JP2011214807A - Fluidized-bed dryer and fluid-bed drying facility - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a fluidized-bed dryer and a fluidized-bed drying facility capable of suppressing dew formation by setting a temperature of generated steam generated by drying brown coal in a fluidized bed to be a temperature preventing dew formation of the generated steam.SOLUTION: The fluidized-bed dryer includes: a drying container 120 wherein the fluidized bed 111 is formed in a drying chamber 126 by making the brown coal 101 supplied to the drying chamber 126 flow by fluidized steam 107 supplied to the drying chamber 126 formed inside; and a superheating member 130 provided within the drying container 120 and arranged in a freeboard part F which is a region where the generated steam 104 is generated by drying the brown coal 101 in the fluidized bed 111.

Description

  The present invention relates to a fluidized bed drying apparatus and a fluidized bed drying facility for drying an object to be dried such as lignite while flowing.

  2. Description of the Related Art Conventionally, there is known a control device capable of controlling a coal drying / classifying device that blows hot air from below the coal supplied to the fluidized drying chamber to dry the coal while flowing (see, for example, Patent Document 1). . This control device has a hot air flow rate control device for controlling the flow rate of hot air blown into the fluidized drying chamber. Here, when the temperature of the exhaust gas, which is hot air that has passed through the coal, falls below the condensation temperature, moisture contained in the exhaust gas is condensed, and fine coal (pulverized coal) that has been dried by hot air is deposited in the condensed portion. Adhere to. For this reason, the hot air flow rate control device suppresses the occurrence of condensation by increasing the flow rate of hot air and raising the temperature of the exhaust gas.

JP 7-11270 A

  By the way, the temperature of the generated gas changes with time depending on the easiness of evaporation of moisture contained in coal, the temperature in the fluidized drying chamber, and the like. In other words, the flow rate of hot air that can prevent the occurrence of condensation differs depending on the easiness of evaporation of moisture contained in coal, the temperature in the fluidized drying chamber, and the like. For this reason, it is difficult to stably control the temperature of the generated gas.

  Therefore, the present invention can suppress the occurrence of condensation by setting the temperature of the generated steam generated by drying the material to be dried in the fluidized bed to a temperature at which the generated steam is not stably condensed (condensed). It is an object to provide a fluidized bed drying apparatus and a fluidized bed drying facility.

  The fluidized bed drying apparatus of the present invention is a dryer in which a fluidized bed is formed in a drying chamber by flowing a material to be dried supplied to the drying chamber with a fluidizing gas supplied to the drying chamber formed inside. And a superheater provided in a region where the generated steam is generated by drying the material to be dried of the fluidized bed.

  According to this structure, the generated steam generated by drying the material to be dried in the fluidized bed can be directly heated by the superheating means. For this reason, since the temperature of the generated steam can be set to a temperature at which the generated steam is not stably condensed (condensed), the occurrence of condensation can be suppressed.

  In this case, it is preferable to further include a temperature control means capable of controlling the superheating temperature of the superheating means.

  According to this configuration, since the superheat temperature of the superheater can be controlled, the temperature of the generated steam that passes through the superheater can be set to a suitable temperature.

  In this case, in the flow direction of the generated steam, it further includes a temperature detection means provided on the downstream side of the superheat means, and the temperature control means determines the superheat temperature of the superheat means based on the detected temperature detected by the temperature detection means. It is preferable to control.

  According to this configuration, the temperature of the generated steam on the downstream side of the superheating means can be detected by the temperature detection means. Thereby, since the temperature control means can grasp the temperature of the generated steam on the downstream side of the superheating means, the temperature of the superheating means can be set to a suitable temperature based on the detected temperature of the generated steam.

  In this case, in the flow direction of the generated steam, a processing device capable of performing processing on the generated steam is provided downstream of the superheating means, and the pressure of the generated steam introduced into the processing device and the processing device are derived. Pressure difference detection means capable of detecting a pressure difference with the pressure of the generated steam, and the temperature control means controls the superheat temperature of the superheat means based on the pressure difference detected by the pressure difference detection means, preferable.

  According to this configuration, the pressure difference of the generated steam before and after passing through the processing apparatus can be detected by the pressure difference detection means. As a result, the temperature control means can grasp the pressure difference of the generated steam before and after passing through the processing apparatus. Therefore, the temperature control means sets the temperature of the superheating means to a suitable temperature based on the pressure difference of the generated steam. can do.

