KR940000879B1 - Operation control device for fluidized bed combustion apparatus - Google Patents

Abstract

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Description

Operation control device of fluidized bed combustion device

1 is a schematic control system diagram of a fluidized bed combustion apparatus according to an embodiment of the present invention.

2 is a flowchart of operation control according to the present embodiment.

3 is a schematic configuration diagram of a conventional fluidized bed combustion apparatus.

4 is a strength characteristic diagram of combustion ash of sludge coal.

5 is a characteristic diagram showing the relationship between the particle diameter of the flow medium and the fluidization start rate.

* Explanation of symbols for main parts of the drawings

2: porous plate 3: fluidized bed

4: window box 5: sludge bullet

6: sludge coal supply device 7: ash discharge pipe

8: normal coal 9: coal supply device

11: particle size supply separator 18: ratio detection means

30: weight ratio detection signal 31: control unit

32: first weight ratio setting signal 33: second weight ratio setting signal

34: third weight ratio setting signal 38a, 38b, 38c: control signal

48: hard sludge coal 49a: bark

49b: Sodast 51: Extrusion Machine

53: control means

[Industrial use]

TECHNICAL FIELD The present invention relates to the control of the amount of fluid medium discharged from a fluidized bed, and more particularly, to the operation control of a fluidized bed combustor which improves the automation of operation, energy efficiency and the stability of the operation.

[Private Technology]

The fluidized bed combustor forms a fluidized bed by residues of angels or incinerators in the furnace and can raise the temperature in the furnace to 800 to 900 ° C. Therefore, industrial wastes such as EP ash and plastics collected by high moisture content mud or electrostatic precipitator are used. Even low-grade coal such as sludge coal recovered from coal wastewater from coal mines can be effectively used as fuel.

This is because, because of the large heat capacity in the furnace in the fluidized bed combustion apparatus, particularly flame retardant industrial waste and low-grade coal can be burned and burned and incinerated.

In addition, when the heat transfer pipe is embedded in the fluidized bed, the heat transfer rate (heat shear rate) in the heat transfer pipe layer is about 5 to 10 times larger than that of the gas flow of a conventional boiler, and has the advantage of bringing a large amount of heat transfer and efficient energy efficiency. Recently, fluidized bed combustors have been in the spotlight.

Next, a fluidized bed boiler will be described as an example of the outline of the fluidized bed combustion apparatus using FIG. 3.

In the figure, the fluidized bed boiler 1 forms the fluidized bed 3 by the fluid medium, such as coal combustion and sand, on the porous board 2 provided in the bottom part of a furnace. When the air for combustion and fluidization is ventilated to the window box 4 installed in the lower part of the porous plate 2 from a press-fit fan (not shown), the fluidized medium of the fluidized bed 3 through the porous plate 2 in accordance with the increase of the air volume. Vigorously fluidizes as if it is boiling.

Sludge coal 5 which is the main fuel is introduced into the fluidized bed 3 from the sludge coal supply device 6. The injected sludge coal 5 is thermally and physically pulverized by the fluidization motion of the fluidized bed 3 having a large heat capacity, and is dried and ignited momentarily, so that good contact with combustion air is obtained in the fluidized bed 3. Can be burned with efficiency.

Since this sludge coal 5 is a product from the coal mine drainage process, the quality is very poor.

The sludge coal 5 is a heterogeneous mixture with pulverized coal, coal, moisture and accompanying minerals, in particular, clay minerals, and various components of the sludge coal 5 due to changes in the coal seam and changes in the coal process. Table 1 below shows an example of the properties of sludge coal.

TABLE 1

In addition, sample 1 of the coal is sludge coal which is a filter flake, sample 2 is sludge coal which is settled granules, and sample 3 is sludge coal which is a fine grain.

In order to use the sludge coal 5 having unstable granularity as the main fuel, even in the combustion by the fluidized bed 3, for example, when the ash-rich sludge coal 5 is supplied, it is naturally introduced into the fluidized bed boiler 1. Calories are lowered. For this reason, if the supply amount of the sludge coal 5 located near the top of the fluidized bed boiler 1 is increased, incineration ash of the ash-rich sludge coal 5 does not differentiate in the fluidized bed 3 because of its high strength. In addition, since the average medium particles become large because they stay in the fluidized bed 3 as the fluid medium of the opposite diameter, the fluidization itself is slowed down and the fluidized fluidized bed 3 becomes unstable.

