JP2013178027A - Exhaust device of non-condensable gas, integrated gasification combined cycle facility, and exhaust method of non-condensable gas - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide an exhaust device of non-condensable gas, an integrated gasification combined cycle facility, and an exhaust method of non-condensable gas capable of efficiently recovering the latent heat of steam by suppressing the mixing of non-condensable gas.SOLUTION: An exhaust device 8 is provided between a fluid bed drying device 1 capable of drying brown coal while making the brown coal flow by fluidizing gas and a coal supplying device 111 capable of supplying the brown coal toward the fluid bed driving device 1 while being separated by the use of a partition from the coal supplying device 111 and from the fluid bed driving device 1, non-condensable gas which is mixed in together with the brown coal supplied from the coal supplying device 111 is exhausted.

Description

  The present invention relates to a non-condensable gas exhaust device that exhausts non-condensable gas mixed when supplying wet fuel such as lignite, a gasification combined power generation facility, and a non-condensable gas exhaust method.

  Conventionally, a low-grade coal drying method and apparatus for supplying low-grade coal, such as brown coal, from a hopper to a drying vessel, and flowing the low-grade coal supplied in the drying vessel with steam (steam) to dry it is known. (For example, refer to Patent Document 1). In this low-grade coal drying apparatus, the steam discharged from the drying vessel is supplied to the partial condenser to recover the latent heat of the steam.

Japanese Patent Laid-Open No. 61-250096

  By the way, in a fluidized bed drying apparatus that dries wet fuel such as lignite with fluidized steam such as water vapor, the steam discharged from the fluidized bed drying apparatus may be recompressed and used. At this time, if non-condensable gas is mixed into the steam discharged from the fluidized bed drying device, the recompressed steam becomes low quality (quality: ratio of vapor in the vapor phase to the total amount of vapor), that is, liquid As the proportion of vapor in the phase increases, the proportion of vapor in the gas phase decreases and the proportion of non-condensable gas increases. As a result, the steam with low quality increases the proportion of the non-condensable gas, so that the steam temperature is lowered and it is difficult to recover latent heat.

  Accordingly, the present invention provides a non-condensable gas exhaust device, a gasification combined power generation facility, and a non-condensable gas exhaust capable of efficiently recovering the latent heat of the steam by suppressing the mixing of the non-condensable gas. It is an object to provide a method.

  The non-condensable gas exhaust apparatus of the present invention includes a fluidized bed drying apparatus capable of drying wet fuel while fluidizing the wet fuel with fluidized steam, and a fuel supply capable of supplying the wet fuel toward the fluidized bed drying apparatus. The non-condensable gas mixed with the wet fuel supplied from the fuel supply device is exhausted in a state where the fuel supply device and the fluidized bed drying device are separated from each other. Features.

  According to this configuration, the non-condensable gas mixed with the wet fuel can be exhausted in a state where the fuel supply device and the fluidized bed drying device are separated from each other. For this reason, it is possible to supply the wet fuel to the fluidized bed drying apparatus while suppressing the mixing of the non-condensable gas. Thereby, the vapor | steam discharged | emitted from a fluidized-bed drying apparatus can be made into a thing with little mixing amount of noncondensable gas. Therefore, when the steam discharged from the fluidized bed drying device is recompressed and the recompressed steam is used, the steam temperature is difficult to decrease even if the steam is of low quality. Is suppressed, and the latent heat of steam can be efficiently recovered.

  In this case, a fuel storage unit that stores wet fuel supplied from the fuel supply device, and a plurality of partitions provided between the fuel supply device and the fuel storage unit and between the fuel storage unit and the fluidized bed drying device, respectively. And a gas exhaust part for exhausting the non-condensable gas in the fuel storage part.

  According to this configuration, wet fuel is stored in the fuel storage unit, and the partition units partition the fuel supply unit and the fuel storage unit and the fuel storage unit and the fluidized bed drying unit, respectively. By exhausting the non-condensable gas in the fuel storage part by the gas exhaust part, the non-condensable gas can be suitably exhausted.

  In this case, the gas exhaust part preferably has a steam supply part that supplies steam into the fuel storage part and a gas discharge part that discharges the non-condensable gas in the fuel storage part.

  According to this configuration, the vapor supply unit supplies the vapor into the fuel storage unit, and the non-condensable gas in the fuel storage unit is discharged from the gas discharge unit, thereby filling the non-condensable gas in the fuel storage unit with the vapor. Can do. Thereby, since the non-condensable gas in the fuel reservoir can be replaced with steam, the non-condensable gas can be suitably exhausted. Further, the wet fuel stored in the fuel storage unit can be preheated by the supplied steam. For this reason, since the preheated wet fuel can be supplied to the fluidized bed drying device, the recondensation of the steam can be suppressed on the supply side of the fluidized bed drying device, and the fluidization of the wet fuel due to the condensed water can be prevented. Can be suppressed.

  In this case, it is preferable that the gas exhaust part has a gas intake part that intakes the non-condensable gas in the fuel storage part.

  According to this configuration, the non-condensable gas in the fuel storage unit can be sucked by the gas intake unit. Thereby, the noncondensable gas in a fuel storage part can be forcedly exhausted.

