JPH0215770B2 - - Google Patents

Description

[Detailed description of the invention]

[Industrial Application Field] The present invention relates to a fluidized bed thermal reactor such as an incinerator or a pyrolysis furnace using a fluidized bed, and a method of operating the same. [Prior Art] As a thermal reactor of this kind, for example, in incinerators for municipal waste, fluidized bed furnaces have recently been used, which have better incineration efficiency than stoker furnaces and produce less incineration residue. In that case, if the waste is thrown in in a state of a certain size or larger, it will inhibit the fluidization of the fluidized medium, so to prevent this, it is necessary to pre-process the shredding using a shredder before putting it into the incinerator. I was investing. Therefore, crushing equipment including a crusher is required, which causes problems in terms of space and cost. Also,
By using a shredder, non-flammable foreign substances (irons, hammer heads, bullets,
Concrete blocks, etc.) can cause blade wear and breakage, and combustible but bulky garbage (e.g. futons, blankets, fishing nets, etc.) is difficult to crush, so the crushing power increases or the crushing becomes impossible. This may cause the crusher to stop or cause many problems. Furthermore, in the case of such a problem, the crusher must be disassembled or a person must enter the machine to remove the foreign matter using input, which increases the effort and cost of maintenance. The process had to be stopped, which significantly hindered work efficiency. On the other hand, in terms of incineration capacity, the maximum capacity of the furnaces in operation at the time was approximately 75 tons/24 hours.
Even in the design, the maximum is about 150t/24h,
It was difficult to realize a larger capacity than this. In order to solve these problems, the present inventors developed a fluidized bed furnace that does not require pre-crushing treatment and can be made larger, by rotating the fluidized medium in a vertical plane in the furnace space. A fluidized bed thermal reactor, disclosed in Japanese Patent Application Laid-open No. 124608/1982, was invented as a solution to the conventional drawbacks by circulating a fluidized medium to form a fluidized bed and a moving bed. [Problems to be Solved by the Invention] However, even in the fluidized bed furnace disclosed in Japanese Patent Application Laid-Open No. 57-124608, it was thought that about 300 t/d was the practical limit for increasing the size. For example, in a municipal waste incinerator, the hearth load of a fluidized bed furnace is
Generally, the value is about 450Kg/m ² h. On the other hand, in the fluidized bed thermal reactor invented by the present inventors (Japanese Unexamined Patent Publication No. 124608/1982), a swirling flow is generated by the combination of a moving bed and a fluidized bed as shown in Fig. 11, and large waste In order to move heavy non-combustible materials laterally without settling on the hearth, and to perform effective combustion and discharge of non-combustible materials, there is a limit to the width of the furnace. There is. Here, for example, when calculating the hearth area based on 450Kg/m ² h for a 1000t/d furnace, hearth area A = 1000t/d/24h x 1/0.45t/m ² h = 92.6m
² A = 92.6 m ² divided by furnace width L = 4 m gives approximately 23.2 m. At this time, the hearth module becomes an extremely elongated hearth as shown in FIG. 12, resulting in an unrealistic furnace shape. The present invention aims to eliminate these drawbacks, make it possible to make it extremely large, and also make partial load operation sufficiently possible, so that operation from low load to high load can be performed freely. . [Means for Solving the Problems] The present invention includes a fluidizing dispersion plate, and the dispersion plate has both side edges lower than the central part and is formed in a chevron-shaped cross section that is substantially symmetrical with respect to the center line. Fluidized bed thermal reaction sections in which the fluidized gas mass velocity at both side edges is higher than the fluidized gas mass velocity at the center are arranged in parallel at the bottom of the same furnace almost symmetrically with respect to the furnace center line, A common incombustible material discharge port is provided between each of the distribution plates, and a noncombustible material discharge port is provided at each outer side edge, and fluidizing gas is provided directly above the furnace wall side and the furnace center side of the side edge of each distribution plate. The fluidized bed thermal reaction system is equipped with a reflecting wall that reflects and diverts the upward flow toward the center of each fluidized bed thermal reaction section, and a raw material inlet is provided in the ceiling of the furnace so as to correspond to the center of each distribution plate. In the furnace, each of the raw material input ports is provided with a separately driven dust supply device, and a forced air blower for feeding fluidizing gas below the dispersion plate of each reaction section is associated with each thermal reaction section. A fluidized bed thermal reactor and its operating method are characterized in that each reactor is installed separately. [Example] The present invention will be described with reference to the drawings regarding an example in which a dispersion plate is used as a dispersion mechanism for fluidized air in a municipal waste incinerator. FIG. 1 shows an example of municipal waste incineration equipment using a fluidized bed incinerator 6, in which waste stored in a waste pit 1 is transferred to a hopper 4 by a bucket 3 of a crane 2.
