JP2014112020A - Fluid bed drier - Google Patents

Abstract

PROBLEM TO BE SOLVED: To improve drying efficiency by enhancing heat transfer efficiency to wet fuel, in a fluid bed drier.SOLUTION: The fluid bed drier comprises: a hollow drying vessel 101 which can input raw coal from a raw coal input port 102 at one side, and can discharge dried coal which is obtained by heat-drying the raw coal from a dried coal discharge port 103 at the other end; a fluidized gas supply part 104 which makes the raw coal flow and dries it by supplying a fluidized gas to the drying vessel 101; descending fluid chambers 106a, 106b, 106c, 106d and 106e which descend the raw coal; and ascending fluid chambers 107a, 107b, 107c and 107d which ascend the raw coal by using a fluidized gas succeeding the descending fluid chambers 106.

Description

  The present invention relates to a fluidized bed drying apparatus for drying a material to be dried by fluidizing gas.

  For example, a combined coal gasification power generation facility is a power generation facility that aims to further increase the efficiency and environmental performance compared to conventional coal-fired power generation by gasifying coal and combining it with combined cycle power generation. This coal gasification combined cycle power generation facility has a great merit that it can use coal with abundant resources, and it is known that the merit can be further increased by expanding the applicable coal types.

  Conventional coal gasification combined power generation facilities generally have a coal supply device, a drying device, a coal gasification furnace, a gas purification device, a gas turbine facility, a steam turbine facility, an exhaust heat recovery boiler, a gas purification device, and the like. ing. Accordingly, the coal is dried and then pulverized and supplied to the coal gasifier as pulverized coal. And air is taken in and pulverized coal is combusted and gasified and gasified gas (combustible gas) is generated. The gasified gas is refined and then supplied to the gas turbine equipment, and high-temperature and high-pressure combustion gas is generated to drive the turbine. As for the exhaust gas after driving the turbine, thermal energy is recovered by the exhaust heat recovery boiler. Then, steam is generated and supplied to the steam turbine equipment, and the turbine is driven to generate power. On the other hand, the exhaust gas from which the thermal energy has been recovered is released into the atmosphere through a chimney after harmful substances are removed by the gas purification device.

  By the way, the coal used in such a coal gasification combined power generation facility is not only a high-grade coal (high-grade coal) having a high calorific value such as bituminous coal and anthracite, but also a comparison such as sub-bituminous coal and lignite. There is a low-grade coal (low-grade coal) with a low calorific value. Moreover, biomass etc. may be used instead of coal as a fuel. Since this low-grade coal and biomass contain a large amount of water, the power generation efficiency decreases due to this water. Therefore, when using such a wet fuel, it is necessary to dry the fuel by the above-described drying device to remove moisture.

  As a drying apparatus for drying such fuel, there is one described in Patent Document 1 below. The fluidized bed drying apparatus and the fluidized bed drying facility described in Patent Document 1 are for supplying a fluidized gas to a drying chamber to flow and dry the material to be dried supplied to the drying chamber. A crusher that crushes the dried product to a predetermined particle size, a first fluidization chamber that feeds the material to be dried that has been crushed by dividing the inside of the fluidized bed drying device with a partition wall, and starts fluidization and drying; The second flow chamber where the fine particles flowed and dried in the chamber overflow and flow and dry, and the conveyance line that conveys coarse particles discharged from the first flow chamber to the crusher side are provided. is there.

JP 2011-214817 A

  Fuels such as low-grade coal and biomass have a high moisture content and a large variation in the moisture content. When drying such fuel, it is important to increase the heat transfer efficiency. In the conventional fluidized bed drying apparatus described above, a first fluidizing chamber for fluidizing and drying the material to be dried and a second fluidizing chamber for further fluidizing and drying the fine particles fluidized and dried in the first fluidizing chamber. While providing, the coarse particle paid out from the 1st fluidization chamber is conveyed to a crusher, and is crushed again, and favorable drying is enabled. However, taking such a configuration may increase the size of the apparatus and reduce the economic efficiency.

  The present invention solves the above-described problems, and an object of the present invention is to provide a fluidized bed drying apparatus that can improve the drying efficiency by increasing the heat transfer efficiency to the wet fuel.

  In order to achieve the above object, the fluidized bed drying apparatus of the present invention is capable of supplying wet fuel from a charging portion on one end side and discharging a dried product obtained by heating and drying the wet fuel from a discharging portion on the other end side. A hollow container having a hollow shape, a fluidizing gas supply unit for flowing and drying the wet fuel by supplying a fluidizing gas to the drying container, a descending flow chamber for lowering the wet fuel, and the descending type And an ascending fluid chamber in which the wet fuel is raised by the fluidizing gas continuously in the fluid chamber.

  Therefore, by providing a descending flow chamber for lowering the wet fuel and an ascending flow chamber for raising the wet fuel by the fluidizing gas in the descending flow chamber, the wet fuel is separated from the lower flow chamber and the ascending type. It is heated and dried by the fluidizing gas while repeatedly moving up and down the fluid chamber. As a result, a long flow path can be secured without increasing the volume of the drying container, the residence time of the wet fuel in the drying container can be lengthened, the heat transfer efficiency to the wet fuel can be improved, and the drying efficiency can be improved. it can.

  In the fluidized bed drying apparatus of the present invention, a plurality of the descending flow chambers and the ascending fluid chambers are arranged alternately in series in the horizontal direction, and a lower part of the descending fluid chamber and a lower part of the ascending fluid chamber And a lower communication part, and an upper communication part in which the upper part of the ascending flow chamber and the upper part of the descending flow chamber communicate with each other.

  Therefore, the wet fuel that has descended the descending flow chamber passes through the lower communicating portion and moves to the ascending fluid chamber and rises, and the wet fuel that has ascended the ascending fluid chamber descends through the upper communicating portion. Therefore, the wet fuel can be appropriately moved between the descending flow chamber and the ascending flow chamber, and the wet fuel can be efficiently dried.

  In the fluidized bed drying apparatus of the present invention, the fluidizing gas supply unit supplies the fluidizing gas to at least the lower part of the ascending fluid chamber.

  Therefore, by supplying the fluidizing gas from the fluidizing gas supply unit to the lower part of the ascending fluid chamber, the wet fuel in the ascending fluid chamber can be heated and dried while being appropriately raised.

  In the fluidized bed drying apparatus of the present invention, the fluidizing gas supply unit can supply fluidizing gas to the lower part of the descending fluid chamber and the ascending fluid chamber, and the superficial velocity of the ascending fluid chamber is It is characterized by being set higher than the superficial velocity of the descending flow chamber.

  Therefore, by setting the superficial velocity of the ascending fluid chamber higher than the superficial velocity of the descending fluid chamber, the wet fuel can properly ascend the ascending fluid chamber and make the descending fluid chamber appropriate. Can descend.

  The fluidized bed drying apparatus of the present invention is characterized in that the pressure in the ascending fluid chamber is set lower than the pressure in the descending fluid chamber.

  Accordingly, by setting the pressure in the ascending flow chamber to be lower than the pressure in the descending flow chamber, the wet fuel in the ascending flow chamber can appropriately rise in the low pressure space, and the wet fuel in the descending flow chamber Can efficiently move down to the ascending flow chamber of the adjacent low pressure space by properly descending the high pressure space.

  The fluidized bed drying apparatus of the present invention is characterized in that a pressure adjusting device is provided above the ascending flow chamber.

  Accordingly, the fluidizing gas is supplied to the drying container by the fluidizing gas supply unit, so that the descending fluid chamber is set as a high-pressure space, but the pressure of the ascending fluid chamber is adjusted by the pressure regulator. Therefore, it can be set to an appropriate low pressure space.