Thus, the fluid medium of the assembly which inhibits fluidization is discharged by using the ash discharge pipe 7 as shown in FIG.

On the other hand, in the fluidized bed boiler 1, two types of fuels are used as fuel, sludge coal 5 as a main fuel and ordinary coal 8 as an auxiliary fuel. Sludge coal (5), which is a clay-grade low-grade coal, is supplied from the sludge coal supply device (6) at the top of the furnace, and the bulk coal (8) is supplied from a spreader type coal supply device (9) on the side wall of the furnace. Supply. Since the sludge coal 5 contains clay powder as described above, the ash after combustion maintains its original form. Severe mixing and stirring in the fluidized bed 3 causes the combustion ash to be crushed, resulting in an appropriate particle size as the flow medium, with most of the remainder being left unbroken, as a coarse ash, ie the perforated plate. Even if deposited on (2) to inhibit or fluidize, it does not become an active fluidized state. In addition, debris such as ash or hydrated ash is also included in the coal (8) supplied from the spreader coal supply device (9). During long periods of operation, they are deposited on the bottom of the furnace, causing fluidization to be inhibited. The amount is very small compared with the production amount of the cooking meal resulting from the combustion coal of the sludge coal 5 described above.

FIG. 4 shows various sludge coals formed into pellets having a diameter of 5 mm and a length of 10 mm and burning them in an electric furnace to make a combustion ash and measure the crush strength thereof. As can be clearly seen in this figure, it can be seen that the crush strength of the combustion ash varies greatly depending on the clay powder included. As described above, when the particle size is coarse and an inappropriate particle size as the fluid medium of the fluidized bed 3 remains in the fluidized bed 3 and the average particle size of the fluidized medium in the fluidized bed 3 is increased, weaning may be performed in any manner. It is necessary to keep the particle size of the medium in an appropriate range, for example, in the range of 0.8 to 3.5 mm.

In this way, the particle size adjusting granules 10 of the intralayer media such as silica sand or coal stone adjusted to an appropriate particle size are supplemented from the particle size adjusting powder supply device 11 and the average particle diameter of the fluidizing medium in the fluidized bed 3 is lowered. In addition, the fluid medium in the fluidized bed 3 is extracted from the recirculation pipe 7, fed from the screw conveyor 12 to the sieve 13 and sieved about 4 mm, and the coarse material is removed from the assembling outlet 14. Removed as the waste assembly ash 15, and recover | recovers only the media of an appropriate particle size of 4 mm or less to the hopper 16, and returns to the fluidized bed 3 from the recycle tube 17, and the like.

3 shows a method of extracting a fluid medium, collecting only the fluid medium having an appropriate particle size by filtering the sieve 13, and returning it to the fluidized bed 3 as a method for controlling the particle size of the fluid medium. As shown in the figure, the porous plate 2 is inclined, and a discharge pipe 7 is provided at the center to discharge a flow medium including granulated ash, slag, slaked stones, and the like. At this time, since the flow medium of an appropriate particle size is simultaneously discharged | emitted from the revolving pipe 7, the withdrawn material is collected through the sieve 13 via the screw conveyor 12, and only the ash of an appropriate particle size is collected to the hopper 16, and a recycling pipe is carried out. It returns to the fluidized bed 3 via (17). The inquiry which is not suitable for fluidization is discharged from the assembly outlet 14 of the sieve 13 and becomes the waste assembly ash 15.

[Problem trying to solve the invention]

As described above, in the conventional drawing-out method, increasing the amount of discharge of the flowing medium from the drawing-out tube 7 is not economical because the heat loss caused by drawing out the high-temperature fluidizing medium increases. On the other hand, when the amount of fluid medium discharged is small, granulated ash is deposited on the furnace, which impairs fluidization.

SUMMARY OF THE INVENTION The present invention seeks to overcome this drawback of the prior art, and its object is to provide a motion control device for a fluidized bed combustor capable of maintaining a stable flow state in the long term due to less heat loss due to the discharge of a fluid medium. .

[Means to solve the problem]

The present invention is directed to a fluidized bed combustor equipped with a fuel supply device for supplying fuel, such as sludge coal, and a fluidized medium extraction device in which the amount of outflow of the fluidized medium from the fluidized bed is adjustable in order to achieve the above object. It is.

And granulating ash detection means for detecting the content of granulated ash in the fluidized medium in the fluidized bed, and control means for adding or subtracting the amount of discharge of the fluid medium in accordance with the content of granulated ash detected by the granulated ash detection means. It is to be done.