and is supplied to the incinerator 6 through two raw material input ports 48 by two dust supply devices 5 serving as supply devices. The two dust supply devices 5 are each driven separately by separate motors 27. In the incinerator 6, the fluidized air supplied by the two blowers 7 is blown upward into the furnace from the two distribution plates 8, hits the inclined walls 9 on both sides and in the center, and hits the inclined walls 9 on the left and right sides in the vertical plane. A fluidized medium such as sand is made to flow along the swirling flow 10 to form a swirling fluidized bed, and two left and right fluidized bed thermal reaction sections are formed. Furthermore, as will be described later, a descending moving bed is formed in the center of each thermal reaction section, and the swirling fluidized bed and descending moving bed allow the waste to be burnt well in a short time.
Even if crushing is not performed in advance, high combustion efficiency can be obtained without inhibiting fluidization. 11 is a combustion exhaust gas duct, 12 is a non-combustible material discharge device, 13 is a vibrating sieve, 14 is a conveyor for discharging lump non-combustible materials, and 15 is an elevator for collecting a fluid medium such as sand. As shown in FIGS. 2 and 3, for example, the dust supply device 5 has a structure in which a hopper 4 is connected to a conveyor case 20 via a waste inlet 16, and waste outlets 17 are provided at both lower ends. It is being Inside the conveyor case 20, there is a parallel screw center axis 1.
Two screws 21 and two screws 22, which are divided into right and left at the center, are rotatably provided around the screws 8 and 19. Screw 2 on the left
1 and 22 are driven by a motor 27 on the left side, and in addition to this, screws 21 and 22 on the right side are driven independently by a motor 27 on the right side. The blades 23 of the screw 21 on the screw center axis 18 and the blades 24 of the screw 22 on the screw center axis 19 are twisted in opposite directions,
Furthermore, the blades 23 of the screw 21 are twisted in opposite directions on the left and right sides of the center. The direction of these twists is such that when the upper sides of the screw 21 and the screw 22 are rotated in a forward direction, and the upper sides of the screw 21 and the screw 22 are rotated in a forward direction, the garbage that falls in the center during forward rotation is distributed and transferred to the left and right. It is designed to be discharged from the exit on the right side. Support shafts 40 and 41 are protruded from one of the left and right sides and rotatably inserted into the other shaft so that the left and right parts of the screws 21 and 22 can rotate relative to each other. Since the screw center shaft 19 does not move in the direction perpendicular to the axis as will be described later, the left and right screws 22 may be supported by bearings in the center so that they can rotate relative to each other. The pitch of the blades 23 and 24 of the screws 21 and 22 is at the entrance 16.
The pitch near exit 17 is larger than the pitches nearby. In addition, at the ends of the screw which is twisted in the opposite direction at approximately the center, the outer diameter is gradually increased so as not to attract dust. Screw 22 of one screw center shaft 19
is supported by bearings 25 and 26 at a fixed position relative to the conveyor case 20, and is directly rotated by a motor 27. Screw 22 during normal operation
rotates in a normal counterclockwise direction when viewed from the motor 27 side, and the screw 21 rotates in a normal clockwise direction. Two hoppers and two screws may be provided to form two lines. Screw 21 of the other screw center shaft 18
As shown in FIGS. 3 and 4, the cylinder 28,
29 and is supported by moving bearings 31 and 32 that move along a guide rail 30. Since the cylinders 28 and 29 are configured to be displaced by the same distance as described below, the screw 21 moves parallel to the screw 22, and the center distance adjustment is performed from _l1 to _l2. It is becoming more and more popular. The shaft ends of the screws 21 and 22 on the motor 27 side are connected to links 33 and 3 as shown in FIGS.