  In the fluidized bed drying apparatus of the present invention, the drying container is provided with a dispersion plate having a plurality of openings at a predetermined distance from a bottom plate at a lower portion thereof, thereby dividing a wind box, and the fluidizing gas supply unit includes Fluidizing gas can be supplied to the lower part of the ascending flow chamber and the descending flow chamber via a wind box, and the aperture ratio of the dispersion plate corresponding to the ascending flow chamber corresponds to the descending flow chamber. It is characterized by being set higher than the aperture ratio of the dispersion plate.

  Therefore, by setting the aperture ratio of the dispersion plate corresponding to the ascending flow chamber higher than the aperture ratio of the dispersion plate corresponding to the descending flow chamber, the superficial velocity of the ascending flow chamber is increased. It becomes higher than the tower speed, so that the wet fuel can be properly raised in the ascending flow chamber, and the wet fuel can be properly lowered in the descending flow chamber.

  In the fluidized bed drying apparatus of the present invention, the drying container is provided with a dispersion plate having a plurality of openings at a predetermined distance from the bottom plate at the lower portion thereof, thereby corresponding to the ascending flow chamber and the descending flow chamber, respectively. An air box is defined, and the fluidizing gas supply unit can supply fluidizing gas to the lower part of the ascending fluid chamber and the descending fluid chamber via the air box, and corresponds to the ascending fluid chamber. The supply amount of the fluidizing gas to the wind box is set to be larger than the supply amount of the fluidizing gas to the wind box corresponding to the descending flow chamber.

  Therefore, by setting the supply amount of the fluidizing gas to the wind box corresponding to the ascending flow chamber more than the supply amount of the fluidizing gas to the wind box corresponding to the descending flow chamber, the empty flow chamber is empty. The tower speed becomes higher than the superficial speed of the descending flow chamber, so that the wet fuel can be appropriately raised in the ascending flow chamber, and the wet fuel can be properly lowered in the descending flow chamber.

  In the fluidized bed drying apparatus of the present invention, the bottom surface of the descending flow chamber is formed with an inclined surface that inclines downward toward the ascending fluid chamber.

  Therefore, the descending flow chamber is formed with an inclined surface, so that the wet fuel descending the descending flow chamber can appropriately move to the ascending flow chamber along the inclined surface. Fluidization can be promoted.

  In the fluidized bed drying apparatus of the present invention, the descending flow chamber and the ascending fluid chamber are alternately arranged in a honeycomb shape in the horizontal direction, and the upper part of the descending fluid chamber on the uppermost stream side is arranged above. An introduction part is provided, and the discharge part is provided in a lower part of the descending flow chamber on the most downstream side.

  Therefore, by ensuring a long flow path without increasing the volume of the drying container, the residence time of the wet fuel in the drying container can be extended, and the efficiency of heat transfer to the wet fuel can be improved to improve the drying efficiency. Can do.

  According to the fluidized bed drying apparatus of the present invention, the descending fluid chamber for lowering the wet fuel and the ascending fluid chamber for continuously raising the wet fuel by the fluidizing gas are provided in the descending fluid chamber. The heat transfer efficiency can be improved, the drying efficiency can be improved, the moisture content of the wet fuel can be reduced, and the variation in the moisture content can be suppressed.

FIG. 1 is a schematic diagram illustrating a fluidized bed drying apparatus according to Embodiment 1 of the present invention. 2 is a cross-sectional view taken along the line II-II of FIG. 3 is a cross-sectional view taken along the line III-III in FIG. 4 is a cross-sectional view taken along the line IV-IV in FIG. FIG. 5 is a schematic configuration diagram of a coal gasification combined power generation facility to which the fluidized bed drying apparatus of Example 1 is applied. FIG. 6A is a graph showing the weight concentration with respect to residence time of raw coal in a conventional fluidized bed drying apparatus. FIG. 6-2 is a graph showing the weight concentration with respect to the water content of raw coal in a conventional fluidized bed drying apparatus. 7-1 is a graph showing the weight concentration with respect to residence time of raw coal in the fluidized bed drying apparatus of Example 1. FIG. 7-2 is a graph showing the weight concentration with respect to the water content of raw coal in the fluidized bed drying apparatus of Example 1. FIG. FIG. 8 is a schematic diagram showing a fluidized bed drying apparatus according to Embodiment 2 of the present invention. FIG. 9 is a schematic diagram showing a fluidized bed drying apparatus according to Example 3 of the present invention. FIG. 10 is a schematic diagram showing a fluidized bed drying apparatus according to Example 4 of the present invention.

  Exemplary embodiments of a fluidized bed drying apparatus according to the present invention will be described below in detail with reference to the accompanying drawings. In addition, this invention is not limited by this Example, Moreover, when there exists multiple Example, what comprises combining each Example is also included.

  1 is a schematic view showing a fluidized bed drying apparatus according to Example 1 of the present invention, FIG. 2 is a sectional view taken along the line II-II of FIG. 1 showing the fluidized bed drying apparatus of Example 1, and FIG. 1 is a sectional view taken along the line III-III in FIG. 1, FIG. 4 is a sectional view taken along the line IV-IV in FIG. 1 representing the fluidized bed drying apparatus of Example 1, and FIG. It is a schematic block diagram of the coal gasification combined cycle facility to which the drying apparatus was applied.

  The coal gasification combined power generation facility (IGCC: Integrated Coal Gasification Combined Cycle) of Example 1 adopts an air combustion method in which gas is generated in a gasification furnace using air as an oxidant and is purified by a gas purification device. The gasified gas is supplied to the gas turbine equipment as fuel to generate electricity. That is, the coal gasification combined power generation facility of Example 1 is an air combustion type (air blowing) power generation facility. In this case, low-grade coal is used as the wet fuel supplied to the gasifier.

  In Example 1, as shown in FIG. 5, the coal gasification combined power generation facility 10 includes a coal supply device 11, a fluidized bed drying device 12, a pulverized coal machine (mill) 13, a coal gasification furnace 14, and a char recovery device 15. , A gas refining device 16, a gas turbine facility 17, a steam turbine facility 18, a generator 19, and a heat recovery steam generator (HRSG) 20.

  The coal feeder 11 includes a raw coal bunker 21, a coal feeder 22, and a mill 23. The raw coal bunker 21 can store low-grade coal, and can drop a predetermined amount of low-grade coal into the coal feeder 22. The coal feeder 22 can transport the low-grade coal dropped from the raw coal bunker 21 by a conveyor or the like and drop it on the mill 23. The mill 23 can crush the dropped low-grade coal into a predetermined size.

  The fluidized bed drying device 12 supplies the fluidized gas (for example, heated steam) to the low-grade coal introduced by the coal feeder 11 so that the low-grade coal is heated and dried while flowing. The moisture contained in the low-grade coal can be removed. Then, the dried low-grade coal taken out from the fluidized bed drying device 12 (hereinafter referred to as dry coal) is conveyed to the dry coal bunker 32 via the cooler 31. The gas discharged from the upper part of the fluidized bed drying device 12 is separated into gas and dry coal particles by the gas cyclone 33 and the electric dust collector 34, and the particles are stored in the dry coal bunker 32. The gas from which the dry coal is separated by the electric dust collector 34 is exhausted and then supplied to the economizer of the plant to recover latent heat.

  The pulverized coal machine 13 is a coal pulverizer, and the dry coal stored in the dry coal bunker 32 is input to the pulverized coal machine 13 by a coal feeder 36. The pulverized coal machine 13 is a coal pulverizer, and pulverizes dry coal into pulverized coal having a predetermined particle size or less. The pulverized coal after pulverization is separated from the carrier gas by the pulverized coal bag filters 37a and 37b and stored in the pulverized coal supply hoppers 38a and 38b.

  The coal gasification furnace 14 is supplied with the pulverized coal processed by the pulverized coal machine 13, and the char (unburned coal) recovered by the char recovery device 15 is returned to be recycled.

