° and 15' to the combustion section.

In addition, heat transfer tubes 15 and 15' for passing steam and heating boiler water are arranged in the circulation layer sections 9 and 9', which are connected to the waste heat point 17 through pipes 14 and 2 degrees, and are connected to the circulation layer section downward. By exchanging heat with the moving fluid medium, the distribution of g
The pipe 20' is configured to obtain superheated steam from the boiler 14' and to circulate boiler water mixed with heated and generated steam to the waste heat boiler 17 to recover heat.

Then, the temperature of the steam extracted from the arrangement W14' is measured by the total temperature measuring device 21, and based on this temperature, the temperature controller 2
2, the opening degree of the flow rate adjustment damper 24 is all i! In Section 11, the temperature of the superheated steam is controlled to a predetermined temperature by adjusting the flow rate of the fluidizing gas in the circulation layer section. That is, when the temperature of the superheated steam is lower than the predetermined temperature, the flow adjustment dunk 4
By increasing the opening degree of
By increasing it within the range of 5 to 3, the total amount of fluidized medium circulation is increased, the heat transfer coefficient is increased, and the heat recovery t is increased, thereby raising the temperature of superheated steam to a constant temperature of 1'i. .If the temperature of the superheated steam is higher than a predetermined temperature, the control is reversed to the above.

On the other hand, the temperature of the main combustion part of the fluidized bed is the maximum temperature of the combustion part, for example, 600°C to 800°C for municipal waste, and 800°C to 850°C for coal and coke. When the temperature is lower than a certain temperature or a certain width temperature range, the temperature controller 26 is used to reduce the opening degree of the F flow rate adjustment damper 27 based on the temperature measured by the temperature measuring device 25 in the main combustion section of the fluidized bed. The fluidized medium is circulated by reducing the amount of air diffused into the circulation layer. ! By decreasing r and making the heat transfer coefficient small, the temperature of the fluidized bed main combustion part is controlled so that the temperature of the fluidized bed main combustion part is increased by making the heat recovery t' (f - small). When the temperature rises above a predetermined temperature, the control is performed in the opposite manner to the above to avoid problems such as the temperature of the fluidizing medium rising above the predetermined temperature and causing sintering of the fluidizing medium.

[Problem that the invention seeks to solve]

The steam well shown in Figure 50 has the following features: ■ A steam superheater (or steam reheater) and an evaporator are installed in the same furnace, so changes in the amount of heat recovered by the superheater or reheater are not affected. The load on the evaporator increases because it needs to be absorbed by the evaporator, and because all of the heat is recovered by the evaporator, only about half of the recovered heat can be used for steam rise (superheating or reheating).

■ There is a limit to the amount of heat recovery in the layer, and if the steam superheating temperature rises or the steam reheating temperature rises, the amount of heat will be insufficient. The benefits of eliminating this gas superheater would be lost.

■ The temperature of the heat transfer surface of the steam superheater or reheater is higher than the heat transfer surface of the evaporator9, and when the steam outlet temperature is made high,
The heat transfer surface of the superheater or reheater is CL, Na, K, 8
If waste containing these components is used as fuel, the heat transfer surface should be made of a material with high resistance to high temperature corrosion. It was necessary to use a nickel-chromium alloy, etc. [Structure of the Invention] The present invention provides a boiler for solving the above problems and a control device for efficiently operating the boiler. 1. Equipped with one or more sets of air distribution plates that eject fluidization gas upward from the bottom of the furnace, and blocking the upward flow path of the fluidization gas above the ends of the air distribution plates,
In addition, by providing a reflective partition that reflects and diverts the fluidized gas toward the upper part of the gas jetting part where the upward flow path is not blocked, the fluidized medium is directed toward the upper part of the jetting part where the upward flow path is not blocked. A moving bed that settles in a fixed bed or a fluidized bed state is formed, and the fluidized medium is actively fluidized in the upper part near the spout where the upward flow path is blocked, and the fluidic medium in this part is A swirling flow is created by swirling the fluid toward the top of the moving bed! - forming a heat recovery chamber between the back of the reflective partition and the furnace wall or between the back of the reflective partition and the back of the reflective partition, and during operation, a part of the fluid medium passes over the top of the reflective partition and recovers heat; A gas diffuser for ventilation configured to enter the chamber, and located at the lower part of the heat recovery chamber and on the back side of the reflective partition, for changing the fluidized medium in the heat recovery chamber from a fixed bed state to a weak fluidized bed state. At the same time, two swirling flow overflow bed boilers were installed, each having a heat recovery chamber with an opening communicating above the hearth bottom at the bottom of the heat recovery chamber, and a heat transfer surface through which the heat-receiving fluid passed inside the heat recovery chamber. , - The heat recovery part of the furnace 1 is an air-water drum.

