JP6459297B2 - Drying equipment - Google Patents

Description

  The present invention relates to a drying apparatus that dries a hydrated material, for example, low-grade coal such as high moisture-containing biomass or lignite containing a large amount of moisture.

  In recent years, it has been required to use a high moisture content biomass or a water content such as a low grade coal such as a high moisture content lignite as a fuel for a boiler.

  When using hydrated products as boiler fuel, the amount of water brought into the furnace is large, so energy is consumed to evaporate the moisture in the hydrated product, and the temperature inside the furnace decreases due to water vapor evaporated from the hydrated products. However, there is a problem that the efficiency of the boiler is lowered.

  For this reason, when using a hydrated product as a fuel for a boiler, a drying device is provided, and the hydrated product is dried while flowing the hydrated product through a fluid medium in the drying device, and dried in advance to remove the moisture hydrated product. Things need to be supplied to the furnace.

  However, in the conventional drying apparatus, since the fluid medium is uniformly supplied according to the water-containing material that is difficult to flow, the fluid medium is supplied more than necessary, and the energy consumption increases and the particle size is small. There was a problem that scattering of water-containing materials increased.

  In Patent Document 1, a drying container is divided into an upper drying chamber and a lower chamber chamber by a gas dispersion plate, and the drying chamber is divided into five drying compartments by four dividing plates. The fluidized gas introduced from the fluidized gas supply section provided in the flow into the dry compartment through the gas dispersion plate, a fluidized bed of lignite is formed in the dry compartment, the fluidized bed Fluidized bed drying apparatus, fluidized bed drying equipment, and wet raw material drying method that are sequentially dried by being heated by a heat transfer member provided for each drying compartment in the process of moving over the dividing plate to the adjacent drying compartment Is disclosed.

JP 2012-215316 A

  In view of such circumstances, the present invention provides a drying apparatus that improves the fluidity of a hydrated product and improves the drying efficiency.

  The present invention discharges the hydrated material dried from the drying chamber in which the hydrated material is dried, the hydrated material supply means for supplying the hydrated material from one end of the drying chamber, and the other end of the drying chamber. Discharging means, heating means provided in the drying chamber, exhaust means for exhausting steam generated by heating from the other end of the drying chamber, and liquefying the hydrated matter by ejecting a fluid medium into the drying chamber Dividing the drying chamber into a plurality of drying compartments, and allowing the adjacent drying compartments to communicate with each other at the upper or lower part so that the hydrated material flows while reversing up and down between the drying compartments. And the fluid medium supply means has a wind box formed at the bottom of the drying chamber, and the window box is divided corresponding to each drying compartment, and the window box is divided for each divided window box. Fluid medium is supplied The supply amount of the fluidized medium with respect to the dry compartment where the hydrous material flows downwards, the hydrate is related to the drying apparatus be less than the supply amount of the fluidized medium with respect to the dry compartment to flow upward.

  The present invention further includes a pressure gauge for detecting the pressure in each drying compartment and a control section, and the control section supplies the flow medium to each wind box based on the detection result of the pressure gauge. The present invention relates to a drying device that controls

  Further, according to the present invention, in the drying chamber, a heating region is formed by a plurality of drying compartments on the upstream side, a cooling region is formed by a plurality of drying compartments on the downstream side, and each window corresponding to each drying compartment in the heating region. The present invention relates to a drying apparatus in which steam is supplied for each box, and cooling air is supplied for each wind box corresponding to each drying compartment in the cooling region.

  According to the present invention, there is provided a drying chamber in which the hydrated product is dried, a hydrated product supplying means for supplying the hydrated product from one end of the drying chamber, and the hydrated product dried from the other end of the drying chamber. A discharge means for discharging, a heating means provided in the drying chamber, an exhaust means for exhausting steam generated by heating from the other end of the drying chamber, a fluid medium is ejected into the drying chamber, and the hydrated material is discharged. A plurality of fluid medium supply means for liquefaction and the drying chamber divided into a plurality of drying compartments, and the adjacent drying compartments communicate with each other at the upper part or the lower part so that the hydrated material flows while reversing between the drying compartments. The fluid medium supply means has a wind box formed at the bottom of the drying chamber, and the window box is divided corresponding to each drying compartment, and each divided wind box Is provided with the fluid medium. And the amount of the fluid medium supplied to the dry compartment in which the water content flows downward is less than the amount of fluid medium supplied to the dry compartment in which the water content flows upward. The fluid medium having an optimal flow rate can be supplied in accordance with the fluidity, and the fluidity of the hydrated material can be improved and the drying efficiency can be improved.