  That is, the coal gasification furnace 14 is connected to the compressed air supply line 41 from the gas turbine equipment 17 (compressor 61), and can supply compressed air compressed by the gas turbine equipment 17. The air separation device 42 separates and generates nitrogen and oxygen from air in the atmosphere. A first nitrogen supply line 43 is connected to the coal gasifier 14, and a pulverized coal supply hopper is connected to the first nitrogen supply line 43. Charging lines 44a and 44b from 38a and 38b are connected. The second nitrogen supply line 45 is also connected to the coal gasification furnace 14, and the char return line 46 from the char recovery device 15 is connected to the second nitrogen supply line 45. Further, the oxygen supply line 47 is connected to the compressed air supply line 41. In this case, nitrogen is used as a carrier gas for pulverized coal and char, and oxygen is used as an oxidizing agent.

  The coal gasification furnace 14 is, for example, a spouted bed type gasification furnace, which combusts and gasifies coal, char, air (oxygen) supplied therein or water vapor as a gasifying agent, and produces carbon dioxide. A combustible gas (product gas, coal gas) containing carbon as a main component is generated, and a gasification reaction takes place using this combustible gas as a gasifying agent. The coal gasification furnace 14 is provided with a foreign matter removing device 48 that removes foreign matter mixed with pulverized coal. In this case, the coal gasification furnace 14 is not limited to the spouted bed gasification furnace, and may be a fluidized bed gasification furnace or a fixed bed gasification furnace. The coal gasification furnace 14 is provided with a gas generation line 49 for combustible gas toward the char recovery device 15, and can discharge combustible gas containing char. In this case, by providing a gas cooler (not shown) in the gas generation line 49, the combustible gas may be cooled to a predetermined temperature and then supplied to the char recovery device 15.

  The char recovery device 15 includes a dust collector 51 and a supply hopper 52. In this case, the dust collector 51 is constituted by one or a plurality of bag filters or cyclones, and can separate char contained in the combustible gas generated in the coal gasification furnace 14. The combustible gas from which the char has been separated is sent to the gas purification device 16 through the gas discharge line 53. The supply hopper 52 stores the char separated from the combustible gas by the dust collector 51. A bin may be disposed between the dust collector 51 and the supply hopper 52, and a plurality of supply hoppers 52 may be connected to the bin. A char return line 46 from the supply hopper 52 is connected to the second nitrogen supply line 45.

The gas purification device 16 performs gas purification by removing impurities such as sulfur compounds and nitrogen compounds from the combustible gas from which the char has been separated by the char recovery device 15. The gas purifier 16 purifies the combustible gas to produce fuel gas and supplies it to the gas turbine equipment 17. In the gas purifier 16, since the combustible gas from which the char is separated still contains sulfur (H ₂ S), the sulfur is finally removed by removing it with the amine absorbent. Is recovered as gypsum and used effectively.

  The gas turbine equipment 17 includes a compressor 61, a combustor 62, and a turbine 63, and the compressor 61 and the turbine 63 are connected by a rotating shaft 64. The combustor 62 has a compressed air supply line 65 connected to the compressor 61, a fuel gas supply line 66 connected to the gas purifier 16, and a combustion gas supply line 67 connected to the turbine 63. Further, the gas turbine equipment 17 is provided with a compressed air supply line 41 extending from the compressor 61 to the coal gasification furnace 14, and a booster 68 is provided in the middle. Therefore, in the combustor 62, the compressed air supplied from the compressor 61 and the fuel gas supplied from the gas purifier 16 are mixed and burned, and the rotating shaft 64 is rotated by the generated combustion gas in the turbine 63. By doing so, the generator 19 can be driven.

  The steam turbine facility 18 includes a turbine 69 that is coupled to the rotating shaft 64 in the gas turbine facility 17, and the generator 19 is coupled to the base end portion of the rotating shaft 64. The exhaust heat recovery boiler 20 is provided in the exhaust gas line 70 from the gas turbine equipment 17 (the turbine 63), and generates steam by exchanging heat between the air and the high temperature exhaust gas. Therefore, the exhaust heat recovery boiler 20 is provided with the steam supply line 71 between the steam turbine equipment 18 and the turbine 69 of the steam turbine equipment 18, the steam recovery line 72 is provided, and the steam recovery line 72 is provided with the condenser 73. Yes. Therefore, in the steam turbine facility 18, the turbine 69 is driven by the steam supplied from the exhaust heat recovery boiler 20, and the generator 19 can be driven by rotating the rotating shaft 64.

  The exhaust gas from which heat has been recovered by the exhaust heat recovery boiler 20 is freed of harmful substances by the gas purification device 74, and the purified exhaust gas is discharged from the chimney 75 to the atmosphere.

  Hereinafter, the fluidized bed drying apparatus 12 in the coal gasification combined power generation facility 10 described above will be described in detail.

  As shown in FIGS. 1 to 4, the fluidized bed drying device 12 includes a drying container 101, a raw coal charging port (charging unit) 102, a dry coal discharging port (discharging unit) 103, and a fluidizing gas supply unit 104. And a gas discharge port 105.

  The drying container 101 has a hollow box shape, and includes a descending flow chamber 106 that lowers the raw coal therein, and an ascending flow chamber 107 that raises the raw coal with fluidized gas (for example, fluidized steam). Are arranged in series alternately in the horizontal direction. Specifically, descending flow chambers 106 (106a, 106b, 106c, 106d, 106e) and ascending flow chambers 107 (107a, 107b, 107c, 107d) are alternately arranged in a honeycomb shape in the horizontal direction. Are arranged. In this embodiment, the descending flow chamber 106 includes five descending flow chambers 106a, 106b, 106c, 106d, and 106e, and the ascending fluid chamber 107 includes four ascending fluid chambers 107a, 107b, 107c, 107d.

  In the drying container 101, a raw coal charging port 102 for charging raw coal is formed at the upper part of the side wall of the first descending flow chamber 106a on one end side, and the side wall of the fifth descending flow chamber 106e on the other end side is formed. A dry charcoal discharge port 103 for discharging a dried product obtained by heating and drying raw coal is formed in the lower part. In this case, the raw coal input port 102 and the dry coal discharge port 103 are provided one by one at the end of the drying container 101, but a plurality of them may be provided. In addition, the drying container 101 can adjust the amount of raw coal supplied from the raw coal inlet 102 to the inside by a coal feeder 22 (see FIG. 5). Moreover, the dry container 101 can adjust raw coal discharge | emission amount by adjusting the rotation speed of the rotary valve which is not shown in the dry charcoal discharge port 103 provided.

  In addition, the drying container 101 is provided with a dispersion plate 108 having a plurality of openings at a predetermined distance from the bottom plate 101a in the lower portion, so that an air box 109 is partitioned. The drying container 101 is provided with a fluidized gas supply unit 104 that supplies fluidized gas (heated steam) to the bottom plate 101a via the wind box 109 and above the dispersion plate 108. Further, in the drying container 101, a gas discharge port 105 for discharging the fluidized gas and the generated gas is formed in the ceiling plate 101b on the dry coal discharge port 103 side.

  In the drying container 101, raw coal is supplied from the raw coal inlet 102 to the descending flow chamber 106a. Further, the drying container 101 includes all the descending flow chambers 106a, 106b, 106c, 106d, 106e and the ascending fluid chambers 107a, 107b, the fluidizing gas from the fluidizing gas supply unit 104 through the wind box 109 and the dispersion plate 108. By being supplied to 107 c and 107 d, a fluidized bed is formed above the dispersion plate 108.