  The combined gasification power generation facility of the present invention includes a fluidized bed drying device capable of drying wet fuel while fluidizing the wet fuel with fluidized steam, and a fuel supply device capable of supplying wet fuel to the fluidized bed drying device. The non-condensable gas exhaust device provided between the fluidized bed drying device and the fuel supply device, and the dried wet fuel supplied from the fluidized bed drying device are processed and converted into gasified gas. A gasification furnace, a gas turbine that is operated using gasified gas as fuel, a steam turbine that is operated by steam generated by an exhaust heat recovery boiler that introduces turbine exhaust gas from the gas turbine, and a gas turbine and a steam turbine connected to each other It is characterized by having a generator.

  According to this configuration, since the non-condensable gas can be exhausted by the exhaust device, the wet fuel is suitably supplied to the fluidized bed drying device while suppressing the mixing of the non-condensable gas into the fluidized bed drying device. be able to. For this reason, the wet fuel suitably fluidized and dried in the fluidized bed drying apparatus can be supplied to the gasification furnace.

  The non-condensable gas exhaust method of the present invention includes a fuel storage step for storing supplied wet fuel, a fuel isolation step for isolating wet fuel after execution of the fuel storage step, and a wet operation after execution of the fuel isolation step. And an exhaust process for exhausting the non-condensable gas mixed together with the supply of fuel.

  According to this configuration, by executing the fuel isolation step and the exhaust step, the non-condensable gas mixed together with the supply of the wet fuel can be exhausted in a state where the wet fuel is isolated in the fuel reservoir. For this reason, it is possible to supply the wet fuel to the fluidized bed drying apparatus while suppressing the mixing of the non-condensable gas. Thereby, the vapor | steam discharged | emitted from a fluidized-bed drying apparatus can be made into a thing with little mixing amount of noncondensable gas. Therefore, when the steam discharged from the fluidized bed drying device is recompressed and the recompressed steam is used, the steam temperature is difficult to decrease even if the steam is of low quality. Is suppressed, and the latent heat of steam can be efficiently recovered.

  According to the non-condensable gas exhaust device and the non-condensable gas exhaust method of the present invention, the steam discharged from the fluidized bed drying device by suppressing the mixing of the noncondensable gas into the fluidized bed drying device. Since the mixing amount of the non-condensable gas contained in can be suppressed, the temperature drop of the recompressed steam can be suppressed, and the latent heat of the recompressed steam can be efficiently recovered.

FIG. 1 is a schematic configuration diagram of a combined coal gasification combined power generation facility to which an exhaust device according to a first embodiment is applied. FIG. 2 is a schematic configuration diagram schematically illustrating the exhaust device according to the first embodiment. FIG. 3 is a graph relating to the quality of drying steam in a conventional fluidized bed drying apparatus. FIG. 4 is a graph relating to the quality of the drying steam in the fluidized bed drying apparatus according to the first embodiment. FIG. 5 is a schematic configuration diagram schematically illustrating the exhaust device according to the second embodiment. FIG. 6 is a schematic configuration diagram schematically illustrating the exhaust device according to the third embodiment.

  Hereinafter, a non-condensable gas exhaust apparatus, a combined gasification power generation facility, and a non-condensable gas exhaust method 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.

  FIG. 1 is a schematic configuration diagram of a combined coal gasification combined power generation facility to which an exhaust device according to a first embodiment is applied. An integrated coal gasification combined cycle (IGCC) 100 to which the exhaust device 8 of the first embodiment is applied employs an air combustion method in which coal gas is generated in a gasification furnace using air as an oxidant, Coal gas after being refined by a gas purifier is supplied to gas turbine equipment as fuel gas to generate electricity. That is, the combined coal gasification combined power generation facility 100 according to the first embodiment is an air combustion type (air blowing) power generation facility. In this case, lignite is used as wet fuel supplied to the gasifier.

  In Example 1, lignite was used as the wet fuel, but low-grade coal including sub-bituminous coal, peat such as sludge, etc. may be applied as long as the moisture content is high. Even charcoal is applicable. In addition, the wet fuel is not limited to coal such as lignite, but may be biomass used as organic resources derived from renewable organisms. For example, thinned wood, waste wood, driftwood, grass, waste, It is also possible to use sludge, tires, and recycled fuel (pellets and chips) made from these raw materials.

  In the first embodiment, as shown in FIG. 1, the coal gasification combined power generation facility 100 includes a coal supply device (fuel supply device) 111, an exhaust device 8, a fluidized bed drying device 1, a pulverized coal machine 113, a coal gasification furnace. 114, a char recovery device 115, a gas purification device 116, a gas turbine facility 117, a steam turbine facility 118, a generator 119, and a heat recovery steam generator (HRSG) 120.

  The coal feeder 111 includes a raw coal bunker 121, a coal feeder 122, and a crusher 123. The raw coal bunker 121 can store lignite, and drops a predetermined amount of lignite into the coal feeder 122. The coal feeder 122 transports the brown coal dropped from the raw coal bunker 121 by a conveyor or the like and drops it on the crusher 123. The crusher 123 finely pulverizes the dropped lignite into fine particles.

  The exhaust device 8 exhausts non-condensable gas mixed with the lignite supplied from the coal supply device 111. The non-condensable gas is so-called nitrogen-containing air. The details of the exhaust device 8 will be described later.