It is the schematic which shows the boiler apparatus with which the drying apparatus which concerns on the Example of this invention is applied. It is the schematic which shows the hydrated matter drying system with which the drying apparatus which concerns on the Example of this invention is applied. It is the schematic which shows the drying apparatus which concerns on the Example of this invention. It is a graph which shows the relationship between the bed pressure loss and the fluid medium flow rate in the drying apparatus which concerns on the Example of this invention.

  Embodiments of the present invention will be described below with reference to the drawings.

  First, referring to FIG. 1, a boiler device 1 to which a hydrated matter drying system according to an embodiment of the present invention is applied will be described.

  In FIG. 1, 2 indicates a furnace of the boiler device 1, and 3 indicates a burner provided on the furnace wall of the furnace 2. The furnace wall of the furnace 2 is provided with a heat transfer tube (not shown) for absorbing radiant heat from the inside of the furnace, and a super heater (superheated steam generation) for heating the generated steam above the furnace 2. 4) is provided.

  In FIG. 1, reference numeral 5 denotes a hydrated material drying system for drying hydrated materials such as biomass and low-grade coal, such as lignite, and when lignite 6 containing moisture is supplied to the hydrated material drying system 5. The hydrated coal drying system 5 dries the lignite 6 and supplies it as the dried lignite 7 to the burner 3.

  By supplying the dry lignite 7 to the burner 3, the dry lignite 7 is burned in the burner 3, and a flame is formed in the furnace 2. The combustion exhaust gas 8 generated by the combustion heats the inside of the furnace 2 and exchanges heat with the super heater 4 to be exhausted through the flue 9.

  Next, referring to FIG. 2, the hydrated material drying system 5 according to an embodiment of the present invention will be described.

  In FIG. 2, 11 indicates a pulverizer such as a hammer mill that pulverizes the lignite 6 to a predetermined particle size, for example, 2 mm or less, and 12 indicates a drying device. The drying device 12 is pulverized inside. A drying chamber 13 for drying the lignite 6 and cooling it after drying is formed.

  The drying chamber 13 has a heating region 14 formed on the upstream side and a cooling region 15 formed on the downstream side, and the heating region 14 heats the lignite 6 to dry it, and The region 15 cools the dried lignite 7 heated and dried in the heating region 14.

  A lignite supply line 16 for the lignite 6 is connected to an upper portion of the side wall of the drying chamber 13 on the heating region 14 side, and the pulverizer 11 is provided in the middle of the lignite supply line 16, downstream of the pulverizer 11. On the side, a brown coal hopper 17 is provided. The lignite hopper 17, the pulverizer 11, and the lignite supply line 16 constitute a hydrated material supply means.

  An exhaust line 19 as exhaust means is connected to a portion of the top plate 18 of the drying chamber 13 corresponding to the cooling region 15, that is, on the opposite side of the drying chamber 13 to the lignite supply line 16.

  A lignite discharge line 21 is connected to the side wall of the drying chamber 13 on the cooling region 15 side, and the lignite discharge line 21 is connected to the burner 3.

  A heating side wind box 23 is provided below the bottom plate 22 on the heating region 14 side of the drying chamber 13, and a plurality of steam supply nozzles 24 are provided on the bottom plate 22. A fluid medium such as high-temperature bubbling steam 25 is introduced from the steam supply nozzle 24 through a hole (not shown). A cooling side wind box 26 is provided below the bottom plate 22 on the cooling region 15 side, and a plurality of cooling air supply nozzles 27 are provided on the bottom plate 22. A fluid medium such as cooling air 28 is introduced from the cooling air supply nozzle 27 through a hole (not shown).