  In the drying container 101, descending flow chambers 106a, 106b, 106c, 106d, 106e and ascending flow chambers 107a, 107b, 107c, 107d are alternately arranged. In other words, the first descending flow chamber 106a is disposed at the corner of the drying vessel 101 and is provided with the raw coal charging port 102, and is adjacent to the first ascending flow chamber 107a and the second descending flow chamber 106b. Are arranged in a straight line. A second ascending flow chamber 107b is arranged in a direction bent at a right angle from the second descending flow chamber 106b, and adjacent to the second ascending flow chamber 107b, the third descending flow chamber 106c and the third ascending flow chamber 106b are arranged. The type flow chamber 107c is arranged in a straight line. Further, a fourth descending flow chamber 106d is disposed at a right angle from the third ascending flow chamber 107c, and the fourth ascending flow chamber 107d and the fifth descending type are adjacent to the fourth descending flow chamber 106d. The flow chamber 106e is arranged in a straight line, and the fifth descending flow chamber 106e is provided with a dry coal discharge port 103.

  The descending flow chambers 106a, 106b, 106c, 106d, and 106e and the ascending flow chambers 107a, 107b, 107c, and 107d that are alternately arranged communicate with each other at the upper part or the lower part. That is, as shown in FIGS. 2 to 4, the first descending flow chamber 106a and the first ascending fluid chamber 107a communicate with each other through the first lower communicating portion 110a, and the first ascending fluid chamber 107a and the first ascending fluid chamber 107a. The second descending flow chamber 106b communicates with the first upper communication portion 111a. The second descending flow chamber 106b and the second ascending fluid chamber 107b communicate with each other through the second lower communication portion 110b. The second ascending flow chamber 107b and the third descending flow chamber 106c communicate with each other through the second upper communication portion 111b. The third descending flow chamber 106c and the third ascending fluid chamber 107c communicate with each other through the third lower communication portion 110c. The third ascending flow chamber 107c and the fourth descending flow chamber 106d communicate with each other through the third upper communication portion 111c. The fourth descending flow chamber 106d and the fourth ascending fluid chamber 107d communicate with each other by the fourth lower communication portion 110d, and the fourth ascending fluid chamber 107d and the fifth descending fluid chamber 106e communicate with the fourth upper communicating chamber. The part 111d communicates.

  In this case, the descending flow chambers 106a, 106b, 106c, 106d, 106e and the ascending flow chambers 107a, 107b, 107c, 107d are set to have substantially the same floor area. An appropriate ratio may be set according to the water content.

  Further, the lower communication portions 110a, 110b, 110c, and 110d and the upper communication portions 111a, 111b, 111c, and 111d are set to have substantially the same opening area and are provided with no step. In this case, a step serving as a weir or an upwardly inclined surface is provided between each descending flow chamber 106a, 106b, 106c, 106d, 106e and each ascending fluid chamber 107a, 107b, 107c, 107d. The residence time of raw coal may be increased.

  Accordingly, the raw coal supplied to the first descending flow chamber 106a is heated and dried by descending while flowing with the fluidizing gas. The raw coal in the first descending flow chamber 106a moves to the first ascending fluid chamber 107a through the first lower communication portion 110a, and flows through the first ascending fluid chamber 107a with the fluidizing gas. To rise. Then, each descending flow chamber 106b, 106c, 106d, 106e and each ascending flow chamber 107b, 107c, 107d are dried while being alternately raised and lowered.

  Further, the drying container 101 is provided with a gas supply line 112 for supplying a fluidizing gas to each descending flow chamber 106a, 106b, 106c, 106d, 106e and each ascending fluid chamber 107a, 107b, 107c, 107d. ing. That is, the tip of the gas supply line 112 is connected to the fluidized gas supply unit 104 provided at the lower part of the wind box 109. Therefore, the fluidizing gas supplied from the gas supply line 112 to the wind box 109 through the fluidizing gas supply unit 104 passes through the dispersion plate 108 to the descending flow chambers 106a, 106b, 106c, 106d, 106e and the ascending fluid chambers. 107a, 107b, 107c and 107d are supplied almost evenly.

  At this time, in the drying container 101, the superficial velocity in each of the ascending flow chambers 107a, 107b, 107c, and 107d is set higher than the superficial velocity in each of the descending flow chambers 106a, 106b, 106c, 106d, and 106e. . Specifically, the pressures in the ascending flow chambers 107a, 107b, 107c, and 107d are set lower than the pressures in the descending flow chambers 106a, 106b, 106c, 106d, and 106e.

  The first descending flow chamber 106a and the upper communication portions 111a, 111b, 111c, and 111d are each provided with a pressure adjusting device on the upper surface (ceiling plate 101b). In this pressure adjusting device, opening-adjustable dampers 113a, 113b, 113c, 113d, and 113e are provided in the gas discharge portions 114a, 114b, 114c, 114d, and 114e, respectively. Therefore, the pressure setting of each of the flow chambers 106a, 106b, 106c, 106d, 106e, 107a, 107b, 107c, 107d is achieved by adjusting the opening by the opening adjustment type dampers 113a, 113b, 113c, 113d, 113e. Can be adjusted.

  Accordingly, in the high-pressure descending flow chambers 106a, 106b, 106c, 106d, and 106e, the raw coal is properly lowered, and the low-pressure ascending flow chambers 107a, 107b, 107d from the lower communication portions 110a, 110b, 110c, and 110d. 107c and 107d can be appropriately moved. Further, in the low pressure ascending flow chambers 107a, 107b, 107c, and 107d, the raw coal is appropriately raised by the fluidizing gas, and the high pressure descending flow chambers 106b and 106c are respectively supplied from the upper communication portions 111a, 111b, 111c, and 111d. , 106d, 106e can be appropriately moved.

  In addition, the drying container 101 has an exhaust chamber 115 formed in the upper part. The exhaust chamber 115 can collect the exhaust gas from the gas exhaust portions 114a, 114b, 114c, 114d, and 114e, and collectively discharge the gas from the gas exhaust port 105 for processing.

  In the first embodiment, the opening areas of the gas discharge portions 114a, 114b, 114c, 114d, and 114e are configured to be substantially the same, but by adjusting the opening degree of the dampers 113a, 113b, 113c, 113d, and 113e, The pressures of the descending flow chambers 106a, 106b, 106c, 106d, 106e and the ascending flow chambers 107a, 107b, 107c, 107d can be adjusted. Here, the opening degree of the damper 113a is set smaller than the opening degree of the other dampers 113b, 113c, 113d, 113e.

  Further, in the first embodiment, gas discharge portions 114a, 114b, 114c, 114d, and 114e and dampers 113a, 113b, 113c, and upper portions of the first descending flow chamber 106a and the upper communication portions 111a, 111b, 111c, and 111d, respectively. Although 113d and 113e are provided, they may be provided above the ascending flow chambers 107a, 107b, 107c, and 107d.

  Here, the whole operation | movement of the fluidized bed drying apparatus 12 of Example 1 is demonstrated.

  In the fluidized bed drying device 12, raw coal is supplied from the raw coal inlet 102 to the drying container 101, and fluidized gas is supplied from the fluidized gas supply unit 104 through the wind box 109 to the dispersion plate 108. Then, a fluidized bed is formed above the dispersion plate 108. The raw coal moves through the fluidized bed to the dry coal discharge port 103 side by the fluidizing gas, and is heated and dried by receiving heat from the fluidizing gas.

  That is, when raw coal is supplied from the raw coal inlet 102 to the first descending flow chamber 106a, the raw coal is heated and lowered while fluidizing the first descending flow chamber 106a by the fluidizing gas. The lowered raw coal moves from the first descending flow chamber 106a to the lower portion of the first ascending fluid chamber 107a through the lower communication portion 110a by the fluidizing gas. In this case, since the damper 113a provided at the upper part of the first ascending flow chamber 107a is open by a predetermined angle, the pressure of the first ascending flow chamber 107a is higher than the pressure of the first descending flow chamber 106a. Is low. Therefore, the flow rate of the fluidized gas flowing from the wind box 109 through the dispersion plate 108 to the first ascending flow chamber 107a is increased, and the superficial velocity of the first ascending flow chamber 107a is increased in the first descending flow chamber 106a. It is higher than the tower speed. As a result, the raw coal at the lower portion of the first descending flow chamber 106a is sucked to the first ascending flow chamber 107a side through the lower communication portion 110a, and the first ascending flow chamber 107a can be raised.