In the specification of the present invention, the ordinary coal indicates that the calorific value is 3,500 kcal / kg or more, and examples thereof include bituminous coal and lignite. Low-grade coal, which is the main fuel, exhibits sludge coal and the like with lower calorific value than ordinary coal. In addition, the combustion material shall contain various miscellaneous incombustibles such as minerals and metals in addition to ashes produced as combustion.

In order to keep the fluidized bed in good condition and to operate safely for a long time, the particle size of the media in the bed must be adjusted to an appropriate particle size range suitable for the device.

The appropriate particle size range is closely related to the tower speed (the gas flow in the furnace) of the flow device. That is, as an index for determining the state of fluidization, there is a ratio between the fluidization start speed Umf and the tower column speed Uo, Uo / Umf, which are inherent values in the media in the bed. The fluidization start rate Umf of the fluidized medium is mainly determined by the particle diameter, specific gravity, and other physical properties of the fluidized medium. In the fluidized bed combustion apparatus used industrially, since the kind of a fluid medium is decided, what is necessary is just to manage the particle diameter plate of a fluid medium. If there is a distribution in the particle size rather than the uniform particle size, the fluidization start rate Umf is determined by the average particle size. Therefore, when the granulation ash of the fluidized bed gradually increases, the particle size management of the medium in the bed may be performed in consideration of the increase in the average particle diameter.

On the other hand, in the fluidized bed combustion apparatus, the amount of fuel to be burned is determined, and the amount of air supplied correspondingly is generally constant. Moreover, since the size of the furnace is also predetermined, it is not possible to significantly change the tower speed Uo. Therefore, the average particle diameter of the medium in the layer may be adjusted so that the value of Uo / Umf falls within a predetermined range.

5 is a characteristic diagram showing the relationship between the particle diameter of the fluidized medium and the fluidization start rate by 800 ° C. air. Curve A in the figure shows the density of the flowing medium is 2.0 g / cm 3 Curve B shows the density of the flowing medium is 1.4 g / cm 3, curve C shows the density of the flowing medium is 1.0 g / cm 3, and curve D shows the density of the flowing medium is 0.75 g / cm 3 and curve e are curves when the density of the flow medium is 0.50 g / cm 3.

As can be seen from this figure, the flow velocity Umf decreases as the flow medium splits or differentiates and the average particle diameter becomes smaller. In this case, since the tower speed Uo is almost constant, the value of Uo / Umf becomes large. On the contrary, when the average particle diameter of the flow medium is increased due to the increase in the assembly ash, the fluidization initiation rate Umf becomes large and accordingly the value of Uo / Umf becomes small.

If the value of Uo / Umf is less than 1.5 according to various kinds of experimental results, the fluidization may be insufficient or the fluidization may be stopped and the bed may be shifted to a fixed bed state. It burns and becomes a hot spot, and the media in a layer melt | fuse each other and generate clinker trouble.

On the other hand, if the value of Uo / Umf exceeds 8, the media in the bed are scattered out of the furnace and the fluidized bed is not formed well. In addition, inadequate things may occur such that the fuel supplied is unburned and scattered outside the furnace, or the combustion gas is discharged which is not sufficiently deoiled by limestone. As such, in the fluidized bed combustion apparatus, it is necessary to adjust the average particle diameter of the media in the bed so as to fall within the range of 1.5 to 9 of the value of Uo / Umf.

Next, the Example of this invention is described using FIG. 1 and FIG. 1 is a schematic control system diagram of a fluidized bed combustion apparatus according to an embodiment, and FIG. 2 is a control flowchart.

In FIG. 1, 1 is a fluidized bed boiler, 2 is a perforated plate, 3 is a fluidized bed, 4 is a window box, 5 is soft sludge coal, 6 is a sludge coal supply device installed near the top of the tower of the fluidized bed boiler 1, 7 Silver discharge medium discharge device, 8 is general coal, 9 is coal supply device, 10 is particle size control granule, 11 is granule supply device, 12 is screw conveyor, 13 is sieve, 14 is assembly outlet, 15 Is a waste assembly assembly, 16 is a hopper, and 17 is a recycling pipe.