  In this case, in the cross-sectional area of the drying container orthogonal to the flow direction of the generated steam, the cross-sectional area of the drying container at the position where the superheating means is disposed should be smaller than the cross-sectional area of the drying container upstream of the superheating means. ,preferable.

  According to this configuration, when the generated steam flowing on the upstream side of the superheating means flows into the superheating means, the cross-sectional area of the drying container is reduced, so that the flow velocity of the generated steam that passes through the superheating means increases. Thereby, the heat transfer efficiency with respect to the generated steam of the superheating means can be improved.

  In this case, it is preferable to further include heating means provided inside the drying container and arranged inside the fluidized bed.

  According to this structure, since the to-be-dried object of a fluidized bed can be heated with a heating means, an to-be-dried object can be dried suitably.

  In this case, the superheating means is provided with a superheated gas flow path through which high temperature gas can be circulated, and the heating means is provided with a heated gas flow path through which high temperature gas can be circulated. It is preferable to further include a high temperature gas supply means capable of supplying a high temperature gas to the channel and the heated gas flow channel.

  According to this configuration, the high temperature gas supply means can superheat the superheating means by circulating the high temperature gas through the superheated gas flow path, and can also heat the heating means by circulating the high temperature gas through the heated gas flow path. Can be heated.

  In this case, the superheating means is provided with a superheated gas flow path through which high temperature gas can be circulated, and the heating means is provided with a heated gas flow path through which high temperature gas can be circulated. It is preferable to further include a gas connection channel that connects the channel and the heated gas channel, and a high-temperature gas supply unit that can supply a high-temperature gas to the superheated gas channel.

  According to this configuration, the high temperature gas supply means can superheat the superheat means by causing the high temperature gas to flow through the superheated gas flow path. The high-temperature gas that has flowed through the superheated gas channel can flow through the gas connection channel to the heated gas channel, thereby heating the heating means.

  The fluidized bed drying facility of the present invention is provided with the above fluidized bed drying apparatus capable of drying an object to be dried, a generated steam line for discharging generated steam to the outside of the fluidized bed drying apparatus, and the generated steam line. A dust collector that removes dust in the steam, a heat recovery system that is disposed downstream of the dust collector in the generated steam line and recovers the heat of the generated steam, and generated steam from which dust has been removed from the dust collector And a cooler that cools an object to be dried that has been dried by the fluidized bed drying device.

  According to this configuration, the object to be dried can be suitably dried while suppressing the occurrence of condensation in the fluidized bed drying apparatus.

  According to the fluidized bed drying apparatus and the fluidized bed drying facility of the present invention, the generated steam generated from the fluidized bed can be directly superheated by the superheating means, whereby the temperature of the generated steam is set to a temperature at which no condensation occurs. Therefore, it is possible to suppress the occurrence of condensation due to the generated steam.

FIG. 1 is a schematic diagram illustrating an example of fluidized bed drying equipment to which the fluidized bed drying apparatus according to the first embodiment is applied. FIG. 2 is a schematic diagram showing an example of a combined coal gasification combined power generation system to which the fluidized bed drying facility shown in FIG. 1 is applied. FIG. 3 is a schematic diagram illustrating an example of fluidized bed drying equipment to which the fluidized bed drying apparatus according to the second embodiment is applied. FIG. 4 is a schematic diagram illustrating an example of fluidized bed drying equipment to which the fluidized bed drying apparatus according to the third embodiment is applied.

  Hereinafter, a fluidized bed drying apparatus and a fluidized bed drying facility according to the present invention will be described with reference to the accompanying drawings. The present invention is not limited to the following examples. In addition, constituent elements in the following embodiments include those that can be easily replaced by those skilled in the art or those that are substantially the same.

  A first embodiment of the present invention will be described with reference to the drawings. FIG. 1 is a schematic diagram illustrating an example of fluidized bed drying equipment to which the fluidized bed drying apparatus according to the first embodiment is applied.