  The fluidized bed drying apparatus 1 causes the lignite supplied from the coal feeder 111 through the exhaust device 8 to flow with fluidized steam such as steam, and heat-drys it with the heat transfer tube 33 to thereby remove moisture contained in the lignite. To be removed. The fluidized bed drying apparatus 1 is connected to a cooler 131 for cooling the discharged dried lignite (dry coal). The cooler 131 is connected to a dry charcoal bunker 132 for storing cooled dry charcoal. In addition, a dry coal cyclone 133 and a dry coal electric dust collector 134 are connected to the fluidized bed dryer 1 as a dust collector 139 for separating dry coal particles from steam discharged to the outside. The dry coal particles separated from the steam in the dry coal cyclone 133 and the dry coal electrostatic precipitator 134 are stored in the dry coal bunker 132. Note that the steam from which the dry coal is separated by the dry coal electrostatic precipitator 134 is compressed by the steam compressor 135 and then supplied to the heat transfer tube 33 of the fluidized bed drying apparatus 1 as a heat medium.

  The pulverized coal machine 113 produces pulverized coal by pulverizing lignite (dried coal) dried by the fluidized bed drying apparatus 1 into fine particles. In other words, when the dry coal stored in the dry coal bunker 132 is dropped by the coal feeder 136, the pulverized coal machine 113 converts the dry coal into pulverized coal having a predetermined particle size or less. The pulverized coal after being pulverized by the pulverized coal machine 113 is separated from the conveying gas by the pulverized coal bag filters 137a and 137b and stored in the pulverized coal supply hoppers 138a and 138b.

  The coal gasifier 114 is supplied with pulverized coal processed by the pulverized coal machine 113 and supplied with char (unburned coal) recovered by the char recovery device 115.

  The coal gasification furnace 114 is connected to a compressed air supply line 141 from a gas turbine facility 117 (compressor 161), and can supply compressed air compressed by the gas turbine facility 117. The air separation device 142 separates and generates nitrogen and oxygen from air in the atmosphere. A first nitrogen supply line 143 is connected to the coal gasifier 114, and a pulverized coal supply hopper is connected to the first nitrogen supply line 143. Charging lines 144a and 144b from 138a and 138b are connected. The second nitrogen supply line 145 is also connected to the coal gasifier 114, and the char return line 146 from the char recovery device 115 is connected to the second nitrogen supply line 145. Further, the oxygen supply line 147 is connected to the compressed air supply line 141. In this case, nitrogen is used as a carrier gas for coal and char, and oxygen is used as an oxidant.

  The coal gasification furnace 114 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. Note that the coal gasification furnace 114 is provided with a foreign matter removing device 148 that removes foreign matter mixed with pulverized coal. In this case, the coal gasification furnace 114 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 114 is provided with a gas generation line 149 for combustible gas toward the char recovery device 115, and can discharge combustible gas containing char. In this case, by providing a gas cooler in the gas generation line 149, the combustible gas may be cooled to a predetermined temperature and then supplied to the char recovery device 115.

  The char recovery device 115 includes a dust collector 151 and a supply hopper 152. In this case, the dust collector 151 is constituted by one or a plurality of bag filters or cyclones, and can separate the char contained in the combustible gas generated in the coal gasification furnace 114. The combustible gas from which the char has been separated is sent to the gas purifier 116 through the gas discharge line 153. The supply hopper 152 stores the char separated from the combustible gas by the dust collector 151. A bin may be disposed between the dust collector 151 and the supply hopper 152, and a plurality of supply hoppers 152 may be connected to the bin. A char return line 146 from the supply hopper 152 is connected to the second nitrogen supply line 145.

The gas purification device 116 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 115. The gas purifier 116 purifies the combustible gas to produce fuel gas, and supplies it to the gas turbine equipment 117. In this gas purifier 116, 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 117 includes a compressor 161, a combustor 162, and a turbine 163, and the compressor 161 and the turbine 163 are connected by a rotating shaft 164. The combustor 162 has a compressed air supply line 165 connected from the compressor 161, a fuel gas supply line 166 connected from the gas purification device 116, and a combustion gas supply line 167 connected to the turbine 163. Further, the gas turbine equipment 117 is provided with a compressed air supply line 141 extending from the compressor 161 to the coal gasification furnace 114, and a booster 168 is interposed in the compressed air supply line 141. Therefore, in the combustor 162, the compressed air supplied from the compressor 161 and the fuel gas supplied from the gas purifier 116 are mixed and burned, and the rotating shaft 164 is rotated by the generated combustion gas in the turbine 163. By doing so, the generator 119 can be driven.

  The steam turbine equipment 118 has a turbine 169 connected to the rotating shaft 164 in the gas turbine equipment 117, and the generator 119 is connected to the base end portion of the rotating shaft 164. The exhaust heat recovery boiler 120 is provided in the exhaust gas line 170 from the gas turbine equipment 117 (the turbine 163), and generates steam by exchanging heat between air and high-temperature exhaust gas. Therefore, the exhaust heat recovery boiler 120 is provided with a steam supply line 171 and a steam recovery line 172 between the turbine 169 of the steam turbine equipment 118, and a condenser 173 is provided in the steam recovery line 172. Yes. Therefore, in the steam turbine equipment 118, the turbine 169 is driven by the steam supplied from the exhaust heat recovery boiler 120, and the generator 119 can be driven by rotating the rotating shaft 164.

  The exhaust gas from which heat has been recovered by the exhaust heat recovery boiler 120 is removed of harmful substances by the gas purification device 174, and the purified exhaust gas is discharged from the chimney 175 to the atmosphere.

  Here, the action | operation of the coal gasification combined cycle power generation equipment 100 of Example 1 is demonstrated.