In order to generate superheated steam by passing the steam generated in the steam-water drum or the low-temperature steam collected by a turbine or the like through the heat recovery section of the other furnace 1'. A double-bed swirling flow fluidized bed boiler with a steam superheater and/or steam reheater.

2. In the double-bed swirling flow type fluidized bed boiler described in item 1 above, the steam temperature at which the outlet steam temperature of the steam superheater and/or steam reheater is detected and a steam temperature signal corresponding to the steam temperature is outputted. means for controlling the amount of combustible material supplied to the fluidized bed combustion section of the boiler 1' comprising the steam superheater and/or the steam reheater in response to the detection means and the steam temperature signal; Steam pressure detection means detects the steam pressure of the water drum and outputs a steam pressure signal corresponding to the steam pressure; Nine multi-bed swirling flow &
Fluidized bed boiler 5 In the double-bed swirling flow type fluidized bed boiler described in item 1 above, the outlet steam temperature of the steam superheater and/or steam reheater is detected and a steam temperature signal corresponding to the steam temperature is outputted. Detecting the temperature of the fluidized medium in the fluidized bed combustion section of the boiler 1' equipped with a steam temperature detection means and a steam superheater and/or a steam reheater, and outputting a fluidized medium temperature signal corresponding to the fluidized medium temperature. fluidized medium temperature detection means, and means for controlling the amount of combustible material supplied to the boiler 1' and the set temperature of the fluidized medium temperature setter of the boiler 1'' based on the steam temperature signal; and the fluidized medium temperature signal. Based on Boi 21
″Hands to control the ventilation rate of the aeration gas to the heat recovery section
further comprising a steam pressure detecting means for detecting the total steam pressure of the steam-water drum and outputting a steam pressure signal corresponding to the steam pressure, and detecting the fluidizing medium temperature of the boiler 1 equipped with the steam generator. A fluidized medium temperature detection means for outputting a fluidized medium temperature signal corresponding to the temperature of the fluidized medium, further comprising means for controlling a set temperature of a fluidized medium temperature setting device of the boiler 1 based on the steam pressure signal, and the steam In addition to providing means for controlling the amount of combustible material supplied to the boiler 1 based on the pressure signal,
A double-bed swirling flow type fluidized bed boiler, comprising means for controlling the ventilation tk of the aeration gas to the heat recovery section of the boiler 1 based on the fluidized bed medium temperature signal.

4. In the enuresis type swirling flow fluidized bed boiler described in the above paragraph 1 or 3, a steam pressure detection means for detecting the steam pressure of the steam-water drum and outputting a steam pressure signal corresponding to the steam pressure. In addition, an evaporation amount detection means is provided which detects the flow rate of steam supplied from the steam drum and outputs a logarithmic signal sound based on the steam amount, and detects combustible gas to the poi 21 based on the steam pressure signal and the steam amount signal. A double-bed swirling flow type fluidized bed boiler equipped with a means to fully control the amount of material supplied.

and 5. In the double-bed swirling flow type fluidized bed boiler 2 described in item 1, 2, 3, or 4, the amount of combustible material supplied to the boiler 1 and/or 1' is further detected. A double-bed swirling flow system equipped with a means for controlling the amount of combustion air supplied to the boiler 1 and/or 1' based on a combustible material supply amount signal that outputs a signal that is a percentage of each supply amount. This is a type fluidized bed boiler.

Next, the present invention will be explained in detail based on the drawings.