  Further, by supplying the bubbling steam 25 and the cooling air 28 to the lignite 6 supplied from the pulverizer 11 via the lignite hopper 17, the lignite powder becomes the bubbling steam 25 and the cooling air 28. A fluidized bed 29 is formed in the drying chamber 13 by the lignite powder that has been floated, liquefied, and liquefied.

  The heating region 14 in the fluidized bed 29 is provided with a large number of heat transfer tubes 31 (only one is shown in FIG. 2) as heating means. A superheated steam introduction line 32 is connected to the upstream end of the heat transfer pipe 31, and a part of the superheated steam extracted from a turbine of an operating boiler (not shown) is introduced into the superheated steam introduction line 32. Superheated steam flows through the heat pipe 31.

  A drain pipe 33 is connected to the downstream end of the heat transfer pipe 31. The superheated steam flows through the heat transfer pipe 31 and is condensed by exchanging heat with the lignite 6 in the fluidized bed 29 to release latent heat of condensation. The condensed water whose latent condensation heat has been recovered is discharged from the drain pipe 33. The drain pipe 33 is connected to a condenser such as a condenser (not shown), and the condensed water is returned to the boiler.

  The superheated steam introduction line 32 is connected to a bubbling steam introduction line 34 that branches from a middle portion of the superheated steam introduction line 32. The bubbling steam introduction line 34 is connected to the heating side wind box 23, and the remaining superheated steam extracted from the boiler turbine serves as the bubbling steam 25 through the heating side wind box 23 and the steam supply nozzle 24. To be supplied.

  A cooling air introduction line 35 is connected to the cooling side window box 26. The cooling air introduction line 35 is connected to a cooling air supply source (not shown), and the cooling air 28 is supplied to the cooling air supply nozzle 27 through the cooling side window box 26.

  The steam supply nozzle 24, the cooling air supply nozzle 27, the heating side wind box 23, the cooling side window box 26, the bubbling steam introduction line 34, and the cooling air introduction line 35 constitute a fluid medium supply means. The

  Next, the details of the drying device 12 will be described with reference to FIG. In FIG. 3, the heat transfer tube 31 is shown only on the upper part of the fluidized bed 29 in the heating region 14, but the heat transfer tube 31 is similarly provided on the middle and lower parts of the fluidized bed 29. It shall be.

  The lignite hopper 17 stores the lignite 6 pulverized by a pulverizer 11 (see FIG. 2), and the lignite 6 is supplied from the lignite hopper 17 to the heating region 14 via the lignite supply line 16. It is supposed to be done. The opening position of the lignite supply line 16 with respect to the drying chamber 13 is located above the opening position of the lignite discharge line 21 with respect to the drying chamber 13. The height difference between the opening position of the lignite supply line 16 and the opening position of the lignite discharge line 21 is appropriately determined according to the fluidity of the lignite 6 liquefied by bubbling and the drying processing capability of the drying device 12. .

  In the drying chamber 13, a plurality of dividing walls provided to divide the drying chamber 13 into a plurality of drying compartments, for example, a first dividing wall 36, a second dividing wall 37, a third dividing wall from the upstream side. There are six divided walls 38, a fourth divided wall 39, a fifth divided wall 40, and a sixth divided wall 41.

  The first dividing wall 36 to the third dividing wall 38 are located in the heating region 14, and the fifth dividing wall 40 and the sixth dividing wall 41 are located in the cooling region 15. The fourth dividing wall 39 is located at the boundary between the heating area 14 and the cooling area 15 so that the heating area 14 and the cooling area 15 are separated by the fourth dividing wall 39. It has become. In addition, the flow length of the lignite 6 is longer in the heating area 14 than in the cooling area 15.

  The first dividing wall 36, the third dividing wall 38, and the fifth dividing wall 40 each have an upper end protruding above the surface of the fluidized bed 29, and between the lower end and the bottom plate 22 of the drying chamber 13. Are formed with gaps 43, 44, 45 having predetermined intervals, respectively. The second dividing wall 37, the fourth dividing wall 39, and the sixth dividing wall 41 are provided so as to protrude above the bottom plate 22 of the drying chamber 13, and the upper end is predetermined from the surface of the fluidized bed 29. It is located below the distance. The size of the gaps 43 to 45 is appropriately selected according to the fluidity of the fluidized bed 29.