4 and gears 35, 36, 37, and 38, the screw 21 continues to be driven and rotated in the opposite direction to the screw 22 even while the distance between the shafts is changing from l ₁ to l ₂ . ing. If dirt gets caught between the screws 21 and 22, the dirt will cause the screws 21 and 22 to
is subjected to an expanding force that increases the distance between their axes, so if this expanding force is large, it will cause damage to the screws 21, 22 and other parts.
These problems must be prevented. In order to meet these requirements, the distance between the axes is adjusted as shown in FIGS. 7a and 7b. That is, assuming that the distance between the shafts is the minimum distance between the shafts l ₁ and the maximum distance between the shafts during steady state l ₂ , the dust 39 caught between the screws 21 and 22
The expansion force generated by this is detected as the oil pressure of the cylinders 28 and 29. For example, as will be described later, an allowable enlarging force is set as an allowable value of the enlarging force in a hydraulic circuit. During normal operation, crushing and bag tearing are performed at the minimum distance _l1 between the centers as shown in FIG. 7a. big garbage 39
Or, if a lump of incombustible material enters and the expanding force exceeds the allowable expanding force, the distance between the axes will open until the expanding force falls to the allowable expanding force in the range of l ₁ to _{l 2} . Even when the bag is being opened, the screws 21 and 22 continue to rotate in the normal direction, and destruction, bag tearing, and transfer are continuously performed. FIG. 8 shows an example of a hydraulic circuit for adjusting the distance between the shafts as described above. Next, the incinerator 6 will be explained. As shown in FIG. 9, two sets of air dispersion plates 8 for fluidization are installed side by side on the left and right at the bottom of the incinerator 6. It is formed in a chevron-shaped cross section (roof-like) that is almost symmetrical with respect to the line. The inclination may be different between the center portion and both side edge portions. Incombustible material discharge ports 4 on both side edges
2 are connected to each other, and since the incombustible material discharge port 42 located at the center of the furnace can be shared at one location, three locations can be provided for the entire width of the furnace. The fluidized air sent from the blower 7 is sent to the air chamber 4.
The mass velocity (Kg/m ² /sec) of the fluidized air is ejected upward from each dispersion plate 8 via air chambers 43 and 45 on both side edges. is large enough to form a fluidized bed, but the mass velocity of the fluidized air jetting out of the central air chamber 44 is chosen to be smaller than the former. For example, the mass velocity of the fluidized air ejected from the air chambers 43 and 45 is 4 to 20 Gmf, preferably 5 to 20 Gmf.
10 Gmf, whereas the mass velocity of the fluidized air ejected from the air chamber 44 is selected to be 0.5 to 3 Gmf, preferably 1 to 2.5 Gmf. Here, 1 Gmf is the fluidization starting mass velocity. The number of air chambers is chosen arbitrarily for each distribution plate 8, and even in the case of a large number, the mass velocity of the fluidized air is
Make the one closest to the center smaller, and the one closer to the edges on both sides larger. Also, the air chambers 43, 4 on the side edge of the distribution plate 8 on the furnace wall side
3 and directly above the air chambers 45, 45 on the furnace center side,
A sloped wall 9 is provided as a reflective wall that blocks the upward flow path of the fluidized air and reflects and diverts the fluidized air toward the center of the furnace. Sloped surface 46 with opposite slope
are provided to prevent the flow medium from accumulating. In addition, the inclined wall 9 on the furnace center side is bridged in the furnace as a beam with a hollow cross section as shown in the illustrated example so that it can be used as a reflecting wall on the left and right dispersion plates 8 at the same time, and its upper side also has inclined surfaces on the left and right. 46 is formed to prevent accumulation of fluid media. The inclined wall 9 may be a wall body made of a metal pipe, and water may be passed through the pipe to generate steam or to produce hot water. The inclination of the dispersion plate 8 is preferably about 5 to 15 degrees, and the inclination of the inclined wall 9 is preferably about 10 to 60 degrees with respect to the horizontal. Furthermore, two raw material input ports 48 connected to the outlet 17 of the dust supply device 5 are arranged in the furnace ceiling 47 so as to correspond to the right and left central air chambers 44, respectively.