As shown in FIG. 1, the fluidized bed drying facility 100 includes a supply hopper 118 that supplies lignite 101 having a high water content as an object to be dried, a fluidized bed drying apparatus 102 that dries the supplied lignite 101, and lignite 101. A generated steam line L ₁ that discharges the generated steam 104 generated during drying to the outside of the fluidized bed drying apparatus 102, and a dust collector that is interposed in the generated steam line L ₁ and removes dust in the generated steam 104. and 105, is interposed on the downstream side of the dust collecting apparatus 105 in generating steam line L _1, the heat recovery system 106 for recovering the steam generated 104 heat, the dust collecting apparatus generates steam 104 where dust is removed from 105 A branch line L _{2 that} is partly branched and supplied into the fluidized bed drying device 102 as fluidized steam (fluidized gas) 107, and extracted from the fluidized bed drying device 102. A cooler 110 that cools the dried lignite 108 to produce product charcoal 109 is provided.

In the fluidized bed drying facility 100, the lignite 101 is introduced into the fluidized bed drying device 102 by the supply hopper 118 via the supply line L _0, and is fluidized by the fluidized steam 107 separately introduced into the fluidized bed drying device 102. Thus, the fluidized bed 111 is formed.

The fluidized bed drying apparatus 102 includes a drying container 120 into which lignite 101 is charged and a gas dispersion plate 121 provided inside the drying container 120. The gas distribution plate 121 divides the space inside the drying container 120 into a chamber chamber 125 located on the lower side in the vertical direction (lower side in the drawing) and a drying chamber 126 located on the upper side in the vertical direction (upper side in the drawing). ing. The fluidized steam 107 is introduced into the chamber chamber 125 from the branch line L ₂ , and a large number of through holes 121 a are formed in the gas dispersion plate 121.

  Therefore, in the fluidized bed drying apparatus 102, the brown coal 101 is introduced into the drying chamber 126 of the drying container 120 by the supply hopper 118, and the fluidized steam 107 is introduced into the chamber chamber 125. Then, the fluidized steam 107 introduced into the chamber chamber 125 passes through the through holes 121a of the gas dispersion plate 121 and blows the fluidized steam 107 to the lignite 101 in the drying chamber 126, thereby Let it flow. As a result, a fluidized bed 111 in which the lignite 101 flows is formed in the drying chamber 126. That is, in the drying chamber 126, the fluidized bed 111 is formed on the lower side in the vertical direction, and the free board portion F is formed on the upper side in the vertical direction. This free board part F is an area where the generated steam 104 is generated by drying the lignite 101 of the fluidized bed 111.

  This fluidized bed drying apparatus 102 includes a heat transfer member 103 as a heating means provided in the fluidized bed 111, a superheat member 130 as a superheater provided in the free board portion F, a heat transfer member 103, and a superheater. A superheated steam supply device (high temperature gas supply means) 135 capable of supplying superheated steam (high temperature gas) A to the member 130 is provided. The fluidized bed drying apparatus 102 includes a temperature control device (temperature control means) 140 that can control the temperature of the superheat member 130, a temperature detection sensor (temperature detection means) 141 connected to the temperature control device 140, and a temperature control. A pressure difference detection sensor (pressure difference detection means) 142 connected to the apparatus 140 and a flow rate adjustment valve 143 as a flow rate adjustment means connected to the temperature control device 140 are provided.

The heat transfer member 103 removes moisture in the lignite 101 of the fluidized bed 111, and the first steam channel (heating gas channel) R _{1 through} which superheated steam (for example, 150 ° C. steam) A can flow is provided. Have. Therefore, when the 150 ° C. superheated steam A is supplied to the first steam flow path R ₁ of the heat transfer member 103, the heat transfer member 103 dries the lignite 101 using the latent heat of the high temperature superheated steam A. Thereafter, the superheated steam A used for drying is discharged outside the fluidized bed drying apparatus 102 as, for example, 150 ° C. condensed water B.

That is, on the inner surface of the first steam flow path R ₁ , the superheated steam A condenses into a liquid (moisture), so the condensed latent heat radiated at this time is effectively used for heating the drying of the lignite 101. . Any heating medium other than the high-temperature superheated steam A may be used as long as it is accompanied by a phase change. Examples thereof include Freon, pentane, and ammonia. In addition to using a heat medium as the heat transfer member 103, an electric heater may be installed. The generated steam 104 generated when the lignite 101 is dried by the heat transfer member 103 flows to the free board portion F on the upper side in the vertical direction (downstream side in the flow direction of the generated steam 104).