FIG. 1 is a schematic diagram showing an embodiment of the present invention, in which swirling fluidized bed voids 21 and 1' having heat recovery chambers 9 and 9', respectively, are provided. The movement of the fluidized bed, the heat recovery chamber, etc. are as explained above, but in the present invention, the air-water drum 1 is
Canned water is supplied from 9 through the pipe W20'i, and after being heated, it is transferred to the steam drum 19 through the piping 20' to generate steam.Canned water is supplied into the heat transfer tube 15 as described above. Because the heat transfer surface is not exposed to high temperatures, the fuels supplied to the furnace 1 through the fuel supply device 17 are Ct, Na, and K.

There is no problem in supplying all the cities, such as those with a high content of SO4 groups, etc. Therefore, the furnace 1 can be used as a garbage-only furnace or a mixed combustion furnace of garbage and coal, etc. Note that part or all of the canned water supplied to the heat transfer tubes of the heat recovery section 9 may be replaced with upper boiler water.

Next, the steam generated in the air/water drum 19 is transferred to the pipe 14
The steam is then supplied to the heat transfer f15' of the heat recovery section 9' of the furnace 1', where it becomes superheated steam and is drawn out through the pipe 14'. When generating high-temperature steam, the heat exchanger tube 15' is exposed to relatively high temperatures, so the fuel supplied from the fuel supply device 17' to the furnace 1' is Ct, Na, or Ct, which causes high-temperature corrosion.
It is preferable to supply coal with a low content of K, 804 groups, etc. By doing this, the heat exchanger tube 15'
There is no need to use an expensive alloy containing N1 and Cr as the material.

First, regarding the boiler, a steam pressure detector 25 is installed on the steam extraction pipe 14 of the steam drum 1, and the steam pressure detected by the steam pressure detector is measured. The signal is compared with a set value in the pressure controller 31, and the comparison value and the steam flow rate signal from the steam flow rate detector 14a provided on the steam extraction pipe 14 are inputted to the full computing unit 34, and calculations are performed to determine the steam pressure and When the steam flow rate is lower than a predetermined value, the rotation speed of the motor 16 of the combustion material supply device is increased based on the calculated value and the fuel supply amount is increased. The fuel supply amount is controlled to be small based on the calculated value. In this case, when the required control accuracy may be low,
It is also possible to perform all control based only on steam pressure.

The primary steam pressure detector 23 may be provided directly on the steam/water drum 1.

On the other hand, the pressure comparison signal from the pressure controller 31 is input to the comparator 52, and the set value of the comparator 32 is completely changed. The set value of the comparator 32 is increased, and it is compared with the temperature signal from the temperature reading device 25 in the fluidized bed, the temperature signal and the set value are compared, and the heat is recovered based on the comparison signal. The aeration air volume controller 33 to the aeration section 9 controls the pulp 11a on the aeration air supply pipe in the direction of closing, and the aeration pipe 12
Heat recovery i in the heat recovery section 9 by reducing the amount of diffused air
Control is performed so that i'ft is small. In addition, pressure detector 2
If the pressure detected in step 3 is lower than the predetermined value, the control is performed in the opposite manner to the case where the pressure is high, and the amount of heat recovered in the heat recovery section 9 is controlled to be large, increasing the amount of water evaporation, and reducing the amount of air. The steam pressure extracted from the steam extraction pipe of the water drum 1 is controlled to be high.

Next, control of the swirling flow type fluidized bed POI 21' in which the heat recovery section is a steam heater (or steam reheater) will be explained.

In controlling the steam boiler 2, the temperature of the steam heated by the heat exchanger tube 15' of the heat recovery section of the fluidized bed boiler 1'' through the steam introduction tube 14 is detected by the steam temperature detector 21 installed on the extraction tube 14'' of the nine steam. The temperature signal is compared with a set value in the temperature controller 31', and the comparison value and the steam flow layer signal from the steam flow rate detector 14a provided on the steam extraction pipe 14 are inputted to the calculator 34' to perform calculations. If the steam temperature and steam flow rate are lower than predetermined values, the rotation speed of the motor 16'' of the fuel supply device 17'' is controlled based on the calculated values to supply fuel, such as coal.
′? 1-pA clause. That is, when the steam temperature and steam flow rate are lower than predetermined values, the fuel supply device 17
The motor 16' of the fuel supply device 117' is controlled to increase its rotation speed and the amount of fuel supplied, and if the steam temperature and the steam R, t are higher than predetermined values, the motor 16 of the fuel supply device 117' is controlled to increase the rotation speed of the motor 16' of the ' is controlled to be small and the fuel supply t is small.