In addition, 18 is a ratio detecting means 19 is a sampling tube, 20 is a sieve, 21 is a fine ash outlet, 22 is an assembly flyout outlet, 23 is a fine fly ash bottle, 24 is a fly ash flow bottle, 25 is a fine fly ash counter, and 26 is Assembly assembly counter, assembly assembly detection means, 27 is weight, 28 is fine ash weight signal, 29 is assembly ash weight signal, 30 is weight ratio detection signal, 31 is control unit, flow state control means, 32, 33, 34 are first , 2nd, 3rd weight ratio setting signal, 35, 36, 37 is motor, 38a, 38b, 38c is control signal, 39 is hopper, 40 is piping, 41 is supply pipe, 42 is belt conveyor, 43 is grinder, 44 And 45 are belt conveyors, 46 and 47 hoppers, 48 hard sludge bins, 49a bark, 49b sodast, 50 grinders, 51 extruders, 52 waste mills and 53 control means.

As described above, one of the great advantages of the fluidized bed boiler is that it can cope with a variety of fuels. In the case of this embodiment, the soft sludge coal 5 having a high moisture content, which is a fine particle having a constituent particle diameter of 2 to 3 or less, and contains a large amount of clay minerals such as kaolinite, and a calorific value of 3,500 kcal / kg or more and an average particle diameter of several For example, ordinary coal 8 such as bituminous coal and constituent particles having a particle diameter of 10 to 15 µm or less, and a hard sludge coal 48 having a low water content and low clay mineral such as kaolinite, are crushed to mm or tens of mm. About 10 to 40 cm and a width of about 3 to 10 cm are technically very difficult to simultaneously burn five types of fuel, such as a bark (49a) having a thickness of about 5 mm or less and soda (sawdust) having a thickness of about 0.5 mm or less.

Tables 2, 3, 4 and 5 below are tables showing the properties of hard sludge coal, soft sludge coal, bark and sodast.

TABLE 2

TABLE 3

TABLE 4

TABLE 5

In order for these fuels to be sufficiently mixed in the fluidized bed 3 and to be combusted in good contact with the combustion air, it is preferable that the size of the fuel at the time of introduction into the bed is in the range of about 0.5 to 50 mm. If it is thinner than this, it will fly to the outside of furnace immediately after inadequate combustion. On the contrary, if it is too large, the temperature of the deposited portion is excessively increased because it precipitates at the bottom of the fluidized bed 3 and does not uniformly disperse in the bed, causing burner trouble due to burnout of the apparatus and ash melting.

Therefore, in fuel supply opening, it is necessary to prevent coarsening by adhesion and coalescence with sticky fuel. On the other hand, the finely divided fuel must be assembled to have a predetermined size.

In this embodiment, the soft sludge coal (5) containing a large amount of clay minerals has a circular ash shape after combustion and has high ash strength, so that an extruder equipped at the tip of the sludge coal supply device (6) 51), pelletized or noodle-shaped, which is about 10 mm or less in size, is introduced into the fluidized bed 3 from the top of the furnace.

The coal coal 8 is sifted to 50 mm or less, and is supplied to the fluidized bed 3 from the spreader type coal supply device 9 provided in the furnace side wall.

On the other hand, the hard sludge coal 48 is fed from the hopper 47 to the grinder 43 by the conveyor 44. In addition, the bark 49a and the sodast 49b are introduced into the grinder 43 together with the hard sludge coal 48 by the conveyor 45 from the hopper 46. The hard sludge coal 48 is crushed to about 50 mm or less by the grinder 43 and mixed with the bark 49a and / or the sodast 49b, so that the hard sludge coal 48 is adhered to the cohesion and coalescence of the hard sludge coal 48. Excessive coarsening by this can be prevented. On the other hand, the particulate soda 49b is fixed by attaching to the hard sludge coal 48, so that combustion is insufficient and scattered outside the furnace. In order to ensure this scattering prevention, the secondary fuel composed of these mixtures is intended to be introduced from the vicinity of the fluidized bed 3.

As mentioned above, a part of the combustion ash is crushed by the vigorous mixing and stirring action in the fluidized bed 3, and the appropriate particle diameter is obtained as the kinetic medium, and most of the remainder is left without being crushed. It is deposited on and inhibits fluidization of the fluidized bed 3. In addition, the solid coal, such as ash or hydrated ash, is contained in the coal (8) supplied from the spreader coal supply device (9), and these are deposited in the furnace during the long-term exercise and fluidization of the fluidized bed (3) is carried out. The amount is small compared with the amount of granulated ash produced by the combustion ash of the sludge coal 5 described above.