The superheating member 130 superheats the generated steam 104 that has flowed into the freeboard portion F, and the second superheater (superheated gas channel) R _{2 through} which superheated steam (for example, 150 ° C. steam) A can flow is provided. Have. Therefore, when the 150 ° C. superheated steam A is supplied to the second steam flow path R ₂ of the superheat member 130, the superheat member 130 uses the latent heat of the high temperature superheated steam A to superheat the generated steam 104. Thereafter, the superheated steam A used for overheating is discharged outside the fluidized bed drying apparatus 102 as, for example, 150 ° C. condensed water B. Note that, similarly to the heat transfer member 103, the superheat member 130 may be provided with an electric heater in addition to using a heat medium.

Superheated steam supplying device 135 via a heating line L _5, and supplies the superheated steam A to the first steam flow passage R ₁ of the heat transfer member 103. Also, superheated steam supplying device 135 via a heating line L ₆ branched from the heating line L _5, and supplies the superheated steam A to the second steam flow passage R ₂ superheating member 130. That is, the superheated steam supply device 135 heats the heat transfer member 103 and superheats the superheat member 130 by supplying the superheated steam A to each of the heat transfer member 103 and the superheat member 130.

Here, the temperature of the overheating member 130 is controlled by adjusting the opening degree of the flow rate adjusting valve 143 by the temperature control device 140. Flow control valve 143 is interposed in overheating line L _6, and adjusts the flow rate of the superheated steam A flowing overheating line L _6.

Temperature detection sensor 141 is provided in the steam generation line L _1, and detects the temperature of the steam generated 104 for circulating steam generated line L _1. The temperature detection sensor 141 outputs the detected temperature detected toward the temperature control device 140.

The pressure difference detection sensor 142 is disposed so as to be able to detect the pressure difference of the generated steam 104 flowing before and after the dust collector (processing device) 105. That is, the pressure difference detection sensor 142 detects the pressure of the generated steam 104 that flows through the generated steam line L ₁ on the upstream side of the dust collector 105, and flows through the generated steam line L ₁ on the downstream side of the dust collector 105. The pressure of the generated steam 104 is detected. The pressure difference detection sensor 142 detects a difference between the pressure of the generated steam 104 on the upstream side of the dust collector 105 and the pressure of the generated steam 104 on the downstream side of the dust collector 105 as a pressure difference, and this pressure difference. Is output to the temperature control device 140.

  The temperature control device 140 adjusts the opening degree of the flow rate adjustment valve 143 based on the detected temperature input from the temperature detection sensor 141 and the pressure difference input from the pressure difference detection sensor 142, so that the superheater member 130. The temperature is controlled.

  More specifically, the temperature control device 140 determines whether or not the detected temperature input from the temperature detection sensor 141 is, for example, a preset temperature, that is, a temperature at which the generated steam 104 is not condensed. To do. As a result of the determination, when the detected temperature is equal to or higher than the set temperature, the temperature control device 140 controls the flow rate adjustment valve 143 to the valve closing side, whereas when the detected temperature is lower than the set temperature, the temperature control device 140 The flow rate adjusting valve 143 is controlled to the valve opening side.

  Further, the temperature control device 140 determines whether or not the pressure difference input from the pressure difference detection sensor 142 is, for example, a preset pressure difference that is set in advance, that is, a pressure difference that does not cause condensation of the generated steam 104. . Here, the case where the pressure difference becomes large is a case where the pressure of the generated steam 104 downstream of the dust collector 105 is lower than the pressure of the generated steam 104 upstream of the dust collector 105. This is because the pressure of the generated steam 104 decreases as the temperature of the generated steam 104 on the downstream side of the dust collector 105 decreases. Therefore, as a result of the determination, when the pressure difference is equal to or larger than the set pressure difference, the temperature control device 140 controls the flow rate adjustment valve 143 to the valve opening side, while when the pressure difference is less than the set pressure difference, the temperature control is performed. The device 140 controls the flow rate adjustment valve 143 to the valve closing side.