  In the combined coal gasification combined power generation facility 100 of the first embodiment, raw coal (brown coal) is stored in the raw coal bunker 121 by the coal feeder 111, and the lignite in the raw coal bunker 121 is crushed by the coal feeder 122. It is dropped to 123, where it is crushed to a predetermined size. The crushed lignite is fed into the fluidized bed drying device 1 after the non-condensable gas is exhausted in the exhaust device 8. The input lignite is heated and dried by the fluidized bed drying apparatus 1, cooled by the cooler 131, and stored in the dry coal bunker 132. The steam discharged from the fluidized bed drying apparatus 1 is separated into dry coal particles by the dried coal cyclone 133 and the dried coal electric dust collector 134 and compressed by the steam compressor 135, and then the heat transfer tube of the fluidized bed drying apparatus 1. 33 is returned as a heating medium. On the other hand, dry coal particles separated from the steam are stored in the dry coal bunker 132.

  The dry coal stored in the dry coal bunker 132 is supplied to the pulverized coal machine 113 by the coal feeder 136, where it is pulverized into fine particles to produce pulverized coal, and the pulverized coal bag filters 137a and 137b are used. And stored in pulverized coal supply hoppers 138a and 138b. The pulverized coal stored in the pulverized coal supply hoppers 138 a and 138 b is supplied to the coal gasification furnace 114 through the first nitrogen supply line 143 by nitrogen supplied from the air separation device 142. Further, the char recovered by the char recovery device 115 described later is supplied to the coal gasifier 114 through the second nitrogen supply line 145 by nitrogen supplied from the air separation device 142. Further, compressed air extracted from a gas turbine facility 117 described later is boosted by a booster 168 and then supplied to the coal gasifier 114 through the compressed air supply line 141 together with oxygen supplied from the air separation device 142.

  In the coal gasification furnace 114, the supplied pulverized coal and char are combusted by compressed air (oxygen), and the pulverized coal and char are gasified, so that combustible gas (coal gas) mainly containing carbon dioxide is obtained. Can be generated. This combustible gas is discharged from the coal gasifier 114 through the gas generation line 149 and sent to the char recovery device 115.

  In the char recovery device 115, the combustible gas is first supplied to the dust collector 151, and the dust collector 151 separates the char contained in the combustible gas. The combustible gas from which the char has been separated is sent to the gas purifier 116 through the gas discharge line 153. On the other hand, the fine char separated from the combustible gas is deposited on the supply hopper 152, returned to the coal gasifier 114 through the char return line 146, and recycled.

  The combustible gas from which the char has been separated by the char recovery device 115 is gas purified by removing impurities such as sulfur compounds and nitrogen compounds by the gas purification device 116 to produce fuel gas. In the gas turbine equipment 117, when the compressor 161 generates compressed air and supplies the compressed air to the combustor 162, the combustor 162 is supplied from the compressed air supplied from the compressor 161 and the gas purifier 116. Combustion gas is generated by mixing with fuel gas and combusting, and the turbine 163 is driven by this combustion gas, so that the generator 119 is driven via the rotating shaft 164 to generate power.

  The exhaust gas discharged from the turbine 163 in the gas turbine facility 117 generates steam by exchanging heat with air in the exhaust heat recovery boiler 120, and supplies the generated steam to the steam turbine facility 118. . In the steam turbine equipment 118, the turbine 169 is driven by the steam supplied from the exhaust heat recovery boiler 120, whereby the generator 119 can be driven via the rotating shaft 164 to generate power.

  Thereafter, in the gas purification device 174, harmful substances in the exhaust gas discharged from the exhaust heat recovery boiler 120 are removed, and the purified exhaust gas is released from the chimney 175 to the atmosphere.

  Hereinafter, the exhaust device 8 provided in the coal gasification combined power generation facility 100 described above will be described in detail. FIG. 2 is a schematic configuration diagram schematically illustrating the exhaust device according to the first embodiment. The exhaust device 8 of Example 1 exhausts the non-condensable gas mixed with the lignite supplied by the coal supply device 111. First, the fluidized bed drying device 1 connected to the exhaust device 8 will be described.

  As shown in FIG. 2, the fluidized bed drying apparatus 1 includes a drying furnace 5 in which lignite is supplied and a gas dispersion plate 6 provided inside the drying furnace 5. The drying furnace 5 is formed in a rectangular box shape. The gas dispersion plate 6 divides the space inside the drying furnace 5 into a wind chamber 11 located on the lower side in the vertical direction (lower side in the drawing) and a drying chamber 12 located on the upper side in the vertical direction (upper side in the drawing). Yes. A number of through holes are formed in the gas dispersion plate 6, and fluidized steam is introduced into the wind chamber 11.

  The drying chamber 12 of the drying furnace 5 discharges brown coal input 31 for introducing lignite, dry coal discharge 34 for discharging dry coal obtained by heating and drying lignite, fluidized steam and generated steam generated during drying. A steam discharge port 35 and a heat transfer tube 33 for heating the brown coal are provided.

  The brown coal inlet 31 is formed on one end side (the left side in the drawing) of the drying chamber 12. The exhaust apparatus 8 is connected to the lignite charging port 31, and the lignite supplied from the coal supply apparatus 111 and passing through the exhaust apparatus 8 is supplied to the drying chamber 12.