  The raw coal is heated and fluidized by the fluidizing gas while fluidizing the first ascending fluid chamber 107a. The rising raw coal moves from the first ascending flow chamber 107a to the second descending flow chamber 106b through the upper communication portion 111a by the fluidizing gas. In this case, since the raw coal moves from the second descending flow chamber 106b through the lower communication portion 110b to the second ascending fluid chamber 107b on the downstream side, the first ascending fluid chamber is generated. The raw coal that has moved up 107a can be sucked into the second descending flow chamber 106b through the upper communication portion 111a and appropriately moved. Then, the raw coal that has moved to the second descending flow chamber 106b descends the second descending flow chamber 106b and then flows from the second descending flow chamber 106b to the lower communication portion 110b by the fluidizing gas, as described above. And moves to the lower part of the second ascending flow chamber 107b, and ascends the second ascending flow chamber 107b. The raw coal receives heat from the fluidized gas, is dried while flowing, and is discharged from the dry coal discharge port 103.

  In addition, the gas generated by heating and drying the raw coal in the fluidized bed rises together with the fluidized gas, and gathers in the discharge chamber 115 from each gas discharge portion 114a, 114b, 114c, 114d, 114e, and is a gas discharge port. 105 is discharged to the outside.

  Thus, in the fluidized bed drying apparatus of Example 1, the volume of the drying container 101 is compared with the configuration in which the raw coal is heated while moving in the horizontal direction by drying with the fluidized gas while moving up and down. Without increasing the flow rate, a long flow path can be secured, the residence time of the raw coal in the drying vessel 101 can be lengthened to increase the heat transfer efficiency to the raw coal, and the drying efficiency can be improved. Reduction of moisture content and variation in moisture content can be suppressed.

  Fig. 6-1 is a graph showing the weight concentration with respect to the residence time of raw coal in the conventional fluidized bed drying device, and Fig. 6-2 is a graph showing the weight concentration with respect to the moisture content of the raw coal in the conventional fluidized bed drying device. is there. Moreover, FIG. 7-1 is a graph showing the weight concentration with respect to the residence time of raw coal in the fluidized bed drying apparatus of Example 1, and FIG. 7-2 is the water content of raw coal in the fluidized bed drying apparatus of Example 1. It is a graph showing a weight concentration.

  In the conventional fluidized bed drying apparatus, as shown in FIG. 6A, the raw coal has the largest residence time T1, and has a variation width A1 of the residence time. On the other hand, in the fluidized bed drying apparatus of Example 1, as shown in FIG. 7A, the raw coal has the largest residence time T2 and has a variation time A2 of the residence time. The width is narrow (A1> A2). Moreover, in the conventional fluidized bed drying apparatus, as shown in FIG. 6-2, the raw coal has the largest water content W1 and the water content variation width B1. On the other hand, in the fluidized bed drying apparatus of Example 1, as shown in FIG. 7-2, the raw coal has the largest water content W2 and has a residence time variation width B2, which is a variation compared to the conventional case. The width is narrow (B1> B2). That is, in the fluidized bed drying apparatus of Example 1, since a long fluid path can be secured with the same volume as the conventional one, the residence time of the raw coal in the drying container 101 is lengthened to further reduce moisture. This makes it possible to suppress variation in residence time in raw coal and reduce variation in water content.

  In the fluidized bed drying apparatus of Example 1, a plurality of descending flow chambers 106a, 106b, 106c, 106d, 106e and ascending fluid chambers 107a, 107b, 107c, 107d are alternately arranged in series in the horizontal direction, The lower part of the descending flow chambers 106a, 106b, 106c, 106d, 106e and the lower part of the ascending flow chambers 107a, 107b, 107c, 107d are communicated by the lower communication part 110, and the ascending flow chambers 107a, 107b, 107c, 107d are connected. And the upper part of the descending flow chambers 106 a, 106 b, 106 c, 106 d, 106 e are communicated by the upper communication part 111. Accordingly, the raw coal that has descended in the descending flow chambers 106a, 106b, 106c, 106d, and 106e moves up to the ascending fluid chambers 107a, 107b, 107c, and 107d through the lower communication portion 110 and then ascends there. The raw coal that has risen in the chambers 107a, 107b, 107c, and 107d moves down to the descending flow chambers 106a, 106b, 106c, 106d, and 106e through the upper communication portion 111, and then descends there. The chambers 106a, 106b, 106c, 106d, 106e and the ascending flow chambers 107a, 107b, 107c, 107d can be appropriately moved, and the raw coal can be efficiently dried.

  In the fluidized bed drying apparatus of the first embodiment, the fluidizing gas supply unit 104 supplies the fluidizing gas to at least the lower part of the ascending flow chambers 107a, 107b, 107c, and 107d. Therefore, the raw coal in the ascending flow chambers 107a, 107b, 107c, and 107d is appropriately raised by supplying the fluidizing gas to the lower portions of the ascending flow chambers 107a, 107b, 107c, and 107d by the fluidizing gas supply unit 104. Heating and drying.

  In the fluidized bed drying apparatus according to the first embodiment, the fluidizing gas supply unit 104 supplies fluidizing gas to the lower part of the descending fluid chambers 106a, 106b, 106c, 106d, 106e and the ascending fluid chambers 107a, 107b, 107c, 107d. The superficial velocity of the ascending flow chambers 107a, 107b, 107c, 107d is set higher than the superficial velocity of the descending flow chambers 106a, 106b, 106c, 106d, 106e. Accordingly, the raw coal can appropriately rise in the ascending flow chambers 107a, 107b, 107c, and 107d, and appropriately move through the descending flow chambers 106a, 106b, 106c, 106d, and 106e from the upper communication portion 111. Can descend.

  In the fluidized bed drying apparatus of the first embodiment, the pressures in the ascending flow chambers 107a, 107b, 107c, and 107d are set lower than the pressures in the descending flow chambers 106a, 106b, 106c, 106d, and 106e. Accordingly, the raw coal in the ascending flow chambers 107a, 107b, 107c, and 107d can appropriately rise in the low pressure space, and the raw coal in the descending flow chambers 106a, 106b, 106c, 106d, and 106e can be used in the high pressure space. It is possible to move properly to the ascending flow chambers 107a, 107b, 107c, 107d in the adjacent low pressure space after being properly lowered.

  In the fluidized bed drying apparatus of the first embodiment, dampers 113a, 113b, 113c, and 113d as pressure adjusting devices are provided above the ascending flow chambers 107a, 107b, 107c, and 107d. Accordingly, when the fluidizing gas is supplied to the drying container 101 by the fluidizing gas supply unit 104, the descending flow chambers 106a, 106b, 106c, 106d, and 106e are set as high-pressure spaces, but the ascending fluid chamber 107a. 107b, 107c and 107d can be set to appropriate low-pressure spaces since the pressure is adjusted by the dampers 113a, 113b, 113c and 113d.

  In the fluidized bed drying apparatus of Example 1, the descending flow chambers 106a, 106b, 106c, 106d, and 106e and the ascending fluid chambers 107a, 107b, 107c, and 107d are alternately arranged in a honeycomb shape in the horizontal direction, A raw coal inlet 102 is provided in the upper part of the first descending flow chamber 106a, and a dry coal discharge port 103 is provided in the lower part of the fifth descending flow chamber 106e. Therefore, by securing a long flow path without increasing the volume of the drying vessel 101, the residence time of the raw coal in the drying vessel 101 can be increased, and the efficiency of heat transfer to the raw coal is improved to improve the drying efficiency. can do.