In this case, when the required control accuracy may be low, control may be performed based only on the steam temperature.

On the other hand, the comparison value from the temperature controller 31' is transferred to the comparator 32.
' to change the set value of the comparator 32'. That is,
For example, if the temperature detected by the steam temperature detector 21 is higher than a predetermined value, the set value of the comparator 32' is increased based on the signal from the temperature controller 31'', and the temperature of the fluidized bed boiler 1' is increased. The temperature signal from the temperature sensor 25'' in the fluidized bed is compared, the temperature signal is compared with a set value, and the aeration air volume controller 35' in the heat recovery section 9' is activated based on the comparison signal.
The pulp 11a' on the diffuser air introduction pipe 1' is controlled in the direction of closing to reduce the diffused air t from the diffuser pipe 12', thereby reducing the heat recovery tt in the heat recovery section 9' and lowering the steam temperature. to control. Further, when the temperature detected by the steam temperature detector 21 is lower than a predetermined value, the opposite control to the above-mentioned case when the temperature is high is performed, and the heat recovery section in the heat recovery section 9' is controlled to be large, so that the steam temperature control so that it is high.

In the present invention, since the fluidized bed boiler 21 is controlled based on the pressure of steam drawn from the steam/water drum, it is possible to prevent the pressure of the steam/water drum from becoming higher than a predetermined value. Since the control is based on the steam temperature,
It is possible to supply steam at the temperature desired by the user.Next, in addition to the control mechanism shown in Figure 1, there is a means for controlling the combustion air supplied from the bottom of the fluidized bed according to the amount of fuel supplied. will be explained based on FIG.

In addition, except for the one installed in the hand &' that controls combustion air
Only the combustion air control means will be described, since they are exactly the same as the means shown in the figure.

As explained previously, the amount of fuel supplied to the fluidized no-boiler 1 is controlled based on the calculated value output from the calculating unit 34, but in the apparatus shown in FIG. Based on the value signal, the combustion air amount controller 35 controls the pulp 57 on the combustion gust pipe 3, thereby controlling the amount of combustion air to be supplied in accordance with the amount of combustibles supplied.

That is, when the steam pressure and the steam flow rate are lower than predetermined values, the rotation speed of the motor 16 of the fuel supply device is controlled to increase the amount of fuel supplied based on the calculated values output from the computing unit 54. Based on the calculated value, the combustion air amount controller 35 controls the pulp 36 on the combustion nitrogen pipe in the direction of opening, so as to supply an amount of combustion air commensurate with the amount of fuel supplied. . Naturally, when the steam pressure and the steam flow wave are higher than a predetermined value, the VC performs the opposite control to the above.

Efforts are made to control the combustion air according to the amount of fuel supplied.
It becomes possible to operate with a constant air ratio in the fluidized bed, which enables operation with low aeration and high desulfurization and denitrification efficiency.

The amount of combustion air supplied to the fluidized bed boiler 1' is controlled in exactly the same manner as the fluidized bed boiler 21, except that it is controlled based on the temperature signal on the steam extraction pipe.

Note that the swirl flow fluidized bed boilers shown in Figures 5, 7, 12, 13, 14, 15, and 16 are also based on Figures 1 and 2 above. As explained above, if two units are installed on the boiler, it can be operated in the same way as the boiler. In this case, it is preferable to provide one heat recovery device from the air/water drum and the combustion gas for common use.