  A first drying compartment 46 is formed between the first dividing wall 36 and the side wall of the drying device 12 on the lignite supply line 16 side, and between the first dividing wall 36 and the second dividing wall 37. A second drying compartment 47 is formed, a third drying compartment 48 is formed between the second dividing wall 37 and the third dividing wall 38, and the third dividing wall 38 and the fourth dividing wall 39 A fourth drying compartment 49 is formed therebetween, a fifth drying compartment 50 is formed between the fourth dividing wall 39 and the fifth dividing wall 40, and the fifth dividing wall 40 and the sixth dividing wall 41 are formed. A sixth drying compartment 51 is formed between the sixth partition wall 41 and a side wall of the drying device 12 on the lignite discharge line 21 side.

  The heating side window box 23 and the cooling side window box 26 are divided so as to correspond to the respective drying compartments 46 to 52. That is, the first wind box 55 for supplying the bubbling steam 25 to the first drying compartment 46, the second window box 56 for supplying the bubbling steam 25 to the second drying compartment 47, and the third drying compartment 48 to the first drying compartment 46, respectively. A third wind box 57 for supplying bubbling steam 25, a fourth wind box 58 for supplying the bubbling steam 25 to the fourth drying compartment 49, and a fifth wind box for supplying the cooling air 28 to the fifth drying compartment 50 59, a sixth window box 60 for supplying the cooling air 28 to the sixth drying compartment 51, and a seventh window box 61 for supplying the cooling air 28 to the seventh drying compartment 52, respectively.

  The bubbling steam introduction line 34 is connected to the first window box 55 to the fourth window box 58, respectively. The bubbling steam introduction line 34 has a first adjustment valve 63 for adjusting the flow rate of the bubbling steam 25 supplied to the first wind box 55 and the bubbling steam 25 supplied to the second wind box 56. The second adjusting valve 64 for adjusting the flow rate of the gas, the third adjusting valve 65 for adjusting the flow rate of the bubbling steam 25 supplied to the third wind box 57, and the bubbling steam 25 supplied to the fourth wind box 58. A fourth adjustment valve 66 for adjusting the flow rate of each is provided.

  The cooling air introduction line 35 is connected to the fifth window box 59 to the seventh window box 61, respectively. The cooling air introduction line 35 has a fifth adjustment valve 67 for adjusting the flow rate of the cooling air 28 supplied to the fifth window box 59 and the cooling air 28 supplied to the sixth window box 60. A sixth adjustment valve 68 for adjusting the flow rate of the cooling air 28 and a seventh adjustment valve 69 for adjusting the flow rate of the cooling air 28 supplied to the seventh window box 61 are provided.

  The drying device 12 includes a first pressure gauge 71 that detects the pressure in the first drying compartment 46, a second pressure gauge 72 that detects the pressure in the second drying compartment 47, and the third pressure gauge. A third pressure gauge 73 for detecting the pressure in the drying compartment 48, a fourth pressure gauge 74 for detecting the pressure in the fourth drying compartment 49, and a fifth pressure for detecting the pressure in the fifth drying compartment 50 A first pressure gauge 71, a sixth pressure gauge 76 for detecting the pressure in the sixth drying compartment 51, and a seventh pressure gauge 77 for detecting the pressure in the seventh drying compartment 52. The seventh pressure gauge 77 is electrically connected to the control unit 78. The controller 78 is electrically connected to the first adjustment valve 63 to the seventh adjustment valve 69 so that the opening degree of the first adjustment valve 63 to the seventh adjustment valve 69 can be controlled. Yes. In FIG. 3, the first pressure gauge 71 to the seventh pressure gauge 77 are provided inside the first dry compartment 46 to the seventh dry compartment 52 for convenience. It is provided outside the drying compartment 46 to the seventh drying compartment 52.