  FIG. 8 is a schematic diagram showing a fluidized bed drying apparatus according to Embodiment 2 of the present invention.

  In Example 2, as shown in FIG. 8, the fluidized bed drying apparatus 200 includes a drying container 201, a raw coal charging port (charging unit) 202, a dry coal discharging port (discharging unit) 203, and a fluidized gas. A supply unit 204 and a gas discharge port 205 are provided.

  The drying container 201 has a hollow box shape, and descending flow chambers 206 for lowering the raw coal inside and rising flow chambers 207 for raising the raw coal by fluidizing gas are alternately arranged in series in the horizontal direction. A plurality are arranged. Specifically, descending flow chambers 206 (206a, 206b... 206e) and ascending flow chambers 207 (207a...) Are alternately arranged in a honeycomb shape in the horizontal direction. The descending flow chamber 206 is composed of a plurality of descending flow chambers 206a, 206b,... 206e, and the ascending fluid chamber 207 is composed of a plurality of ascending fluid chambers 207a. .

  In the drying container 201, the raw coal input port 202 is formed in the first descending flow chamber 206a, and the dry coal discharge port 203 is formed in the fifth descending flow chamber 206e. Further, the drying container 201 is provided with a dispersion plate 208 (208a, 208b) having a plurality of openings in the lower portion, so that the wind box 209 is partitioned. The drying container 201 is provided with a fluidizing gas supply unit 204 that supplies fluidizing gas to the wind box 209. Further, the drying container 201 has a gas discharge port 205 for discharging the fluidized gas and the generated gas gas on the dry coal discharge port 203 side.

  In the drying container 201, raw coal is supplied to the descending flow chamber 206 a from the raw coal inlet 202, and all the fluidizing gas flows from the fluidizing gas supply unit 204 through the wind box 209 and the dispersion plate 208. .. Are supplied to the chambers 206a, 206b... 206e and the ascending flow chambers 207a.

  The descending flow chambers 206a, 206b... 206e and the ascending flow chambers 207a... Alternately arranged at the upper part or the lower part communicate with each other by the lower communication part 210a. doing.

  Therefore, the raw coal supplied to the first descending flow chamber 206a is heated and dried by descending while flowing with the fluidizing gas. The raw coal in the first descending flow chamber 206a moves to the first ascending fluid chamber 207a through the first lower communication portion 210a, and flows in the first ascending fluid chamber 207a with the fluidizing gas. To rise. Thereafter, the raw coal is dried while alternately raising and lowering each descending flow chamber and each rising fluid chamber.

  In addition, the drying container 201 is provided with a gas supply line 212 for supplying fluidized gas to the descending flow chambers 206a, 206b,... 206e and the ascending flow chambers 207a,. That is, the tip of the gas supply line 212 is connected to a fluidized gas supply unit 204 provided at the lower part of the wind box 209. Accordingly, the fluidizing gas supplied from the gas supply line 212 to the wind box 209 through the fluidizing gas supply unit 204 passes through the dispersion plate 208 to the descending flow chambers 206a, 206b... 206e and the ascending fluid chambers 207a.・ ・ Supplied to

  At this time, in the drying container 201, the superficial velocity in each of the ascending flow chambers 207a... Is set higher than the superficial velocity in each of the descending flow chambers 206a, 206b. Specifically, the aperture ratio of the dispersion plate 208b corresponding to each ascending flow chamber 207a... Is set higher than the aperture ratio of the dispersion plate 208a corresponding to each descending flow chamber 206a, 206b. .

  That is, in each ascending flow chamber 207a..., A large amount of fluidizing gas is supplied from the wind box 209 through the dispersion plate 208b because the aperture ratio of the dispersion plate 208b is high. On the other hand, in each of the descending flow chambers 206a, 206b,... 206e, since the aperture ratio of the dispersion plate 208a is low, the fluidized gas supplied from the wind box 209 through the dispersion plate 208a is small. Therefore, the drying vessel 201 has a high superficial velocity in each of the ascending flow chambers 207a... And a low superficial velocity in each of the descending flow chambers 206a, 206b.

  Accordingly, in each of the descending flow chambers 206a, 206b,... 206e with a small supply amount of fluidizing gas, the raw coal is properly lowered, and the supply amount of fluidizing gas is increased from each lower communication portion 210a. It can move appropriately to the type fluid chamber 207a. Further, in the ascending flow chamber 207a... With a large amount of fluidized gas supplied, the raw coal rises appropriately due to the fluidized gas, and the fluidized gas decreases from the upper communication portions 211a. It can move appropriately to the type fluid chamber 206b ... 206e.

  As described above, in the fluidized bed drying apparatus of Example 2, the raw coal is dried by the fluidized gas while being repeatedly raised and lowered in the descending flow chambers 206a, 206b... 206e and the ascending flow chamber 207a. By doing so, it is possible to ensure a long flow path without increasing the volume of the drying container 201 and to increase the residence time of raw coal in the drying container 201 with respect to the configuration heated while flowing in the horizontal direction. As a result, the efficiency of heat transfer to the raw coal can be improved and the drying efficiency can be improved, and the moisture content of the raw coal can be reduced and the variation in the moisture content can be suppressed.

  In the fluidized bed drying apparatus of Example 2, the wind box 209 is partitioned by providing the dispersion plates 208 a and 208 b having a plurality of openings at the lower part of the drying container 201, and the fluidized gas supply unit 204 passes through the wind box 209. The lowering flow chambers 206a, 206b... 206e and the rising flow chamber 207a... Can be supplied with a fluidizing gas, and the aperture ratio of the dispersion plate 208b corresponding to the rising flow chamber 207a. It is set higher than the aperture ratio of the dispersion plate 208a corresponding to the type flow chambers 206a, 206b. Therefore, the superficial velocity of the ascending flow chamber 207a ... becomes higher than the superficial velocity of the descending flow chambers 206a, 206b ... 206e, and the raw coal is appropriately raised in the ascending flow chamber 207a ... It is possible to properly lower the raw coal in the descending flow chambers 206a, 206b,.

  FIG. 9 is a schematic diagram showing a fluidized bed drying apparatus according to Example 3 of the present invention.

  In Example 3, as shown in FIG. 9, the fluidized bed drying apparatus 300 includes a drying container 301, a raw coal charging port (charging unit) 302, a dry coal discharging port (discharging unit) 303, and a fluidized gas. A supply unit 304 and a gas discharge port 305 are provided.

  The drying container 301 has a hollow box shape, and descending flow chambers 306 for lowering raw coal inside and rising flow chambers 307 for raising raw coal by fluidizing gas are alternately arranged in series in the horizontal direction. A plurality are arranged. Specifically, descending flow chambers 306 (306a, 306b,... 306e) and ascending flow chambers 307 (307a,...) Are arranged alternately in a honeycomb shape in the horizontal direction. The descending flow chamber 306 includes a plurality of descending flow chambers 306a, 306b,... 306e, and the ascending flow chamber 307 includes a plurality of ascending flow chambers 307a. .

  The drying container 301 has a raw coal charging port 302 formed in the first descending flow chamber 306a, and a dry coal discharge port 303 formed in the fifth descending flow chamber 306e. In addition, the drying container 301 is provided with a dispersion plate 308 having a plurality of openings in the lower portion, so that an air box 309 (309a, 309b) is partitioned. The drying container 301 is provided with a fluidizing gas supply unit 304 (304a, 304b) that supplies fluidizing gas to the wind box 309. Further, the drying container 301 has a gas discharge port 305 for discharging the fluidized gas and the generated gas on the dry coal discharge port 303 side.

  In the drying container 301, raw coal is supplied to the descending flow chamber 306 a from the raw coal inlet 302, and all of the fluidizing gas flows from the fluidizing gas supply unit 304 through the wind box 309 and the dispersion plate 308. .. Are supplied to the chambers 306a, 306b,... 306e and the ascending flow chambers 307a, so that a fluidized bed is formed above the dispersion plate 308.