There are one or more locations. Next, to explain the function of the incinerator 6, the blower 7 sends fluidized air into the air chamber 43,
The air is ejected from the air chamber 45 at a high mass velocity, and from the air chamber 44 at a small mass velocity. In a normal fluidized bed, the fluidized medium violently moves up and down like boiling water to form a fluidized state, but the fluidized medium above the air chamber 44 does not move violently up and down, but has a weak flow. form a moving layer in the state. The width of this moving layer is narrow at the top, but it widens slightly at the bottom due to the effect of the slope of the dispersion plate 8.
45, it receives a jet of air with a large mass velocity and is blown up. Since some of the fluid medium at the skirt is removed, the layer directly above the air chamber 44 will fall under its own weight. A fluidized medium from a fluidized bed with a swirling flow 10 is replenished and deposited above this layer as will be described later. By repeating this process, the fluidized medium above the air chamber 44 almost comes together in a certain region, forming a downwardly moving layer that gradually descends. The fluidized medium that has moved onto the air chambers 43 and 45 is blown upward, but it hits the inclined wall 9 and is reflected and turned upwards toward the center of the thermal reaction area surrounded by the inclined wall 9, causing a rapid increase in the cross section inside the furnace. As a result, the air loses its rising speed, falls to the top of the downwardly moving layer, gradually descends, reaches the bottom, and is blown up again to circulate. A portion of the fluidized medium circulates in the fluidized bed as a swirling flow 10. The waste input into the incinerator 6 in this state from the raw material input port 48 descends to the top of the downwardly moving layer on each distribution plate 8. Near the top, the flow of the fluid medium flows in a concentrated direction from the outside toward the center, so that the debris is caught up in this flow and sucked into the top of the downwardly moving bed. Therefore, even light materials such as paper can be reliably taken into the descending moving bed, so that the paper burns on the sand and burns without contributing significantly to the heating of the fluidized medium, as in conventional fluidized beds. This can be prevented and the fluidized medium can be reliably heated by combustion in the descending moving bed and the swirling flow 10. In the descending moving bed, thermal decomposition occurs partially and combustible gas is generated.The generated combustible gas spreads horizontally and enters the fluidized bed where it is combusted, so the heat is effective for heating the fluidized medium. useful for. When heavy and large objects such as bottles and irons are dropped onto the surface of the downwardly moving layer, these objects do not fall instantly to the top of the air chamber 44, but are supported by the downwardly moving layer. As the fluid medium flows, it gradually spreads left and right and descends. Therefore, even if the combustible material is quite large, it will dry, gasify, and burn as it gradually descends and diffuses in the descending moving layer, and by the time it reaches the bottom, most of it will be burned and fragmented. Therefore, the formation of a fluidized bed is not inhibited. Therefore, even if the garbage is not crushed in advance using a crusher, it is sufficient to break the bags using the dust supply device 5.
The crusher and crushing process can be omitted, resulting in a compact device. In addition, since the waste thrown into the descending moving bed is quickly diffused into the fluidized medium, the combustion efficiency is increased. The non-combustible materials supplied through the dust supply device 5 are
First, it moves downward and laterally through each descending layer, but at this time, combustible materials that adhere to non-combustible materials or are assembled together (for example, the covering of electric wires) are burned.
Non-combustible materials that have reached the hem are transported by horizontal movement of the fluid medium and distributed by the dispersion plate 8.