  The dry charcoal discharge port 34 is formed in the lower part of the other end side (the right side in the drawing) of the drying chamber 12. From the dry charcoal discharge port 34, the lignite dried in the drying chamber 12 is discharged as dry charcoal, and the discharged dry charcoal is supplied toward the cooler 131 described above.

  The steam discharge port 35 is formed on the upper surface on the other end side of the drying chamber 12. The steam discharge port 35 discharges the generated steam generated by heating the wet fuel together with the fluidized steam supplied to the drying chamber 12 when the lignite is dried. The fluidized steam and generated steam discharged from the steam discharge port 35 are supplied to the dust collector 139 and then supplied to the steam compressor 135.

  The heat transfer tube 33 is configured in a panel shape and is provided inside the fluidized bed 3. The heat transfer pipe 33 is connected to the outflow side of the steam compressor 135, and the steam compressed by the steam compressor 135 is supplied into the pipe as drying steam. For this reason, when the steam for drying is supplied into the pipe, the heat transfer pipe 33 uses the latent heat of the steam for drying to heat the lignite in the fluidized bed 3, thereby removing moisture in the lignite in the fluidized bed 3. By removing, the lignite in the drying chamber 12 is dried. Thereafter, the drying steam used for drying is discharged to the outside of the drying chamber 12.

  Therefore, the lignite supplied to the drying chamber 12 via the lignite charging port 31 flows by the fluidized steam supplied via the gas dispersion plate 6, thereby forming the fluidized bed 3 in the drying chamber 12. The free board portion F is formed above the fluidized bed 3. The flow direction of the fluidized bed 3 formed in the drying chamber 12 is a direction from one end side to the other end side of the drying chamber 12. And the lignite which became the fluidized bed 3 is heated by the heat transfer tube 33, whereby the moisture contained in the lignite becomes generated steam and is discharged from the steam outlet 35 together with the fluidized steam. The steam discharged from the steam outlet 35 is supplied to the steam compressor 135 after the dry coal particles contained in the steam are collected by the dust collector 139 and compressed by the steam compressor 135 to rise. Be warmed. The heated steam is supplied to the heat transfer tube 33 as drying steam and heats the lignite using latent heat.

  The exhaust device 8 is provided between the coal supply device 111 and the fluidized bed drying device 1. The exhaust device 8 has a fuel storage hopper (fuel storage unit) 41 that stores lignite supplied from the coal supply device 111. The fuel storage hopper 41 has one side (upper side in the figure) connected to the coal feeder 111 via the first fuel supply line L1, and the other side (lower side in the figure) flows via the second fuel supply line L2. It is connected to the layer drying apparatus 1. Further, the exhaust device 8 has a first rotary feeder 44 interposed in the first fuel supply line L1 and a second rotary feeder 45 interposed in the second fuel supply line L2. The first rotary feeder 44 operates to supply lignite to the fuel storage hopper 41 from the coal feeder 111. On the other hand, the first rotary feeder 44 functions as a partition that closes the first fuel supply line L <b> 1 and partitions between the coal supply device 111 and the fuel storage hopper 41 by stopping the operation. Similarly, the second rotary feeder 45 operates to supply lignite from the fuel storage hopper 41 toward the fluidized bed drying apparatus 1. On the other hand, the second rotary feeder 45 functions as a partition that closes the second fuel supply line L2 and partitions between the fuel storage hopper 41 and the fluidized bed drying device 1 by stopping the operation. In addition, the partition by the 1st rotary feeder 44 and the 2nd rotary feeder 45 does not require sealing performance.

  The fuel storage hopper 41 has a steam supply line (steam supply unit) L3 connected to the lower portion thereof, and a gas discharge line (gas discharge portion) L4 connected to the upper portion thereof. The steam supply line L <b> 3 supplies steam toward the inside of the fuel storage hopper 41. The steam supplied to the steam supply line L3 is supplied from, for example, an external auxiliary steam supply device. Further, it is also possible to partially extract and supply steam with a reduced concentration of the non-condensable gas in the drying furnace 5 after operation for a certain period of time from the outlet of the compressor 135. The gas discharge line L4 can discharge a non-condensable gas such as nitrogen inside the fuel storage hopper 41. That is, the gas discharge line L4 discharges the non-condensable gas inside the fuel storage hopper 41 by the amount of steam supplied into the fuel storage hopper 41 by the steam supply line L3. The steam supply line L3 and the gas discharge line L4 function as a gas exhaust unit that exhausts the non-condensable gas in the fuel storage hopper 41. The noncondensable gas discharged from the gas discharge line L4 is effectively used as various heat sources.

  Therefore, in the exhaust device 8 configured as described above, the operation of the second rotary feeder 45 is stopped, while the first rotary feeder 44 is operated, whereby lignite is supplied from the coal supply device 111 to the fuel storage hopper 41. Supply. The supplied lignite is stored in the fuel storage hopper 41 (fuel storage step). Thereafter, the exhaust device 8 partitions the first fuel supply line L1 and the second fuel supply line L2 by stopping the operation of the first rotary feeder 44 and the second rotary feeder 45, thereby the fuel storage hopper. It is set as the state which isolated the lignite in 41 (fuel isolation process). Then, steam is supplied into the fuel storage hopper 41 from the steam supply line L3. Then, the non-condensable gas inside the fuel storage hopper 41 is filled with the vapor while the non-condensable gas inside is exhausted from the gas discharge line L4. For this reason, when the fuel storage hopper 41 is filled with the steam, the non-condensable gas is replaced with the steam, whereby the non-condensable gas in the fuel storage hopper 41 is exhausted (exhaust process). At this time, when steam is supplied to the fuel storage hopper 41 through the steam supply line L3, the lignite stored in the fuel storage hopper 41 is preheated while flowing by the steam. Thereafter, the exhaust device 200 operates the second rotary feeder 45 to supply lignite from the fuel storage hopper 41 to the fluidized bed drying device 1.