  The descending flow chambers 306a, 306b,... 306e and the ascending flow chambers 307a,... Alternately arranged at the upper or lower portion are communicated by the lower communication portion 310a. doing.

  Therefore, the raw coal supplied to the first descending flow chamber 306a is heated and dried by descending while flowing with the fluidizing gas. The raw coal in the first descending flow chamber 306a moves to the first ascending fluid chamber 307a through the first lower communication portion 310a, and flows through the first ascending fluid chamber 307a with the fluidizing gas. To rise. Thereafter, the raw coal is dried while alternately raising and lowering each descending flow chamber and each rising fluid chamber.

  In addition, the drying container 301 is provided with a gas supply line 312 for supplying fluidized gas to the descending flow chambers 306a, 306b,... 306e and the ascending flow chambers 307a,. That is, the wind box 309 provided at the lower part of the drying container 301 is divided into a wind box 309a corresponding to each descending flow chamber 306a, 306b... 306e and each ascending flow chamber 307a. A corresponding wind box 309b is partitioned, and fluidized gas supply sections 304a and 304b are provided corresponding to the respective wind boxes 309a and 309b. On the other hand, the gas supply line 312 has its distal end branched into a plurality of branch lines 314a and 314b, and the branch line 314a is connected to fluidized gas supply sections 304a corresponding to the descending flow chambers 306a, 306b,. The branch line 314b is connected to the fluidizing gas supply unit 304b. And the flow regulating valve 315a, 315b is provided in each branch line 314a, 314b.

  Accordingly, the fluidizing gas supplied from the gas supply line 312 to the fluidizing gas supply units 304a and 304b via the branch lines 314a and 314b passes through the wind boxes 309a and 309b and the dispersion plate 308, respectively. 306a, 306b... 306e and the ascending flow chambers 307a.

  At this time, in the drying container 301, the superficial velocity in each of the ascending flow chambers 307a is set higher than the superficial velocity in each of the descending flow chambers 306a, 306b,. Specifically, the supply amount of the fluidizing gas to the wind boxes 309b corresponding to the ascending flow chambers 307a ... is fluidized to the wind boxes 309a corresponding to the descending flow chambers 306a, 306b ... 306e. It is set more than the amount of gas supply.

  That is, by increasing the opening degree of the flow rate adjustment valve 315b of the branch line 314b relative to the opening degree of the flow rate adjustment valve 315a of the branch line 314a, each descending flow Are supplied from the fluidizing gas supply unit 304b through the wind boxes 309b to the ascending flow chambers 307a... With respect to the supply amount (supply speed) of the fluidizing gas supplied to the chambers 306a, 306b. The supply amount of fluidized gas is increased (the supply speed is increased). Therefore, in the drying container 301, the superficial velocity of each ascending flow chamber 307a... Is high, and the superficial velocity of each descending flow chamber 306a, 306b.

  Accordingly, in each of the descending flow chambers 306a, 306b,... 306e with a small amount of fluidized gas supplied, the raw coal is properly lowered and increased with a large amount of fluidized gas supplied from each lower communication portion 310a. It can move appropriately to the type fluid chamber 307a. Further, in the ascending flow chamber 307a... With a large amount of fluidized gas supplied, the raw coal is appropriately raised by the fluidized gas, and the fluidized gas supplied from each upper communication portion 311a. It can move appropriately to the type flow chambers 306b... 306e.

  Thus, in the fluidized bed drying apparatus of Example 3, the raw coal is dried while repeatedly moving up and down the descending flow chambers 306a, 306b,... 306e and the ascending flow chambers 307a,. A long flow path can be secured without increasing the volume of the drying vessel 301 with respect to the configuration heated while flowing in the horizontal direction, and the residence time of the raw coal in the drying vessel 301 is lengthened to increase the raw coal. It is possible to improve the efficiency of heat transfer to the water, improve the drying efficiency, reduce the moisture content of the raw coal, and suppress variations in the moisture content.

  In the fluidized bed drying apparatus according to the third embodiment, by providing the dispersion plate 308 having a plurality of openings at the lower part of the drying container 301, the wind box 309a corresponding to the descending fluid chamber 306, the ascending fluid chamber 307a,. , 309b and fluidized gas supply units 304a and 304b, and flow control valves 315a and 315b are provided in the branch lines 314a and 314b of the gas supply line 312 and connected to the fluidized gas supply units 304a and 314b, respectively. The amount of fluidizing gas supplied to the ascending flow chambers 307a... Is set higher than the amount of fluidizing gas supplied to the descending flow chambers 306a, 306b. Therefore, the superficial velocity of the ascending flow chamber 307a ... becomes higher than the superficial velocity of the descending flow chambers 306a, 306b ... 306e, and the raw coal is appropriately raised in the ascending flow chamber 307a ... It is possible to properly lower the raw coal in the descending flow chambers 306a, 306b,.

  FIG. 10 is a schematic diagram showing a fluidized bed drying apparatus according to Example 4 of the present invention.

  In Example 4, as shown in FIG. 10, the fluidized bed drying apparatus 400 includes a drying container 401, a raw coal charging port (charging unit) 402, a dry coal discharging port (discharging unit) 403, and a fluidized gas. A supply unit 404 and a gas discharge port 405 are provided.

  The drying container 401 has a hollow box shape, and descending flow chambers 406 for lowering raw coal inside and rising flow chambers 407 for raising raw coal by fluidizing gas are alternately arranged in series in the horizontal direction. A plurality are arranged. Specifically, descending flow chambers 406 (406a, 406b... 406e) and ascending flow chambers 407 (407a...) Are alternately arranged in a honeycomb shape in the horizontal direction. The descending flow chamber 406 includes a plurality of descending flow chambers 406a, 406b,... 406e, and the ascending flow chamber 407 includes a plurality of ascending flow chambers 407a,. .

  In the drying container 401, a raw coal input port 402 is formed in the first descending flow chamber 406a, and a dry coal discharge port 403 is formed in the fifth descending flow chamber 406e. Further, the drying container 401 is provided with a dispersion plate 408 having a plurality of openings in the lower portion, so that an air box 409 is partitioned. The drying container 401 is provided with a fluidizing gas supply unit 404 that supplies fluidizing gas to the wind box 409. Further, in the drying container 401, a gas discharge port 405 for discharging fluidized gas and generated gas is formed on the dry coal discharge port 403 side.

  In the drying container 401, the raw coal is supplied from the raw coal inlet 402 to the descending flow chamber 406a, and the fluidizing gas is supplied from the fluidizing gas supply unit 404 through the wind box 409 and the dispersion plate 408. ..., a fluidized bed is formed above the dispersion plate 408.

  The descending flow chambers 406a, 406b,... 406e and the ascending flow chambers 407a, which are alternately arranged, communicate with each other at the upper or lower portion by the lower communication portion 410a. doing.

  Therefore, the raw coal supplied to the first descending flow chamber 406a is heated and dried by descending while flowing with the fluidizing gas. The raw coal in the first descending flow chamber 406a moves to the first ascending fluid chamber 407a through the first lower communication portion 410a, and flows through the first ascending fluid chamber 407a with the fluidizing gas. To rise. Thereafter, the raw coal is dried while alternately raising and lowering each descending flow chamber and each rising fluid chamber.

  Further, the drying container 401 is provided with a gas supply line 412 for supplying a fluidizing gas to the descending flow chambers 406a, 406b,... 406e and the ascending flow chambers 407a,. That is, the tip of the gas supply line 412 is connected to a fluidized gas supply unit 404 provided at the lower part of the wind box 409. Therefore, the fluidizing gas supplied from the gas supply line 412 to the wind box 409 through the fluidizing gas supply unit 404 is supplied to the ascending flow chambers 407a.