[Brief explanation of the drawing]

FIG. 1 is a schematic diagram showing a double-bed rotating light rotating bed boiler of the present invention and a means for controlling the supply amount of combustible material (fuel) and the desired air for aeration, and FIG. 2 is a schematic diagram showing the device shown in FIG. 1. A schematic diagram showing a double-bed swirling flow type fluidized bed boiler of the present invention in which a combustion air supply amount control means is further added to the combustible material (fuel) supply amount,
Figure 3 shows the change in corrosion rate of heat transfer tubes in the heat recovery zone in the furnace depending on temperature, and Figure 4 shows the fluidization mass velocity (Gm
f ), a diagram showing the relationship between the heat transfer coefficient and the wear rate, Figure 5 and the seventh factor are one implementation of the swirling flow fluidized bed heat recovery device? I
6 is a longitudinal cross-sectional view of the entire boiler room shown in FIG. 5, taken along arrow A-AM, and FIG. Figure 9 is a diagram showing the relationship between the aeration gas wind II (Gmf) in the heat recovery chamber and the descending moving bed sedimentation velocity, and Figure 10 is the relationship between the opening at the bottom of the heat recovery chamber. 11 is a cross-sectional view for explaining the nine partitions, FIG. 11 is a view taken along line D-D in FIG. 10, FIG. 12, FIG.
5 and 16 are overall cross-sectional views showing other implementation rows of the rotary type fluidized bed heat recovery device, respectively, and FIG. 17 is a cross-sectional view of the first
Drawings for explaining the heat exchanger tubes and air diffuser of the heat recovery chamber in the embodiment shown in FIGS. 3 to 16, and FIG. 18 is the next drawing for explaining the vertical portion of the water tube and the arrangement of the openings. , FIG. 19, FIG. 20, and FIG. 21 are drawings for explaining the installation state of the air diffuser and the state of the opening of the gas outlet provided in the air diffuser, FIG. 22, and FIG. 23. and Fig. 24 show the gas mass velocity from the opening B and the gas mass velocity from the opening A% C when the diffuser as shown in Figs. 19, 20, and 21 is provided, respectively. The drawings showing the relationships, FIGS. 25, 26 and 27, are for the diffuser w as shown in FIGS. 19, 20 and 21 respectively.
Figure 28 shows the correlation between the mass velocity of the gas ejected from the six nozzles in the case of L. 21
Drawing 29 showing the relationship between the average diffused gas mass velocity and the average amount of heat transfer when provided in the diffuser 1 as shown in the figure.
The figure shows the relationship between the average amount of diffused gas in the heat recovery chamber and the heat transfer coefficient, and FIG. 50 is the ninth figure illustrating the case where the heat recovery section is divided into two parts. 1.51...furnace, 2,52...dispersion plate, 4°5.6
, 54, 55, 56.56'... Air amount, 8.58.
...Reflection wall partition% 9,59...Circulation I-section (heat recovery section)% 12.12',62...Air diffuser, 15.6
5... Opening, 15.15', 65... Heat exchanger tube, 1
9.67...Air/water drum, 25...Pressure detector, 2
1, 25.25'... Temperature detector, 23... Steam pressure detector, 31... Pressure controller, 151'... Temperature controller, 52.52'... Comparator, 55 .55'...
・Diffusion wind controller, 64°3'4'--1 computing unit, 55
．． 55'...Combustion air amount controller lit top (mm/Yeqγ) Fig. 8 flow?t tGmf) Arrow E' Gmf HBAR;t! 6 ratio it'IG
+1! Flow/medium J4 ring weighing, +! Fierce JX, C attack? 1 change r*l + rest and 4 Shikou da upper groan i z-h 3 Ogiai Go II L+ mUk--r%'lh'l'At
3GmL=Er15 style! l Onshapo Ring Volume 9th figure! 6th Ojiji 1 Bun Kiryoku" Sushakushi (Gmf) 10 Figures 11 Figure 13 Figure 14 Figure 17 Figure 19 Kaya... Quantity 23rd 0 1Gaf 2G
nf 3Gsprf trick 8a'Se power"
Figure 24 Sekiguchi Bh/Uno η゛suhawktm Figure 25 OA B C
Opening Fig. 26 OA B C Fig. 27 OAB C O Fig. 28

Claims (1)