The incombustible materials reach each incombustible material discharge port 42 due to the slope of the incombustible material and are smoothly discharged. Also, looking at the hearth module,
If we calculate the hearth module for a 1000t/d furnace, the hearth area = ^92.6m2 , whereas in the conventional example it is approximately 4m (hearth width) x 23.2m (hearth length) as mentioned above. (Fig. 12), as shown in Fig. 10, the furnace has a well-balanced shape of approximately 8 m (hearth width) x 11.6 m (heart length), making it easy to construct an ultra-large furnace of approximately 1000 t/d. It can be made possible. By the way, in the case of a fluidized bed furnace, the fluidized medium is generally cooled by fluidized air, so in order to maintain the fluidized medium temperature, a certain amount of fuel (waste) must be burned in the fluidized medium. . Therefore,
When continuously incinerating waste with a low calorific value below the self-combustion limit of 800 to 900 Kcal/Kg during summer, etc., it is necessary to supply more than a certain amount of waste (fuel) to maintain the temperature of the fluid medium. , high-load operation will be performed. On the other hand, when the calorific value of waste is large, such as in winter, it is necessary to continue operating at a low load. However, the incinerator 6 of the embodiment of the present invention described above
Since the waste can be evenly distributed throughout the furnace, the entire area of the hearth is effectively utilized, allowing for higher load operation (for example, about 30% more) than a conventional fluidized bed incinerator that does not have a swirling flow type. At the same time, part-load operation is also possible. That is, in the above-mentioned incinerator 6, forced air blowers 7 for supplying fluidized air below the dispersion plate 8 of each reaction section are separately installed corresponding to each reaction section (Fig. 1, 9). figure). When performing partial load operation, for example, when the amount of waste is small, only the reaction section on the left side of the ninth example is operated, and if the reaction section on the right side is stopped, the left side is a fluidized bed (corresponding to that section). forced air blower operation),
The right side is a stationary layer (the forced air blower corresponding to that part is stopped), and 1/2 is due to the action of only the reaction part on the left side.
Load operation is performed. Partial load operation is performed, for example, as follows. In the dust supply device 5 shown in Fig. 2, if the left dust supply device is A and the right dust supply device is B, (1) At 100% load A, B forward rotation 50% each from the left and right outlets 17 Discharge (2) At 50% load (i) When only the left thermal reaction section is operating A: Forward rotation B: Reverse rotation 50% discharge from the left outlet 17 No discharge from the right outlet 17 (ii) When only the right thermal reaction section is operating A Reverse rotation B Forward rotation The operation is such that 50% is discharged from the right outlet 17 without discharging from the left outlet 17. Regarding the operation of the incombustible material discharge device 12 shown in FIG. 9, if the left side is C, the center is D, and the right side is E, the extraction capacity (per unit time) ratio is C:D:E=1:1: 1 However, since the following intermittent operation is performed, the ratio of the total amount taken out over a long period of time is C:D:E=1:2:1. (1) At 100% load For example, C, D operation (30 seconds) → C, D rest (15 seconds)
seconds) → D, E operation (30 seconds) → D, E pause (15
(seconds) → (repeat) (2) At 50% load (i) When operating the left thermal reaction section For example, C (30 seconds), D (60 seconds) operation → C (60 seconds)
seconds), D (30 seconds) pause →... (repeat)... (ii) When operating the right thermal reaction section For example, D (60 seconds), E (30 seconds) operation → D (30 seconds)
(seconds), E (60 seconds) pause →...(repeat)... As described above, there are the following problems in the 50% partial load operation in which only one side of the thermal reaction section is operated by operating the dust supply device 5 and the incombustible material discharge device. For example, when the left thermal reaction section is in operation and the right thermal reaction section is inactive, (a) a fluidized bed is formed on the left side, but a stationary bed is formed on the right side because the forced air blower 7 (G in FIG. 9) is stopped. However, when the incombustible material discharge device 12D is operated, the sand in the right stationary layer is also removed and discharged. (b) Sand scattered from the fluidized bed on the left is deposited in the stationary bed on the right. (c) If the stationary layer on the right side is left stationary for a long time, the temperature of the sand will gradually drop, and if it falls below 500℃, auxiliary combustion with oil will be required at the next start. To address these problems, control as shown in FIG. 13 is performed. Regarding (b), the fluidized medium is scattered from the left fluidized bed and deposited in the right stationary bed, and the left fluidized bed pressure decreases. This pressure is detected by the pressure controller H, and when it falls below a predetermined lower limit pressure PL (generally about 1800 mmAe), the forced air blower 7 (G in Fig. 9) corresponding to the right stationary layer is operated. The fluid medium has an angle of repose of almost zero and exhibits water-like flow characteristics, alternating with the left side. At this time, since even a small amount of airflow from the forced air blower 7, G on the right side is effective, the airflow amount is reduced to about 1/3 using a damper in advance. Thus, when the left fluidized bed pressure recovers to the lower limit pressure P _L or more, the right side forced air blower 7G is stopped. For (a), the central incombustible material discharge device 1
When operating 2.D, not only the fluidized medium in the left fluidized bed but also the fluidized medium in the right stationary bed is discharged. However, when the fluidized medium in the right stationary bed becomes lower than the lower surface of the central inclined wall 9, the fluidized medium in the left fluidized bed is ejected, so that the fluidized medium does not become lower than that. However, the discharged fluidized medium is recovered and replenished to the left fluidized bed side. Therefore, the fluidized medium in the left-hand fluidized bed is blocked by the inclined wall at the center of the furnace, and a more than necessary amount accumulates on the left-hand side, increasing the pressure in the left-hand fluidized bed. This pressure is detected by the pressure controller H, and a predetermined upper limit pressure P _H (generally about 2300 mmAq) is set.