  The pressure detected by the first pressure gauge 71 to the seventh pressure gauge 77 varies depending on, for example, the supply amount and particle size distribution of the lignite 6, and the control unit 78 controls the first pressure gauge 71. Based on the detection result of the seventh pressure gauge 77, the layer pressure loss of the first dry compartment 46 to the seventh dry compartment 52 is calculated. The controller 78 individually controls the opening degrees of the first adjustment valve 63 to the seventh adjustment valve 69 based on the calculated layer pressure loss, and the first window box 55 to the seventh window box 61. The supply amount of the bubbling steam 25 and the cooling air 28 supplied to the air is adjusted.

  FIG. 4 is a graph showing the relationship between the laminar pressure loss calculated based on the detected pressure and the fluid medium such as the bubbling steam 25 and the cooling air 28. As shown in FIG. 4, the laminar pressure loss increases as the flow rate of the fluidized medium increases. However, when the fluidized bed 29 reaches the fluidization region where the fluidized layer 29 is in a completely fluidized state, the flow rate of the fluidized medium is increased. However, the layer pressure loss does not increase any more and becomes constant. Assuming that the layer pressure loss at this time is the maximum layer pressure loss Pc, the maximum layer pressure loss Pc has different values in the first drying compartment 46 to the seventh drying compartment 52, respectively. In the storage unit (not shown) of the control unit 78, the layer pressure loss Pc of each of the first drying compartment 46 to the seventh drying compartment 52 is set, and the maximum flow rate Fm on the design of the fluid medium is set.

  The lignite 6 supplied from the lignite supply line 16 is liquefied by bubbling of the bubbling steam 25 and bubbling of the cooling air 28 and is discharged from the lignite discharge line 21 before the first drying. Flows in the compartment 46 to the fourth dry compartment 49 while being turned upside down and dried, and flows in the fifth dry compartment 50 to the seventh dry compartment 52 while being turned upside down and cooled. It is like. By flowing while the first dry compartment 46 to the seventh dry compartment 52 are turned upside down, the flow path length becomes longer, and sufficient time is provided for drying and cooling.

  Next, the drying of the lignite 6 by the hydrated matter drying system 5 according to the present embodiment will be further described.

  First, the unpulverized brown coal 6 is put into the pulverizer 11 and pulverized by the pulverizer 11 so that the particle diameter becomes 2 mm or less. After the lignite 6 pulverized by the pulverizer 11 is stored in the lignite hopper 17, the lignite 6 is charged into the drying device 12 through the lignite supply line 16. At this time, the lignite 6 has a particle size distribution of about 10 μm to 2 mm.

  The lignite 6 supplied to the drying device 12 is accumulated in the first drying compartment 46, and the bubbling steam 25 is supplied from the first wind box 55 to the deposited lignite 6 through the steam supply nozzle 24. By doing so, the fluidized bed 29 of the lignite 6 liquefied and having fluidity is formed.

  At this time, the pressures in the first dry compartment 46 to the seventh dry compartment 52 are detected by the first pressure gauge 71 to the seventh pressure gauge 77, and the first pressure gauge 71 to the seventh pressure gauge are detected. The detection result of the pressure gauge 77 is fed back to the control unit 78. From the detection result, the supply amount of the bubbling steam 25 and the cooling air 28 to the fluidized bed 29 is determined based on a predetermined setting.

  For example, in the case of the second drying compartment 47, the control unit 78 calculates the layer pressure loss P2 of the second drying compartment 47 based on the pressure detected by the second pressure gauge 72, and the layer pressure loss P2 is calculated in advance. The set maximum layer pressure loss Pc in the second drying compartment 47 is compared. When the control unit 78 determines that P2 <Pc, that is, it is not a complete flow state, the control unit 78 opens the second adjustment valve 64 to increase the flow rate of the bubbling steam 25. Further, when the control unit 78 determines that P2 ≧ Pc, that is, a complete flow state and the flow rate of the bubbling steam 25 has reached the maximum flow rate Fm, the control unit 78 controls the second adjustment valve 64 to be closed, The flow rate of the bubbling steam 25 is decreased. By the above process, the bubbling vapor 25 can be supplied so that the fluidized bed 29 in the second drying compartment 47 is always in the fluidized region, and the fluidized bed 29 can be always in a completely fluidized state.