Therefore, in the fluidized bed drying apparatus 102, the heat transfer member 103 provided inside the fluidized bed 111 heats the lignite 101 of the fluidized bed 111 to dry the lignite 101. The generated steam 104 generated by drying the lignite 101 flows from the fluidized bed 111 into the free board portion F. The freeboard unit generating steam 104 flowing into the F, after being superheated by heating member 130 is discharged to the outside of the fluidized bed dryer 102 by generating steam line L _1.

Since the generated steam 104 includes a pulverized coal 101 that has been dried and pulverized, it is collected as a solid component 115 by a dust collector 105 such as a cyclone or an electric dust collector. The solid component 115, through the separating line L _3, are mixed and joins the dry brown coal 108 withdrawn from the fluidized bed dryer 102, which was cooled by the cooler 110, through the product line L ₄ , And discharged as product charcoal 109. This product charcoal 109 is used as a raw material for boilers, gasifiers, and the like.

  On the other hand, since the generated steam 104 after being collected by the dust collector 105 is, for example, steam at 105 to 110 ° C., it is recovered by the heat recovery system 106, processed by the water treatment unit 112, and drained 113. As shown in FIG. Note that the generated steam 104 after being collected by the dust collector 105 may be applied to, for example, a heat exchanger, a steam turbine, or the like to effectively use the heat.

Part of the steam generated 104 after being dust collecting by a dust collector 105, is sent to the fluidized bed dryer 102 by the circulation fan 114 interposed in the branch line L _2, the fluidized bed of lignite 101 It is used as fluidized steam 107 that causes 111 to flow. As a fluidizing medium for fluidizing the fluidized bed 111, a part of the generated steam 104 is reused. However, the fluidizing medium is not limited to this. For example, nitrogen, carbon dioxide, or a low oxygen concentration containing these gases is used. Air may be used.

  In addition, although the brown coal 101 was illustrated as to-be-dried material, as long as it has a high water content, it is good also considering to-be-dried materials, such as low grade coal containing subbituminous coal, sludge, etc., and sludge.

  Next, an example applied to an integrated coal gasification combined cycle (IGCC) system using the product coal 109 dried by the fluidized bed drying apparatus 102 according to the first embodiment will be described. FIG. 2 is a schematic diagram showing an example of a combined coal gasification combined power generation system to which the fluidized bed drying facility shown in FIG. 1 is applied.

  As shown in FIG. 2, the coal gasification combined power generation system 200 is a pulverized coal 201 a obtained by drying brown coal 101 as a fuel in a fluidized bed drying facility 100 to obtain product coal 109 and then pulverizing the product coal 109 in a mill 210. A coal gasification furnace 203 that converts the gasified gas 202 into gasified gas 202, a gas turbine (GT) 204 that is operated using the gasified gas 202 as fuel, and an exhaust gas that introduces turbine exhaust gas 205 from the gas turbine 204. A steam turbine (ST) 208 operated by steam 207 generated by a heat recovery boiler (HRSG) 206, and a generator (G) connected to the gas turbine 204 and / or the steam turbine 208 209.

The coal gasification combined power generation system 200 gasifies pulverized coal 201a pulverized by a mill 210 in a coal gasification furnace 203 to obtain a gasified gas 202 which is a generated gas. The gasified gas 202 is dust-removed and gas-purified by a cyclone 211 and a gas purifier 212, and then supplied to a combustor 213 of a gas turbine 204, which is a power generation means. Is generated. The gas turbine 204 is driven by the combustion gas 214. The gas turbine 204 is connected to a generator 209, and the generator 209 generates electric power when the gas turbine 204 is driven. Since the turbine exhaust gas 205 after driving the gas turbine 204 still has a temperature of about 500 to 600 ° C., it is sent to an exhaust heat recovery boiler (HRSG) 206, where thermal energy is recovered. In the exhaust heat recovery boiler (HRSG) 206, steam 207 is generated by the thermal energy of the turbine exhaust gas 205, and the steam turbine 208 is driven by the steam 207. The exhaust gas 215 from which heat energy has been recovered by the exhaust heat recovery boiler (HRSG) 206 is released into the atmosphere via the chimney 217 after the NOx and SOx components in the exhaust gas 215 are removed by the gas purification device 216. . In the figure, reference numeral 218 denotes a condenser, 219 denotes air, 220 denotes a compressor, and 221 denotes an air separation device (ASU) that separates air into nitrogen (N ₂ ) and oxygen (O ₂ ). .