  By the way, the drying container 401 is provided with inclined surfaces 413a... 413e inclined downward toward the lower part of the ascending flow chambers 407a. Yes.

  Accordingly, in each of the descending flow chambers 406a, 406b,... 406e to which almost no fluidizing gas is supplied, the raw coal is properly lowered by gravity, and the inclined surfaces 413a. It is possible to appropriately move to the ascending flow chamber 407a... Supplied with the fluidizing gas. Further, in the ascending flow chamber 407a to which the fluidizing gas is supplied, the raw coal is appropriately raised by the fluidizing gas, and the descending flow chamber 406b to 406e from each upper communication portion 411a. Can move properly.

  As described above, in the fluidized bed drying apparatus of Example 4, the lowering type flow chamber 406 (406a, 406b,... 406e) for lowering the raw coal and the upward type flow chamber 407 (407a. ..), A fluidizing gas supply unit 404 that flows and drys raw coal by supplying a fluidizing gas to the lower part of the ascending flow chamber 407 (407a...), And a descending flow chamber 406 (406a). , 406b... 406e) are provided with inclined surfaces 413a... 413e inclined downward toward the lower part of the ascending flow chamber 407 (407a...).

  Accordingly, the raw coal is dried by being heated by the fluidizing gas while repeatedly moving up and down the descending flow chambers 406a, 406b... 406e and the ascending flow chamber 407a. In other words, since the raw coal is heated while moving up and down, a long flow path can be secured without increasing the volume of the drying container 401 compared to a configuration in which the raw coal is heated while flowing in the horizontal direction. The residence time of the raw coal in the drying container 401 can be lengthened to increase the heat transfer efficiency to the raw coal and improve the drying efficiency. Further, the raw coal descending the descending flow chambers 406a, 406b,... 406e can be appropriately moved to the ascending flow chamber 407a,. The fluidization of can be promoted.

  In the embodiment described above, the inside of the drying container is divided into nine flow chambers, but the number thereof may be any number as long as it is two or more. Further, although the flow chambers in the drying container are arranged in a honeycomb shape, they may be in a straight line. In addition, an inlet is provided at the upper part of the descending flow chamber and a discharge part is provided at the lower part of the descending fluid chamber. May be disposed at the most downstream portion to provide a discharge portion, or the discharge portion may be provided at the top. And the configuration and arrangement of the shape of the drying container, raw coal inlet, dry coal outlet, fluidized gas supply unit, gas outlet are not limited to each embodiment, and installation of a fluidized bed dryer Changes can be made as appropriate according to the location and use.

  In the above-described embodiment, the wet fuel is heated and dried by the fluidized gas supplied into the drying container. However, a heat transfer tube through which the fluidized gas flows is disposed in the fluidized bed, and drying is performed. It may be promoted. In this case, a partition wall between the descending fluid chamber and the ascending fluid chamber may be formed by the heat transfer tube.

  In the above-described embodiments, low-grade coal is used as the wet fuel, but even high-grade coal can be applied, and is not limited to coal, and can be used as a renewable organic organic resource. For example, it is also possible to use thinned wood, waste wood, driftwood, grass, waste, sludge, tires, and recycled fuel (pellets or chips) using these as raw materials.

DESCRIPTION OF SYMBOLS 11 Coal feeder 12 Fluidized bed dryer 13 Pulverized coal machine 14 Coal gasifier 15 Char recovery device 16 Gas refiner 17 Gas turbine equipment 18 Steam turbine equipment 19 Generator 20 Waste heat recovery boiler 101, 201, 301, 401 Drying Container 102, 202, 302, 402 Raw coal inlet 103, 203, 303, 403 Dry coal outlet 104, 204, 304, 404 Fluidized gas supply unit 105, 205, 305, 405 Gas outlet 106, 106a, 106b 106c, 106d, 106e, 206, 206a, 206b, 206e, 306a, 306b, 306e, 406a, 406b, 406e Lowering flow chamber 107, 107a, 107b, 107c, 107d, 207a, 307a, 407a Ascending flow chamber 108 , 208a, 208 b, 308, 408 Dispersion plate 109, 209, 309a, 309b, 409 Wind box 110a, 110b, 110c, 110d, 210a, 310a, 410a Lower communication portion 111a, 111b, 111c, 111d, 211a, 311a, 411a Upper communication portion 112, 212, 312, 412 Gas supply line 113a, 113b, 113c, 113d, 113e Damper (pressure adjusting device)
315a, 315b Flow rate adjustment valve 413a, 413e Inclined surface

Claims (10)

A drying container having a hollow shape capable of discharging wet fuel from a charging portion on one end side and discharging a dried product obtained by heating and drying the wet fuel from a discharging portion on the other end side;
A fluidized gas supply unit for flowing and drying wet fuel by supplying fluidized gas to the drying container;
A descending flow chamber for lowering wet fuel;
An ascending fluid chamber for raising wet fuel by fluidizing gas continuously to the descending fluid chamber;
A fluidized bed drying apparatus comprising:   A plurality of the descending flow chambers and the ascending flow chambers arranged in series alternately in the horizontal direction, and a lower communication portion that forms a lower portion of the descending flow chamber and a lower portion of the ascending flow chamber; The fluidized bed drying apparatus according to claim 1, wherein an upper communication portion is formed in which an upper portion of the ascending fluid chamber and an upper portion of the descending fluid chamber are communicated.   The fluidized bed drying apparatus according to claim 1, wherein the fluidized gas supply unit supplies a fluidized gas to at least a lower portion of the ascending fluid chamber.   The fluidizing gas supply unit can supply fluidizing gas to the lower part of the descending flow chamber and the ascending fluid chamber, and the superficial velocity of the ascending fluid chamber is the superficial velocity of the descending fluid chamber. The fluidized bed drying apparatus according to claim 3, wherein the fluidized bed drying apparatus is set higher.   The fluidized bed drying apparatus according to any one of claims 1 to 4, wherein the pressure in the ascending fluid chamber is set lower than the pressure in the descending fluid chamber.   The fluidized bed drying apparatus according to claim 5, wherein a pressure adjusting device is provided at an upper portion of the ascending fluid chamber.   The drying container is provided with a dispersion plate having a plurality of openings at a predetermined distance from a bottom plate at a lower portion to partition a wind box, and the fluidizing gas supply unit is connected to the ascending flow through the wind box. The fluidizing gas can be supplied to the lower part of the chamber and the descending flow chamber, and the aperture ratio of the dispersion plate corresponding to the ascending fluid chamber is set higher than the aperture ratio of the dispersion plate corresponding to the descending fluid chamber. The fluidized bed drying apparatus according to any one of claims 1 to 4, wherein   The drying container is provided with a dispersion plate having a plurality of openings at a predetermined distance from a bottom plate at a lower portion so that a wind box corresponding to each of the ascending flow chamber and the descending flow chamber is partitioned, and the fluidization is performed. The gas supply unit can supply a fluidizing gas to the lower part of the ascending flow chamber and the descending flow chamber via the wind box, and the fluid supply gas to the wind box corresponding to the ascending flow chamber. The fluidized bed drying apparatus according to any one of claims 1 to 4, wherein a supply amount is set to be larger than a supply amount of fluidizing gas to an air box corresponding to the descending fluid chamber.   The fluidized bed drying apparatus according to any one of claims 1 to 8, wherein the descending fluid chamber is provided with an inclined surface that slopes downward toward a lower portion of the ascending fluid chamber. .   The descending flow chamber and the ascending flow chamber are alternately arranged in a honeycomb shape in the horizontal direction, and the charging section is provided on the uppermost stream side of the descending flow chamber. The fluidized bed drying apparatus according to any one of claims 1 to 9, wherein the discharge section is provided in a lower part of the descending fluidized chamber.

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