  Similarly, the pressures detected by the first pressure gauge 71 and the third pressure gauge 73 to the seventh pressure gauge 77 in the first dry compartment 46 and the third dry compartment 48 to the seventh dry compartment 52. The layer pressure loss is calculated on the basis of this, the layer pressure loss is compared with a preset maximum layer pressure loss Pc for each drying compartment, and the first adjustment valve 63 and the third adjustment valve 65-65 are compared based on the comparison result. The opening degree of the seventh adjustment valve 69 is controlled, and the supply amounts of the bubbling steam 25 and the cooling air 28 are adjusted.

  At this time, since the fluidized bed 29 flows downward due to its own weight, the fluidized bed 29 flows with respect to the downward flow in the first dry compartment 46, the third dry compartment 48, the fifth dry compartment 50, and the seventh dry compartment 52. The supply amount of the bubbling steam 25 and the cooling air 28 is the supply amount of the bubbling steam 25 and the cooling air 28 with respect to the upward flow in the second drying compartment 47, the fourth drying compartment 49, and the sixth drying compartment 51. Less than. In addition, by intentionally setting P2 <Pc, it is possible to suppress fluidization and promote downward flow.

  In parallel with the supply of the lignite 6 from the lignite supply line 16, superheated steam is introduced into the superheated steam introduction line 32, and the superheated steam flows through the heat transfer pipe 31.

  The fluidized bed 29 flows downward in the first drying compartment 46, passes through the gap 43, and flows into the second drying compartment 47. At this time, since the supplied lignite 6 contains a large amount of water, the lignite 6 descends in the first dry compartment 46 due to its own weight. The lower lignite 6 is extruded from the gap 43 to the second drying compartment 47 by the pressure from the upper part and flows. The lignite 6 is in contact with the heat transfer pipe 31 in the process of flowing from the first drying compartment 46 to the second drying compartment 47, and is heated by heat exchange with superheated steam flowing through the heat transfer pipe 31, It is dried and further heated by heat exchange with the bubbling steam 25 and dried.

  The size of the gap 43 is set according to the fluidity of the fluidized bed 29 so that the lignite 6 does not move over the first partition wall 36 and move to the second drying compartment 47. Further, the amount of lignite 6 fed from the lignite hopper 17 is adjusted so as not to get over the first dividing wall 36 and move to the second drying compartment 47.

  The lignite 6 that has flowed into the second drying compartment 47 is reversed in the second drying compartment 47 and flows upward from below, and passes over the second dividing wall 37 to the third drying compartment 48. Flows in the third drying compartment 48 and flows downward from above, flows through the gap 44 and flows into the fourth drying compartment 49, and inverts in the fourth drying compartment 49. It flows from the bottom to the top.

  At this time, the lignite 6 is dried by heat exchange in the first drying compartment 46 and the fluidity of the fluidized bed 29 is increased, and the lignite 6 is further pressurized by the pressure from the first drying compartment 46 side. It smoothly flows to the third drying compartment 48 and the fourth drying compartment 49 without backflow.

  Also in the second drying compartment 47 to the fourth drying compartment 49, the lignite 6 is heated by the superheated steam flowing through the heat transfer pipe 31 and the bubbling steam 25 in the process of flowing while the lignite 6 is turned upside down. Dried.

  The dry lignite 7 dried in the first dry compartment 46 to the fourth dry compartment 49 flows over the fourth dividing wall 39 and flows into the fifth dry compartment 50 in the cooling region 15. The dried lignite 7 that has flowed into the fifth drying compartment 50 is reversed in the fifth drying compartment 50 and flows downward from above, flows through the gap 45, and flows into the sixth drying compartment 51. To do. In addition, the dry lignite 7 is reversed in the sixth dry compartment 51 and flows upward from below, flows over the sixth dividing wall 41 and flows into the seventh dry compartment 52, and the lignite discharge line 21. More discharged.

  The dry lignite 7 is cooled by the cooling air 28 supplied from the cooling air supply nozzle 27 in the process of flowing while inverting the fifth dry compartment 50 to the seventh dry compartment 52. Further, steam and cooling air generated in the process in which the lignite 6 and the dried lignite 7 flow through the first dry compartment 46 to the seventh dry compartment 52 and are cooled and dried are passed through the exhaust line 19. Exhausted to the outside.