  According to this coal gasification combined cycle power generation system 200, even when gasifying using lignite 101 having a high moisture content, since the lignite 101 is dried by the efficient fluidized bed drying apparatus 102, the gasification efficiency is high. The power generation can be improved stably over a long period of time.

  In addition, as a power generation system using the product charcoal 109 dried with the fluidized-bed drying equipment 100 which concerns on a present Example, it is not restricted to the coal gasification combined cycle power generation system 200 mentioned above. For example, although not explicitly shown in the figure, a brown coal cooking boiler that supplies product charcoal 109 dried in the fluidized bed drying facility 100 to a boiler furnace, drives a steam turbine with steam generated in the boiler furnace, and obtains output by a generator. May be a power generation system.

  According to the above configuration, by using the fluidized bed drying apparatus 102 of the first embodiment, the generated steam 104 generated by drying the lignite 101 of the fluidized bed 111 can be directly superheated by the superheating member 130. Further, the temperature control device 140 can control the temperature of the superheating member 130 so that the generated steam 104 does not condense (condensate). Thereby, the fluidized-bed drying apparatus 102 which concerns on Example 1 can suppress generation | occurrence | production of the dew condensation by the generated steam 104, and can control the temperature of the generated steam 104 stably by the temperature control apparatus 140. .

  Further, the temperature control device 140 can control the temperature of the superheated member 130 based on the detected temperature of the generated steam 104 detected by the temperature detection sensor 141, and the generated steam 104 detected by the pressure difference detection sensor 142. Based on the pressure difference, the temperature of the superheat member 130 can be controlled. For this reason, the temperature control apparatus 140 can grasp | ascertain suitably the temperature and pressure difference of the generation | occurrence | production steam 104, and can perform suitably the temperature control of the overheating member 130 by this.

Also, superheated steam feeding device 135, the first steam flow passage R ₁ and the second steam flow passage R _2, it is possible to supply superheated steam A, respectively, can be suitably heated heat transfer member 103 The overheating member 130 can be suitably heated.

  In the first embodiment, the heat transfer member 103 is disposed inside the fluidized bed 111. However, the heat transfer member 103 may be omitted. In this case, the lignite 101 of the fluidized bed 111 is preferably configured to be dried by the fluidized steam 107. Further, although the superheated steam A is sent to the heat transfer member 103 and the superheated member 130 by the superheated steam supply device 135, not only the superheated steam A but also other high-temperature gas may be sent. Furthermore, in the first embodiment, the temperature control device 140 controls the flow rate adjustment valve 143 based on the detection results of the temperature detection sensor 141 and the pressure difference detection sensor 142, but the temperature detection sensor 141 or the pressure difference detection sensor 142 It is good also as a structure which abolished either one. That is, the temperature control device 140 may control the flow rate adjustment valve 143 based on the detection result of the temperature detection sensor 141 or the pressure difference detection sensor 142.

  Next, Example 2 will be described with reference to the drawings. FIG. 3 is a schematic diagram illustrating an example of fluidized bed drying equipment to which the fluidized bed drying apparatus according to the second embodiment is applied. Only different parts will be described in order to avoid duplicate descriptions. In the fluidized bed drying apparatus 102 according to the first embodiment, the superheated steam A is supplied to the heat transfer member 103 and the superheated member 130 by the superheated steam supply apparatus 135, but in the fluidized bed drying apparatus 250 according to the second embodiment, the superheated steam A is supplied. After the superheated steam A is supplied to the superheated member 256 by the supply device 257, it is supplied from the superheated member 256 to the heat transfer member 255. Hereinafter, the fluidized bed drying apparatus 250 of Example 2 will be described.

As shown in FIG. 3, the fluidized bed dryer 250, the heat transfer and member 255, the superheated member 256 having a second steam flow passage _{R 2,} the first steam flow passage _{R 1} having a first steam flow path _{R 1} and a connecting channel R ₃ in which the second connecting steam path R _2, and a superheated steam supplying device 257 capable of supplying superheated steam a to a second steam flow path R _2.