  Next, referring to FIG. 3 and FIG. 4, the quality of the drying steam flowing through the heat transfer pipe 33 of the conventional fluidized bed drying apparatus 1 to which the exhaust apparatus 8 is not connected, and the implementation in which the exhaust apparatus 8 is connected. The quality of the drying steam flowing through the heat transfer tube 33 of the fluidized bed drying apparatus 1 of Example 1 is compared. FIG. 3 is a graph relating to the quality of drying steam in a conventional fluidized bed drying apparatus. FIG. 4 is a graph relating to the quality of the drying steam in the fluidized bed drying apparatus according to the first embodiment.

  In the graphs shown in FIGS. 3 and 4, the horizontal axis represents the quality of the drying steam, and the vertical axis represents the temperature of the drying steam. The quality is the ratio of vapor in the vapor phase to the total amount of vapor, and the lower the quality, the smaller the ratio of vapor in the vapor phase and the higher the ratio of liquid vapor.

  In the graph of FIG. 3, since the exhaust device 8 is not connected, the mixing ratio of the non-condensable gas contained in the atmosphere in the drying furnace 5 is 5 wt%. On the other hand, in the graph of FIG. 4, since the exhaust device 8 is connected, the mixing ratio of the non-condensable gas contained in the atmosphere in the drying furnace 5 is 1 wt%. At this time, in FIGS. 3 and 4, the pressure of the atmosphere in the drying furnace 5 is 0.1 MPa, and the dew point temperature T1 in the drying furnace 5 is about 100 ° C. Since the dew point temperature T1 in the drying furnace 5 is around 100 ° C., the temperature T2 of the drying steam supplied to the heat transfer tube 33 is 100 ° C. or more, and the dew point temperature T1 and the drying steam (heat transfer tube) 33) is a predetermined temperature difference ΔT.

  Further, in FIG. 3, the steam discharged from the drying furnace 5 is recompressed by the steam compressor 135 and supplied to the heat transfer tube 33, so that the non-condensable property contained in the drying steam flowing through the heat transfer tube 33. The gas mixing rate is 5 wt%. Similarly, in FIG. 4, since the steam discharged from the drying furnace 5 is recompressed by the steam compressor 135 and supplied to the heat transfer pipe 33, the steam contained in the drying steam flowing through the heat transfer pipe 33 is not included. The mixing rate of the condensable gas is 1 wt%. At this time, the pressure in the heat transfer tube 33 through which the drying steam shown in FIGS. 3 and 4 flows is 0.49 MPa.

  As shown in FIG. 3, in the conventional fluidized bed drying apparatus 1, since the mixing rate of the non-condensable gas in the drying steam is high, the quality of the drying steam supplied to the heat transfer tube 33 is smaller than 0.2. As a result, the proportion of the non-condensable gas in the vapor phase of the drying vapor is increased. For this reason, the temperature T2 of the drying steam in the low quality region is rapidly reduced, the temperature difference ΔT is also reduced, and it is difficult to recover the latent heat. Thereby, in the conventional fluidized bed drying apparatus 1, it becomes difficult to use the drying steam having a quality lower than 0.2.

  On the other hand, as shown in FIG. 4, in the fluidized bed drying apparatus 1 of Example 1, since the mixing rate of the non-condensable gas in the drying steam is low, the quality of the drying steam supplied to the heat transfer tube 33 is 0. Even if it becomes smaller than .2, the proportion of the non-condensable gas in the vapor phase of the drying steam is reduced as compared with the conventional case. For this reason, since it is possible to suppress a rapid decrease in the temperature T2 of the drying steam and to secure the temperature difference ΔT, the fluidized bed drying apparatus 1 of Example 1 uses lower-quality drying steam than in the past. Is possible. In addition, in the fluidized bed drying apparatus 1 of Example 1, if the quality of the drying steam is 0.1 or more, a decrease in the temperature T2 of the drying steam can be suppressed, and the latent heat of the drying steam is efficiently recovered. It becomes possible.

  As described above, according to the configuration of the first embodiment, the exhaust device 8 exhausts the non-condensable gas mixed with the lignite in a state where the first fuel supply line L1 and the second fuel supply line L2 are partitioned. be able to. For this reason, the exhaust apparatus 8 can supply lignite to the fluidized bed drying apparatus 1 while suppressing the mixing of non-condensable gas. Thereby, since the vapor | steam discharged | emitted from the fluidized bed drying apparatus 1 can be made into the thing with little mixing amount of non-condensable gas, even if the drying vapor | steam recompressed becomes low quality, it is for drying The temperature drop of the steam can be suppressed, and the latent heat of the drying steam can be efficiently recovered.

  Moreover, according to the structure of Example 1, the exhaust apparatus 8 can pre-heat the brown coal stored in the fuel storage hopper 41 with the steam supplied from the steam supply line L3. For this reason, since the preheated lignite can be supplied to the fluidized bed drying device 1, the recondensation of the steam can be suppressed on the supply side of the fluidized bed drying device 1, and the lignite coalesces by the condensed water and flows. Occurrence of poor formation can be suppressed.