[Claims] 1. One set or two or more sets of air distribution plates are provided that eject fluidization gas upward from the bottom of the furnace, and above the ends of the air distribution plates, an upward direction of the fluidization gas is provided. By providing a reflective partition that blocks the flow path and reflects and diverts the fluidized gas toward the gas jet section where the upward flow path is not blocked, the gas jet section where the upward flow path is not blocked is At the top, the fluidized medium forms a fixed bed or a moving bed that settles in a fluidized bed state, and at the upper part near the spout where the upward flow path is blocked, the fluidized medium is actively fluidized, and due to the action of the reflective partition. A swirling fluidized bed is formed by swirling the fluidized medium in this portion toward the top of the moving bed, and a heat recovery chamber is formed between the back of the reflective partition and the furnace wall or between the back of the reflective partition and the back of the reflective partition. The structure is such that during operation, a part of the fluidized medium passes over the upper part of the reflective partition and enters the heat recovery chamber, and the fluidized medium in the heat recovery chamber is placed in a fixed layer at the lower part of the heat recovery chamber and on the back side of the reflective partition. In addition to providing a ventilation gas diffuser to change the state from low to weak fluidized bed conditions, an opening communicating above the furnace bottom is provided at the bottom of the heat recovery chamber, and a heat transfer surface through which the heat receiving fluid passes through the heat recovery chamber is provided. There are two swirling flow type fluidized bed boilers equipped with heat recovery chambers, the heat recovery section of one furnace (1) is used as a liquid heater for generating steam in a steam-water drum, and the heat recovery section of the other furnace (
1') A double bed in which the heat recovery section is a steam superheater and/or steam reheater for generating superheated steam by passing steam generated in the steam drum or low-temperature steam recovered from a turbine, etc. Swirling flow type fluidized bed boiler. 2. In the double-bed swirling flow type fluidized bed boiler according to claim 1, the outlet steam temperature of the steam superheater and/or steam reheater is detected and a steam temperature signal corresponding to the steam temperature is generated. output steam temperature detection means and means for controlling the amount of combustibles supplied to the fluidized bed combustion section of the boiler (1') equipped with the steam superheater and/or steam reheater in response to the steam temperature signal; a steam pressure detection means for detecting the steam pressure of the steam-water drum and outputting a steam pressure signal corresponding to the steam pressure; A double-bed swirling flow type fluidized bed boiler is provided with means for controlling the amount of combustible material supplied. 3. In the double-bed swirling flow type fluidized bed boiler according to claim 1, the outlet steam temperature of the steam superheater and/or steam reheater is detected and a steam temperature signal corresponding to the steam temperature is generated. A fluidized medium temperature signal corresponding to the fluidized medium temperature by detecting the fluidized medium temperature of the fluidized bed combustion section of the boiler (1') equipped with an output steam temperature detection means and a steam superheater and/or a steam reheater. and a fluidized medium temperature detection means for outputting the steam temperature signal, and controls the amount of combustible material supplied to the boiler (1') and the set temperature of the fluidized medium temperature setting device of the boiler (1') based on the steam temperature signal. and a means for controlling the ventilation rate of the aeration gas to the heat recovery section of the boiler (1') based on the temperature signal of the fluidized medium and the temperature signal of the fluidized medium; a steam pressure detection means for outputting a steam pressure signal corresponding to the temperature of the fluidized medium; The boiler (
1), comprising means for controlling the set temperature of the fluidized medium temperature setting device and means for controlling the amount of combustible material supplied to the boiler (1) based on the steam pressure signal, and based on the fluidized bed medium temperature signal. A double-bed swirling flow fluidized bed boiler equipped with means for controlling the amount of gas for aeration into the heat recovery section of the boiler (1). 4. In the double-bed swirling fluidized bed boiler according to claim 2 or 3, a steam pressure for detecting the steam pressure of the steam drum and outputting a steam pressure signal corresponding to the steam pressure. In addition to the detection means, an evaporation amount detection means is provided which detects the flow rate of steam supplied from the steam drum and outputs a signal corresponding to the steam amount. ) A double-bed swirling flow fluidized bed boiler equipped with means for controlling the amount of combustible material supplied to the boiler. 5. In the double-bed swirling flow fluidized bed boiler according to claim 2, 3 or 4, the boiler (1
) and/or (1'), and outputs a signal corresponding to the respective supply amount.Based on the combustible material supply amount signal, A double-bed swirling flow fluidized bed boiler equipped with means for controlling the amount of combustion air supplied to the boiler.