When the temperature exceeds that level, the forced air blower 7, G on the right stationary layer is operated. When the left side fluidized bed pressure is restored to below the upper limit pressure P _H by exchanging the fluidized medium, the right side forced air blower is stopped. Furthermore, regarding (c), if the right stationary layer remains stationary for a long period of time, the temperature of the fluidized medium will gradually decrease, and when it reaches the lower limit, for example 500℃, auxiliary fuel will be required at the next start. Become. Therefore, the temperature of the stationary layer on the right side is detected by the temperature controller L, and when the temperature falls below the lower limit temperature T _L (for example, 500°C), the forced air blower 7, G on the right side is operated, and the temperature reaches the lower limit temperature T. When the air pressure has recovered to _L or above, the forced air blower 7 and G on the right side are stopped. In the case of the above control, the forced air blowers 7 and F on the left side continue to operate. 50% due to only the thermal reaction part on the right side
The above control also applies to load operation. Incidentally, sand is generally used as the fluidizing medium, and according to experiments, the angle of repose becomes zero when the mass velocity of the fluidizing air from below is 1 Gmf or more. Therefore, when a small amount of forced air is introduced into the stationary layer on the right side, the sand on the right side also exhibits water-like flow characteristics.
Sand is exchanged alternately with sand in the left fluidized bed. From this, the forced air blower 7, G on the right stationary layer can be throttled in advance to about 1/3 of the air volume using a damper. Furthermore, the amount of electricity used by ventilation equipment is as follows. Generally, the ventilation equipment of a fluidized bed furnace uses an induced blower for exhaust gas and a forced blower for supplying fluidized air.The induced blower has a shaft power that is approximately the cube of the air volume by controlling the rotation speed. However, in the case of a forced air blower, the resistance of the fluid medium does not change (does not decrease) even if the air volume is reduced, so the effect of controlling the rotation speed is very small. However, as in the embodiment of the present invention described above, for 1/2 load operation, two forced air blowers are installed in the fluidized bed furnace, one for each thermal reaction section, and one fan is installed depending on the load. By stopping the ventilation system and controlling the rotational speed of the induced fan, it is possible to reduce the power consumption of the ventilation equipment, which makes up the majority of the equipment, to less than half, greatly contributing to energy savings. It is something. Compared to conventional fluidized bed incinerators that do not use a swirling flow system, the incinerator shown in the above example makes more effective use of the entire area of the hearth, so it can handle up to a high load of about 130%, and at the same time By limiting the operation of the furnace to one side, it can cope with loads as low as 50%, and eventually can easily and reliably cope with a load range of 50-130%. Further, the present embodiment can easily respond to a wide load range of 50 to 130% by selecting the operating state according to the load as shown in Table 1, for example.

[Table] [Effects of the invention] As described above, according to the present invention, municipal waste,
In incinerators or pyrolysis furnaces that efficiently burn all kinds of materials to be combusted, such as sludge and coal, it is possible to increase the size of the furnace, which was previously considered impossible, and it is energy-saving and allows partial load operation. This has an extremely beneficial effect in that it can be carried out in many different ways.

[Brief explanation of drawings]

The drawings show an embodiment of the present invention, and FIG. 1 is a cross-sectional front view of a waste incinerator, FIG. 2 is a vertical cross-sectional front view of a dust supply device, FIG. 3 is a plan view of the dust supply device, and FIG. 4 is a front view of a dust supply device. Figure 2 is a - line arrow view, Figure 5 is a - line view in Figure 2.