As described above, the particle size of the combustion ash of the fuel is rough, and an inappropriate particle size as the fluid medium of the fluidized bed 3 remains in the fluidized bed 3, thereby increasing the average particle diameter of the fluidized medium, thereby maintaining the particle size distribution in an appropriate range. There is a need.

In the embodiment of the present invention, the following operation control is performed.

It is mainly comprised as the ratio detection means 18 and the control part 31 of the control means 53 which concerns on this embodiment, Although these are not shown, they are an input port, an output port, a central processing unit (cpu), and a readout. It consists of a dedicated memory (ROM), a random access memory (RAM), etc. Although not shown in the control means 53, an input device such as a keyboard switch for inputting and setting the condition of the boiler and the setting values described later, a display device such as a display unit for displaying the operating state of the boiler, and the boiler, etc. Display apparatuses, such as a disc clay, which display the operation state, etc., and the printer etc. which record the operation state of a boiler etc. are provided.

As shown in FIG. 1, the intake port of the sampling pipe 19 is inserted in the discharge-out pipe 7. A part of the flow medium collected by the sampling tube 19 is divided into two types of particle size measurements, such as granulated ash and fine grain ash. As for the size of the eye of the sieve of this sieve 20, about 3-6 mm is suitable. The fine ash from the fine ash outlet 21 is fed into the fine ash metering bottle 23, and the granulated ash from the assembly ash outlet 22 is fed into the assembly ash weighing bottle 24, respectively. When the amount is balanced with the weight (27), which is the weight of the assembly of the fine ash measuring bottle (2 3) or the assembly of the weighing assembly (24), the fine ash measuring bottle (23) or the assembly ash measuring bottle ( 24), the ash in the weighing bottles (23, 24) is discharged, and after the discharge is finished, the weighing bottles (23, 24) return to their original positions. The weights of the weights 27 placed on the measuring bottles 23 and 24 are the same in both.

The number of times of up and down of the measuring bottles 23 and 24 within a predetermined time is counted by the fine ash counter 25 and the assembly ash counter 26, respectively, and are output as the fine ash weight signal 28 and the assembly ash weight signal 29. do.

As described above, the metered ash is temporarily stored in the hopper 39 and then sent to the sieve 13 by the tubing 40 to join the other ash. The coarse ash classified into the sieve 13 is crushed by the grinder 50, sent to the hopper 16, and used again, and when it is not necessary to recycle the flow medium, it is discarded as some waste ash 52.

Next, a control flow is demonstrated using FIG.

The first weight ratio signal 32, the second weight ratio setting signal 33, and the third weight ratio setting signal that define the ratio of the granular phase in the fluid medium in step 1 (hereinafter abbreviated as S) ( 34 is input to the predetermined RAM area of the control part 31 via the input device beforehand, and is set. In this embodiment, the first weight ratio setting signal 32 (hereinafter abbreviated as set value S ₁ ) is 25% by weight of coarse ash content rate, and abbreviated as second weight ratio setting signal 33 (hereinafter set value S ₂₎ . be) is assembled to the content of 55% by weight, also abbreviated as a third by weight of the set signal 34 (the set value S ₃ of) the can is determined in the assembly once the content 75% by weight.

Next, from the fine ash weight signal 28 (measurement number W ₁ ) and the assembly weight weight signal 29 (measurement number W ₂ ) obtained as described above, the ratio detecting means 18 occupies the whole in the following equation. The ratio H% of the assembly ash, that is, the weight ratio detection signal 30 is obtained (S ₂ ).

Thus by operation of the assembly once it is determined that the weight ratio H S ₃ is not in the set value S ₃ is greater than (75%). The assembly weight weight ratio H exceeding the set value S ₃ means that the assembly assembly of the fluid medium is proceeding considerably. In this case, the control signal 38 a is output to drive the motor 37, and the granular material From the supply apparatus 11, the granular material 10 for particle size adjustment, such as silica sand and limestone, is thrown into a fluidized bed, and the average input in the fluidized bed 3 is rapidly lowered. In this way, if an abnormality is judged at the initial stage of the control flow, it is possible to respond quickly to an emergency.

If S ₃ is determined to be no, proceed to S ₅ and judge whether or not the weight ratio of the assembly ashes H% is greater than the measured value S ₁ (25% by weight) .If H is smaller than the set value S ₁ , the assembly ashes are small and there are many fine ashes. Therefore, the fluidization is good, so that the soft sludge coal 5 is supplied at a normal operation, that is, at a normal speed, without any special operation, and the fluid medium is ejected from the ash extraction pipe 7 at a normal timing.