  Further, according to the configuration of the first embodiment, the exhaust device 8 stores lignite in the fuel storage hopper 41, and the first fuel supply line L <b> 1 and the second fuel supply by the first rotary feeder 44 and the second rotary feeder 45. With the lines L2 partitioned, the steam is supplied from the steam supply line L3 into the fuel storage hopper 41, and the non-condensable gas in the fuel storage hopper 41 is discharged from the gas discharge line L4. The non-condensable gas inside can be suitably exhausted.

  Next, an exhaust device 200 according to the second embodiment will be described with reference to FIG. FIG. 5 is a schematic configuration diagram schematically illustrating the exhaust device according to the second embodiment. In the second embodiment, parts that are different from the first embodiment will be described in order to avoid duplicated descriptions, and parts that have the same configuration as the first embodiment are denoted by the same reference numerals. In the exhaust device 200 according to the second embodiment, an intake device (gas intake portion) 201 is interposed in the gas discharge line L4 of the first embodiment. Hereinafter, the exhaust device 200 according to the second embodiment will be described.

  In the exhaust device 200 of the second embodiment, the intake device 201 interposed in the gas discharge line L4 sucks the non-condensable gas in the fuel storage hopper 41, and the sucked non-condensable gas in the fuel storage hopper 41. Exhaust to the outside. The steam supply line L3, the atmosphere discharge line L4, and the intake device 201 function as a gas exhaust unit that exhausts the non-condensable gas in the fuel storage hopper 41.

  Therefore, in the exhaust device 200 configured as described above, the operation of the second rotary feeder 45 is stopped, while the first rotary feeder 44 is operated, whereby lignite is supplied from the coal supply device 111 to the fuel storage hopper 41. Supply. The supplied lignite is stored in the fuel storage hopper 41 (fuel storage step). Thereafter, the exhaust device 200 divides the first fuel supply line L1 and the second fuel supply line L2 by stopping the operation of the first rotary feeder 44 and the second rotary feeder 45, thereby the fuel storage hopper. It is set as the state which isolated the lignite in 41 (fuel isolation process). In this state, the intake device 201 sucks the non-condensable gas inside the fuel storage hopper 41 to exhaust the non-condensable gas in the fuel storage hopper 41 via the gas discharge line L4 (exhaust process). .

  When the non-condensable gas inside the fuel storage hopper 41 is sucked by the intake device 201, the inside of the fuel storage hopper 41 becomes a negative pressure. For this reason, steam is supplied from the steam supply line L3 to the fuel storage hopper 41 to equalize the pressure in the fuel storage hopper 41 and the fluidized bed drying device 1, thereby fluidizing and drying the lignite in the fuel storage hopper 41. It can be fed into the device 1. Further, the fuel storage hopper 41 is filled with the non-condensable gas therein. Thereby, the exhaust device 200 can suppress the inflow of the non-condensable gas into the fuel storage hopper 41. Thereafter, the exhaust device 200 operates the second rotary feeder 45 to supply lignite from the fuel storage hopper 41 to the fluidized bed drying device 1.

  As described above, also in the configuration of the second embodiment, the exhaust device 200 exhausts the non-condensable gas mixed with the lignite in a state where the first fuel supply line L1 and the second fuel supply line L2 are partitioned. Can do. Thereby, the exhaust device 200 can suppress the mixing of non-condensable gas, and even if the drying steam becomes low quality, it can suppress the temperature drop of the drying steam, and the latent heat of the drying steam is efficiently It can be recovered well.

  Further, according to the configuration of the second embodiment, the exhaust device 200 stores lignite in the fuel storage hopper 41, and the first fuel supply line L <b> 1 and the second fuel supply by the first rotary feeder 44 and the second rotary feeder 45. In the state where the lines L2 are partitioned, the intake device 201 sucks non-condensable gas in the fuel storage hopper 41 from the gas discharge line L4, and then supplies steam from the steam supply line L3 into the fuel storage hopper 41. The non-condensable gas in the fuel storage hopper 41 can be suitably exhausted.

  In the second embodiment, it is preferable that the first rotary feeder 44 and the second rotary feeder 45 have high sealing properties.

  Next, an exhaust device 210 according to Embodiment 3 will be described with reference to FIG. FIG. 6 is a schematic configuration diagram schematically illustrating the exhaust device according to the third embodiment. In the third embodiment, portions that are different from the second embodiment will be described in order to avoid redundant descriptions, and portions that have the same configuration as the second embodiment are denoted by the same reference numerals. In the exhaust device 200 according to the second embodiment, the intake device 201 is interposed in the gas discharge line L4 of the first embodiment. In the exhaust device 210 according to the third embodiment, the steam supply line L3 is eliminated, and a first ball valve 211 and a second ball valve 212 are provided instead of the first rotary feeder 44 and the second rotary feeder 45. Hereinafter, the exhaust device 210 according to the third embodiment will be described.

  In the exhaust device 210 of the third embodiment, the first ball valve 211 and the second ball valve 212 (partition part) are a kind of on-off valves, and when opened, the first fuel supply line L1 and the second fuel supply line. The distribution of L2 lignite is allowed. On the other hand, the first ball valve 211 and the second ball valve 212 close the first fuel supply line L1 and the second fuel supply line L2, respectively, when the valves are closed. Thereby, by closing the 1st ball valve 211 and the 2nd ball valve 212, the 1st fuel supply line L1 and the 2nd fuel supply line L2 can be partitioned, respectively, and lignite in the fuel storage hopper 41 is isolated. It can be in the state. At this time, the first ball valve 211 and the second ball valve 212 are highly sealed. Note that the intake device 201 is the same as that of the second embodiment, and thus the description thereof is omitted. The gas discharge line L4 and the intake device 201 function as a gas exhaust unit that exhausts the non-condensable gas in the fuel storage hopper 41.