A line sectional view, FIG. 6 is a diagram at another point in time, FIGS. 7a and b are cross-sectional views of the screw in different steps, FIG. 8 is a hydraulic circuit diagram, and FIG. 9 is a longitudinal sectional view of the incinerator. FIGS. 10a and 10b are a plan view and a side view of the hearth module of the present invention, FIG. 11 is an explanatory diagram of the flow state in the furnace, and FIGS. 12a and b are a plan view and a side view of a conventional hearth module. , FIG. 13 is a flowchart of an example of control. 1...garbage pit, 2...crane, 3...bucket, 4...hopper, 5...dust supply device, 6...
...Incinerator, 7...Blower, 8...Dispersion plate, 9...
Inclined wall, 10...Swirling flow, 11...Combustion exhaust gas duct, 12...Incombustibles discharge device, 13...Vibration sieve, 14...Conveyor, 15...Elevator, 1
6... Inlet, 17... Outlet, 18, 19... Screw center axis, 20... Conveyor case, 21,
22... Screw, 23, 24... Feather, 2
5, 26... Bearing, 27... Motor, 28, 29
...Cylinder, 30...Guide rail, 31,3
2...Moving bearing, 33, 34...Link, 35,
36, 37, 38...gear, 39...garbage, 4
0,41...Spindle, 42...Incombustible material discharge port, 4
3, 44, 45...Air chamber, 46...Slanted surface, 4
7... Ceiling section, 48... Raw material input port.

Claims (1)

[Scope of Claims] 1. A fluidizing dispersion plate is provided, and the dispersion plate has both side edges lower than the center part and is formed in a chevron-shaped cross section that is substantially symmetrical with respect to the center line, and the dispersion plate is formed to have a chevron-shaped cross section that is substantially symmetrical with respect to the center line, and the fluidizing gas at the both side edges is lower than the center. Fluidized bed thermal reaction parts whose mass velocity is higher than the fluidized gas mass velocity in the central part are arranged in parallel at the bottom of the same furnace almost symmetrically with respect to the furnace center line,
A common incombustible material discharge port is provided between each of the distribution plates, and a noncombustible material discharge port is provided at each outer side edge, and fluidizing gas is provided directly above the furnace wall side and the furnace center side of the side edge of each distribution plate. The fluidized bed thermal reaction system is equipped with a reflecting wall that reflects and diverts the upward flow toward the center of each fluidized bed thermal reaction section, and a raw material inlet is provided in the ceiling of the furnace so as to correspond to the center of each distribution plate. In the furnace, each of the raw material input ports is provided with a separately driven dust supply device, and a forced air blower for feeding fluidizing gas below the dispersion plate of each reaction section is associated with each thermal reaction section. A fluidized bed thermal reactor characterized by each being installed separately. 2 A dispersion plate for fluidization is provided, and the dispersion plate has both side edges lower than the center and formed in a chevron-shaped cross section that is substantially symmetrical with respect to the center line, and the fluidizing gas mass velocity at the both side edges is lower than the center. A fluidized bed thermal reaction section with a fluidization gas mass velocity larger than that of
A common incombustible material discharge port is provided between each of the distribution plates, and a noncombustible material discharge port is provided at each outer side edge, and fluidizing gas is provided directly above the furnace wall side and the furnace center side of the side edge of each distribution plate. Each of the fluidized bed thermal reaction sections is provided with a reflecting wall that reflects and diverts the upward flow toward the center of each fluidized bed thermal reaction section, and a raw material inlet is provided in the ceiling of the furnace so as to correspond to the center of each of the distribution plates. for,
A fluidized bed thermal reactor in which a dust supply device that is driven separately is provided, and a forced blower for feeding fluidizing gas below the dispersion plate of each reaction section is installed separately corresponding to each thermal reaction section. During partial load operation in which only one reaction section and dust supply device are operated, when the fluidized bed pressure in that reaction section is out of the specified range, or the fluidized bed temperature in the other idle reaction section falls below the specified temperature. 1. A method for operating a fluidized bed thermal reactor, comprising operating a forced air blower in a dormant reaction section when the reaction is stopped.