  The superheated steam flowing through the heat transfer tube 31 is exchanged with the brown coal 6 in the fluidized bed 29 in the process of flowing through the heat transfer tube 31. Through heat exchange with the lignite 6, the latent heat of condensation of the superheated steam is recovered and phase-changed to become condensed water, which is sent to a condenser such as a condenser (not shown) through the drain pipe 33.

  The cooled dry lignite 7 discharged from the drying chamber 13 is sent to the burner 3, and the dry lignite 7 is burned by the burner 3.

  As described above, in this embodiment, the supply amount of the fluid medium supplied to the first drying compartment 46 to the seventh drying compartment 52 is individually adjusted by the first adjustment valve 63 to the seventh adjustment valve 69. The supply amount of the fluid medium with respect to the downward flow of the fluidized bed 29 that flows downward due to its own weight is made smaller than the supply amount of the fluid medium with respect to the upward flow of the fluidized bed 29.

  Therefore, since the fluid medium more than necessary is not supplied to the lignite 6 in the fluidized bed 29, it is possible to prevent the lignite 6 from being scattered and to reduce the supply amount of the fluid medium, The power required to supply the fluid medium can be reduced.

  Further, since the fluid medium can be supplied to the first dry compartment 46 to the seventh dry compartment 52 in accordance with the fluidity of the fluidized bed 29, the fluidity of the fluidized bed 29 is improved. The drying efficiency of the lignite 6 can be improved.

  Further, the first pressure gauge 71 to the seventh pressure gauge 77 are provided in the first drying compartment 46 to the seventh drying compartment 52, and the maximum layer pressure loss Pc is preset for each of the drying compartments 46 to 52, Based on the comparison of the detection results of the first pressure gauge 71 to the seventh pressure gauge 77 and the maximum bed pressure loss Pc for each of the drying compartments 46 to 52, the supply amount of the fluid medium can be changed. Even if there is a change in the supply amount or particle size distribution of the brown coal 6, the fluidized medium having an optimum flow rate according to the fluidity can be supplied so that the fluidized bed 29 is always in a completely fluid state. can do.

  Further, in this embodiment, the fourth dividing wall 39 divides the drying chamber 13 into the heating region 14 for heating and drying the lignite 6 and the cooling region 15 for cooling the dry lignite 7, Since both the drying of the lignite 6 and the cooling of the dried lignite 7 can be performed in the drying chamber 13, there is no need to separately provide a cooling mechanism for cooling the dried lignite 7, and the apparatus configuration is simplified. Manufacturing cost can be reduced.

  Further, the heating region 14 is divided into the first drying compartment 46, the four partition walls, the first partition wall 36, the second partition wall 37, the third partition wall 38, and the fourth partition wall 39. Divided into four dry compartments, a second dry compartment 47, a third dry compartment 48, and a fourth dry compartment 49, and each division so that the lignite 6 flows while turning upside down between the dry compartments 46-49. Walls 36 to 39 are arranged. Therefore, the distance over which the lignite 6 flows is increased, the time for heating by the heat transfer tube 31 and the bubbling steam 25 can be increased, the drying device 12 can be downsized, and a large amount of the lignite 6 can be obtained. It can be dried efficiently.

  In addition, the cooling region 15 is divided into the fifth drying compartment 50, the sixth drying compartment 51, the three partition walls of the fourth partition wall 39, the fifth partition wall 40, and the sixth partition wall 41. Each of the dividing walls 39 to 41 is arranged so that the dry lignite 7 is divided into three drying compartments of the seventh drying compartment 52 and flows while the dry lignite 7 is turned upside down between the respective drying compartments 50 to 52. Therefore, the distance that the dried lignite 7 flows, that is, the time for cooling by the cooling air 28 can be increased, and a large amount of the dried lignite 7 can be efficiently cooled.