  Therefore, in the exhaust device 210 configured as described above, the second ball valve 212 is closed while the first ball valve 211 is opened, whereby brown coal is supplied from the coal supply device 111 to the fuel storage hopper 41. Supply. The supplied lignite is stored in the fuel storage hopper 41 (fuel storage step). Thereafter, the exhaust device 210 divides the first fuel supply line L1 and the second fuel supply line L2 by closing the first ball valve 211 and the second ball valve 212, whereby the fuel storage hopper is divided. It is set as the state which isolated the lignite in 41 (fuel isolation process). In this state, the intake device 201 sucks the non-condensable gas inside the fuel storage hopper 41 to exhaust the non-condensable gas in the fuel storage hopper 41 via the gas discharge line L4 (exhaust process). . Thereafter, when the second ball valve 212 is opened, the exhaust device 210 supplies lignite to the fluidized bed drying device 1 from the fuel storage hopper 41.

  As described above, also in the configuration of the third embodiment, the exhaust device 210 exhausts the non-condensable gas mixed with the lignite in a state where the first fuel supply line L1 and the second fuel supply line L2 are partitioned. Can do. As a result, the exhaust device 210 can suppress the mixing of non-condensable gas, and even if the drying steam becomes low quality, it can suppress the temperature drop of the drying steam, and the drying steam has an efficient latent heat. It can be recovered well.

  Further, according to the configuration of the third embodiment, the exhaust device 210 stores lignite in the fuel storage hopper 41, and the first fuel supply line L <b> 1 and the second fuel supply by the first ball valve 211 and the second ball valve 212. With the lines L2 partitioned, the non-condensable gas in the fuel storage hopper 41 is preferably exhausted by sucking the non-condensable gas in the fuel storage hopper 41 from the gas discharge line L4 by the intake device 201. Can do.

  In the exhaust devices 8, 200, and 210 of the first to third embodiments, the first rotary feeder 44 and the second rotary feeder 45, or the first ball valve 211 and the second ball valve 212 are used as a plurality of partitions. Although applied, it is not limited to this configuration. In other words, any one can partition the first fuel supply line L1 and the second fuel supply line L2 while permitting the flow of lignite in the first fuel supply line L1 and the second fuel supply line L2. May be.

DESCRIPTION OF SYMBOLS 1 Fluidized bed drying apparatus 3 Fluidized bed 5 Drying furnace 6 Gas dispersion plate 8 Exhaust device 11 Wind chamber 12 Drying chamber 31 Brown coal inlet 33 Heat transfer pipe 34 Dry coal outlet 35 Steam outlet 41 Fuel storage hopper 44 First rotary feeder 45 Second rotary feeder 200 Exhaust device (Example 2)
201 Intake device 210 Exhaust device (Example 3)
211 First ball valve 212 Second ball valve L1 First fuel supply line L2 Second fuel supply line L3 Steam supply line L4 Gas exhaust line F Free board section

Claims (6)

  Provided between a fluidized bed drying device capable of drying the wet fuel while fluidizing the wet fuel with fluidized steam, and a fuel supply device capable of supplying the wet fuel toward the fluidized bed drying device, Non-condensable gas exhausted together with the wet fuel supplied from the fuel supply device in a state where the fuel supply device and the fluidized bed drying device are separated from each other Sex gas exhaust system. A fuel storage section for storing the wet fuel supplied from the fuel supply device;
A plurality of partition portions respectively provided between the fuel supply device and the fuel storage portion and between the fuel storage portion and the fluidized bed drying device;
2. The non-condensable gas exhaust device according to claim 1, further comprising a gas exhaust unit that exhausts the non-condensable gas in the fuel storage unit. The gas exhaust part is
A steam supply section for supplying steam into the fuel storage section;
The exhaust device for non-condensable gas according to claim 2, further comprising: a gas discharge unit that discharges the non-condensable gas in the fuel storage unit. The gas exhaust part is
4. The non-condensable gas exhaust device according to claim 2, further comprising a gas intake unit configured to intake the non-condensable gas in the fuel storage unit. 5. A fluidized bed drying device capable of drying the wet fuel while fluidizing the wet fuel with fluidized steam;
A fuel supply device capable of supplying the wet fuel toward the fluidized bed drying device;
The exhaust device for non-condensable gas according to any one of claims 1 to 4, provided between the fluidized bed drying device and the fuel supply device;
A gasification furnace that processes the wet fuel after drying supplied from the fluidized bed drying device and converts it into gasification gas;
A gas turbine operated using the gasified gas as fuel;
A steam turbine operated by steam generated by an exhaust heat recovery boiler that introduces turbine exhaust gas from the gas turbine;
A gasification combined power generation facility comprising the gas turbine and a generator connected to the steam turbine. A fuel storage step for storing the supplied wet fuel;
A fuel isolation step for isolating the wet fuel after execution of the fuel storage step;
An exhaust process for exhausting the non-condensable gas mixed with the supply of the wet fuel after the execution of the fuel isolation process.

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