Superheated steam supplying device 257 via a heating line L _6, and supplies the superheated steam A to the second steam flow passage R ₂ superheating member 256. Superheating member 256, a second end of the steam flow path R ₂ is connected to a superheated line L _6, second end of the steam channel R ₂ is connected to one end of the connecting channel R _3. One end of the connection channel R ₃ is connected to the other end of the second steam channel R ₂ , and the other end is connected to one end of the first steam channel R ₁ of the heat transfer member 255. The heat transfer member 255 has one end of the first steam flow path R ₁ connected to the other end of the connection flow path R ₃ , and the other end of the first steam flow path R ₁ supplies condensed water B to the outside of the fluidized bed drying apparatus 250. It is configured so that it can be discharged. Note that the heating line L _6, flow control valve 143 of Embodiment 1 is interposed.

Accordingly, when the superheated steam A passes from the superheated steam supply device 257 through the superheat line L ₆ and is supplied to the superheated member 256, the superheated steam A flows through the second steam flow path R ₂ and flows into the superheated member 256. Overheat. Thereafter, the superheated steam A that has flowed through the second steam flow path R ₂ flows through the connection flow path R ₃ and flows into the heat transfer member 255. Superheated steam A which has flown into the heat transfer member 255, and flows through the first vapor passage R _1, heating the heat transfer member 255.

  According to the above configuration, the superheated steam supply device 257 can superheat the superheat member 256 by supplying the superheated steam A to the superheat member 256 and can heat the heat transfer member 255. Thereby, since the flow of the superheated steam A can be serialized, the structure of the fluidized bed drying apparatus 250 can be simplified.

  Next, Example 3 will be described with reference to the drawings. FIG. 4 is a schematic diagram illustrating an example of fluidized bed drying equipment to which the fluidized bed drying apparatus according to the third embodiment is applied. In this case, only different parts will be described in order to avoid redundant description. In the fluidized bed drying apparatus 102 according to the first embodiment, the cross-sectional area perpendicular to the vertical direction of the drying container 120 is the same in the vertical direction. That is, the cross-sectional area of the drying container 120 in the free board portion F provided with the superheating member 130 and the cross-sectional area of the drying container 120 in the fluidized bed 111 are the same. On the other hand, in the fluidized bed drying apparatus 270 according to the third embodiment, the cross-sectional area of the drying container 271 in the free board portion F provided with the superheat member 273 is different from the cross-sectional area of the drying container 271 in the fluidized bed 111. . Hereinafter, the fluidized bed drying apparatus 270 of Example 3 will be described.

  In the drying container 271 of the fluidized bed drying device 270, the fluidized bed 111 is formed on the lower side in the vertical direction, and the free board portion F is formed on the upper side in the vertical direction. At this time, the drying container 271 has a tapered shape in which a portion of the freeboard portion F tapers as it goes upward in the vertical direction. For this reason, in the cross-sectional area of the drying container 271 orthogonal to the vertical direction (that is, the flow direction of the generated steam), the cross-sectional area of the drying container 271 in the free board portion F is compared with the cross-sectional area of the drying container 271 in the fluidized bed 111. It is getting smaller. And the overheating member 273 is arrange | positioned at the front end side (vertical direction upper side) of the free board part F formed in the taper shape. The superheating member 273 has substantially the same configuration as that of the superheating member 130 of the first embodiment, but the size of the superheating member 273 is also reduced because the cross-sectional area of the drying container 271 in the free board portion F is small.

  Therefore, when the generated steam 104 is generated from the fluidized bed 111, the generated steam 104 passes through the free board part F. At this time, the cross-sectional area of the drying container 271 in the free board part F is directed upward in the vertical direction. It gets smaller. For this reason, as for the generated steam 104 heading upward in the vertical direction, the flow velocity of the generated steam 104 increases as the cross-sectional area of the free board portion F decreases. As a result, the generated steam 104 having an increased flow rate passes through the superheating member 273.

  According to the above configuration, the generated steam 104 generated from the fluidized bed 111 toward the upper side in the vertical direction is generated steam 104 because the cross-sectional area of the drying container 271 in the free board portion F provided with the superheat member 273 is reduced. Increases the flow rate. For this reason, since the generated steam 104 having an increased flow velocity passes through the superheat member 273, the heat transfer efficiency of the superheat member 273 with respect to the generated steam 104 can be improved.

  As described above, the fluidized bed drying apparatus and the fluidized bed drying facility according to the present invention are useful for those using lignite as a material to be dried, and are particularly suitable for suppressing the occurrence of condensation.