  The upper ends of the first dividing wall 36, the third dividing wall 38, and the fifth dividing wall 40 are protruded upward from the surface of the fluidized bed 29, so that the first dividing wall 36 and the third dividing wall are projected. 38, the gaps 43 to 45 are formed between the lower end of the fifth dividing wall 40 and the bottom plate 22, respectively, and the second dividing wall 37, the fourth dividing wall 39, and the sixth dividing wall 41 are provided. Since it is provided so as to protrude upward from the bottom plate 22 and no gap is formed between the bottom plate 22, the lignite 6 and the dry lignite 7 can be reliably reversed upward, It is possible to prevent the lignite 6 and the dried lignite 7 from staying in the drying chamber 13.

  Furthermore, since the fourth dividing wall 39 is provided at the boundary between the heating region 14 and the cooling region 15, the bubbling vapor 25 can be prevented from entering the cooling region 15, and the cooling air 28 can be prevented. Can be prevented from being mixed into the heating region 14, and the heating efficiency of the lignite 6 and the cooling efficiency of the dry lignite 7 can be prevented from decreasing.

  In the drying apparatus 12 of the present embodiment, seven drying compartments 46 to 52 are formed by six dividing walls 36 to 41, but the number of the dividing walls and the dividing walls are used. The number of dry compartments to be selected is appropriately selected according to the dry state of the lignite 6 and the like, for example, 5 or less dry compartments may be formed by 4 or less divided walls, or 7 or more divided compartments. Eight or more dry compartments may be formed by walls.

  Further, in this embodiment, the case where the lignite 6 is dried by the drying device 12 is described, but the drying device 12 of the present embodiment is also used when other hydrated materials such as biomass are dried. Needless to say, is applicable.

DESCRIPTION OF SYMBOLS 1 Boiler apparatus 5 Water content drying system 6 Brown coal 12 Drying apparatus 13 Drying room 14 Heating area 15 Cooling area 23 Heating side wind box 24 Steam supply nozzle 25 Bubbling steam 26 Cooling side wind box 27 Cooling air supply nozzle 28 Cooling air 29 Fluidized bed 31 Heat transfer tube 36-41 Partition wall 46-52 Drying compartment 55-61 Wind box 63-69 Adjusting valve 71-77 Pressure gauge 78 Control unit

Claims (3)

A drying chamber in which the hydrated material is dried, a hydrated material supplying means for supplying the hydrated material from one end of the drying chamber, and a discharging means for discharging the hydrated material dried from the other end of the drying chamber; Heating means provided in the drying chamber, exhaust means for exhausting steam generated by heating from the other end of the drying chamber, and fluid medium supply for ejecting a fluid medium into the drying chamber and liquefying the hydrated material Means, a plurality of dividing walls that divide the drying chamber into a plurality of drying compartments, and the adjacent drying compartments communicate with each other at the upper part or the lower part so that the hydrated material flows while reversing up and down between the respective drying compartments ; A pressure gauge for detecting the pressure in the drying compartment, and a controller; and the fluid medium supply means has a wind box formed at the bottom of the drying compartment, and the wind box corresponds to each drying compartment. And the divided window The fluid medium is supplied to each de box, the supply amount of the fluidized medium and the control unit with respect to the dry compartment where the hydrous material flows downward, the fluid medium relative to the dry compartment where the hydrous material flows upwardly Less than the supply amount of the pressure, calculate the layer pressure loss for each drying compartment based on the detection result of the pressure gauge, and based on the comparison between the layer pressure loss and a preset maximum layer pressure loss, A drying apparatus for controlling a supply amount of a fluid medium .   When the control unit determines that the laminar pressure loss is smaller than the maximum laminar pressure loss, the control unit increases the supply amount of the fluid medium, and when it determines that the laminar pressure loss is greater than the maximum laminar pressure loss, the supply of the fluid medium 2. The drying device of claim 1 which reduces the amount.   In the drying chamber, a heating region is formed by a plurality of drying compartments on the upstream side, a cooling region is formed by a plurality of drying compartments on the downstream side, and steam is supplied to each wind box corresponding to each drying compartment in the heating region. The drying apparatus according to claim 1 or 2, wherein cooling air is supplied to each wind box corresponding to each drying compartment in the cooling region.

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