If it is determined that S ₅ is no, it is judged in S ₆ whether the assembly weight weight ratio H is between the set value S ₁ and the set value S ₂ . If the result of this determination is an example, it shows the state where the particle size of the fluid medium in the fluidized bed 3 started to become slightly rough.

In this case, as shown in FIG. 1, the control signal 38b is sent to the motor 35, and it is controlled to increase the discharge amount of the movement medium from the rotary discharge pipe 7, thereby preventing coarsening of the particle size of the fluid in the bed. do.

In spite of the manipulation of the flow medium discharged amount from the ash discharge pipe 7 as described above, if the assembly ash in the fluid medium in the fluidized bed 3 increases further, the assembly ash weight ratio H exceeds the set value S ₂ , and the set value S fits between the _second and the set value S _3, S _b is determined to be a no. In this case, the coarsening of the fluid medium which can maximize the amount of outflow of the fluid medium from the ash discharge pipe 7 can be suppressed. In this case, send a control signal (38c), as shown in FIG. 1 as the next unit to the motor 36 to within ridorok control the amount of supply of the assembly meeting the primary generated cause sludge bullet (5) (S _8).

Thus, by controlling the increase in the amount of discharge from the ash discharge pipe (7), the decrease in the supply amount of the sludge coal (5), the increase in the supply amount of the granular material for controlling the particle size (10), the heat loss due to the discharge of the fluid medium is reduced In addition, even if the sludge is burned, it is possible to maintain a safe flow state in the long term, thereby enabling continuous operation.

When limestone is used as the particle size control powder as in the above embodiment, the deoiling effect is also obtained at the same time.

According to the present invention, since the fluidization of the fluidized bed combustion apparatus is stabilized, automation of operation and energy efficiency can be achieved.

Claims (10)

An operation control device of a fluidized bed combustion apparatus comprising a fuel supply device, a medium supply device, and a recirculation device, wherein a fluid medium composed of a fuel and a medium supplied by fluidized air forms a fluidized bed, wherein the content of the coarse ash in the fluidized bed is detected. And a flow control means for subtracting the ash discharge amount and the fuel supply amount in accordance with the signal from the ratio of the assembly ash detection means, the ratio from the assembly ash detection means to the detection signal, and the signal from the ratio detection means. Operation control device of fluidized bed combustion device. The fluidized bed combustor according to claim 1, characterized in that the particle size distribution of the fluidized medium is adjusted to a ratio Uo / Umf of the flow start velocity U of the fluidized air and the tower speed Umf of the combustion apparatus in the range of 1.5 to 8. Control unit. The operation control apparatus for a fluidized bed combustion apparatus according to claim 1, wherein the assembly ash detection means comprises a sampling tube for removing a part of the fluid medium and a classifier for dividing the extracted sample into fine grain and assembly circuits. 4. The fluidized bed control means according to claim 1, 2 or 3, wherein the fluidized bed control means is capable of setting at least three levels of setpoints in accordance with the assembly ash content, and the zones between the setpoints are compatible with the extraction of fuel residues and / or control of the fuel supply amount. Operation control apparatus of the fluidized bed combustion apparatus. 2. An operation control apparatus for a fluidized bed combustion apparatus according to claim 1, wherein said fuel is low grade coal. 6. An operation control apparatus for a fluidized bed combustion apparatus according to claim 5, wherein said low-grade coal is sludge coal. 5. The operation control of a fluidized bed combustion apparatus according to claim 4, wherein the fuel is composed of a low quality primary fuel and a sub-fuel of ordinary coal, and the control of the fuel supply amount includes the control of the ratio of the main fuel and the sub fuel. Device. 2. The operation control apparatus for a fluidized bed combustion apparatus according to claim 1, wherein the fuel supply device comprises a main fuel supply device installed near the top of the combustion device and a sub-fuel supply device installed near the fluidized bed. 9. A fluidized bed combustor according to claim 8, wherein the main fuel is soft sludge coal, the sub-fuel is a mixture of hard sludge coal and buck and / or soast, and the soft sludge coal is formed in a predetermined size. Driving control system. 4. The operation control apparatus for a fluidized bed combustion apparatus according to claim 3, wherein an intake port of the sampling tube is arranged in the outlet tube of the fuel residual gas extraction unit.

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