DESCRIPTION OF SYMBOLS 100 Fluidized bed drying equipment 101 Brown coal 102 Fluidized bed drying apparatus 103 Heat transfer member 104 Generated steam 105 Dust collector 106 Heat recovery system 107 Fluidized steam 108 Dry brown coal 109 Product charcoal 110 Cooler 111 Fluidized bed 120 Drying container 125 Chamber chamber 126 Drying chamber 130 Superheated member 135 Superheated steam supply device 140 Temperature control device 141 Temperature detection sensor 142 Pressure difference detection sensor 143 Flow rate adjustment valve 200 Coal gasification combined power generation system 250 Fluidized bed drying device (Example 2)
255 Heat transfer member (Example 2)
256 Overheating member (Example 2)
257 Superheated steam supply device (Example 2)
270 Fluidized bed dryer (Example 3)
271 Drying container (Example 3)
273 Superheater (Example 3)
A Superheated steam B Condensate F Free board section L ₁ Generation steam line L ₂ Branch line L ₃ Separation line L ₄ Product line L ₅ Heating line L ₆ Superheating line R ₁ 1st steam flow path (heating gas flow path)
R ₂ second steam channel (superheated gas channel)
R ₃ connecting channel (Example 2)

Claims (9)

A drying container in which a fluidized bed is formed in the drying chamber by flowing the material to be dried supplied to the drying chamber by a fluidizing gas supplied to the drying chamber formed inside,
A fluidized bed drying apparatus comprising: superheating means provided in a region where generated steam is generated by drying the material to be dried of the fluidized bed provided inside the drying container.   The fluidized bed drying apparatus according to claim 1, further comprising temperature control means capable of controlling a superheating temperature of the superheating means. In the flow direction of the generated steam, further comprising a temperature detecting means provided on the downstream side of the superheating means,
The fluidized bed drying apparatus according to claim 2, wherein the temperature control unit controls the superheat temperature of the superheat unit based on the detected temperature detected by the temperature detection unit. In the flow direction of the generated steam, a processing apparatus capable of executing processing on the generated steam is provided downstream of the superheating means,
Pressure difference detection means capable of detecting a pressure difference between the pressure of the generated steam introduced into the processing apparatus and the pressure of the generated steam derived from the processing apparatus;
The fluidized bed drying apparatus according to claim 2 or 3, wherein the temperature control means controls a superheat temperature of the superheat means based on the pressure difference detected by the pressure difference detection means.   In the cross-sectional area of the drying container perpendicular to the flow direction of the generated steam, the cross-sectional area of the drying container at the position where the superheating means is disposed is larger than the cross-sectional area of the drying container on the upstream side of the superheating means. The fluidized bed drying apparatus according to any one of claims 1 to 4, wherein the fluidized bed drying apparatus is small.   The fluidized bed drying apparatus according to any one of claims 1 to 5, further comprising heating means provided inside the drying container and disposed inside the fluidized bed. The superheating means is provided with a superheated gas passage capable of circulating a high-temperature gas therein,
The heating means is provided with a heating gas flow path through which the high-temperature gas can flow,
The fluidized bed drying apparatus according to claim 6, further comprising a high-temperature gas supply unit capable of supplying the high-temperature gas to the superheated gas channel and the heated gas channel, respectively. The superheating means is provided with a superheated gas passage capable of circulating a high-temperature gas therein,
The heating means is provided with a heating gas flow path through which the high-temperature gas can flow,
A gas connection channel connecting the superheated gas channel and the heated gas channel;
The fluidized bed drying apparatus according to claim 6, further comprising a high-temperature gas supply unit capable of supplying the high-temperature gas to the superheated gas flow path. The fluidized bed drying apparatus according to any one of claims 1 to 8, capable of drying an object to be dried;
A generated steam line for discharging the generated steam to the outside of the fluidized bed drying device;
A dust collector that is interposed in the generated steam line and removes dust in the generated steam;
A heat recovery system that is interposed downstream of the dust collector in the generated steam line and recovers the heat of the generated steam;
A branch line for branching a part of the generated steam from which dust is removed from the dust collector, and supplying the fluidized gas into the fluidized bed drying device;
A fluidized bed drying facility comprising: a cooler for cooling the material to be dried dried by the fluidized bed drying device.

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