JP6697312B2 - Wet biomass incinerator system and method of operating wet biomass incinerator - Google Patents

Description

  The present invention relates to a wet biomass incineration system and a method for operating a wet biomass incinerator.

  BACKGROUND ART As a treatment facility for high-moisture content biomass such as sewage sludge, for example, a wet biomass incineration system including an internal circulation fluidized bed type wet biomass incinerator is known. The internal circulation fluidized bed type wet biomass incinerator has a drying chamber and a combustion chamber as disclosed in, for example, Patent Document 1 and Japanese Patent Application No. 2015-013429. Below each of the drying chamber and the combustion chamber, a fluidized bed in which a fluidized medium flows is provided across the drying chamber and the combustion chamber.

  In this wet biomass incinerator, the drying agent gas supplied from below the fluidized bed into the drying chamber dries the biomass while mixing it with the fluid medium, and the high temperature combustion agent gas supplied from below the fluidized bed into the combustion chamber. Thereby, the biomass dried in the drying chamber is burned while being mixed with the fluid medium. The dry exhaust gas generated by drying the biomass or the combustion exhaust gas generated by burning the biomass is subjected to heat recovery and introduced into, for example, a power generation device provided outside the incinerator for power generation.

JP, 2006-275442, A

  It is desirable that the wet biomass incinerator can be operated at an appropriate temperature in order to reduce the emission of greenhouse gases and dioxins. However, fluctuations in the water content of the biomass and the calorific value per unit weight of the solid content of the biomass may make the temperature in the combustion chamber unstable and increase the amounts of greenhouse gases and dioxins generated. Further, if the temperature of the drying chamber rises, a gasification reaction may occur depending on the temperature, and troubles such as tars adhering to the equipment downstream of the incinerator may occur. Further, when power is generated using dry exhaust gas or combustion exhaust gas, the power generation efficiency decreases when the temperature of the wet biomass incinerator becomes unstable.

  For such a problem, it may be difficult to quickly adjust the temperature of each chamber even if the amount of the desiccant gas supplied to the drying chamber or the amount of the combustion agent gas supplied to the combustion chamber is adjusted.

  Therefore, in the present invention, in a wet biomass incinerator of an internal circulation fluidized bed type having a drying chamber and a combustion chamber, the heat generation amount per unit weight of the moisture content of the biomass or the solid content of the biomass supplied to the wet biomass incinerator is temporarily changed. Even if the temperature fluctuates over time, it is intended to facilitate quick adjustment of the temperatures of the drying chamber and the combustion chamber of the wet biomass incinerator.

  In order to solve the above problems, a wet biomass incineration system according to an aspect of the present invention is a drying chamber and a combustion chamber, a fluidized bed including a fluid medium that flows over the lower portion of the drying chamber and the lower portion of the combustion chamber, A wet biomass incinerator having a partition wall that divides the space above the fluidized bed of the drying chamber and the space above the fluidized bed of the combustion chamber and has a lower end located inside the fluidized bed, and the drying chamber. Side of the fluidized bed, a desiccant gas supply path for supplying a desiccant gas for drying the biomass in the drying chamber while mixing with the fluidized medium into the drying chamber, and the flow on the combustion chamber side. A combustion agent gas supply path for supplying, into the combustion chamber, a combustion agent gas for burning the biomass dried in the drying chamber while mixing with the fluidized medium in the combustion chamber from below the floor, and the drying chamber. A first flow rate control valve, which is provided in a dry exhaust gas discharge passage communicating with the upper space, and controls a flow rate of the dry exhaust gas discharged from the upper space of the drying chamber to the outside of the drying chamber; A second flow rate control valve that is provided in a combustion exhaust gas discharge path communicating with a space and that controls a flow rate of the combustion exhaust gas discharged from the upper space of the combustion chamber to the outside of the combustion chamber, the first flow rate control valve And an opening of one of the second flow rate control valves is narrower than an opening of the other valve, so that one of the drying chamber and the combustion chamber is provided with the one valve. The fluidized bed height of the fluidized bed on the chamber side, and the fluidized bed height of the fluidized bed on the other chamber side where the other valve is provided, the gas pressure in the upper space of the one chamber, and The other chamber is adjusted so as to be relatively displaced in a direction in which the difference from the gas pressure in the upper space is reduced.

  According to the above configuration, the opening degree of one of the first flow rate adjusting valve and the second flow rate adjusting valve is narrower than the opening degree of the other valve, thereby utilizing the fluidity of the fluidized medium, The fluidized bed height on the one chamber side and the fluidized bed height on the other chamber side are relatively quick in the direction in which the difference between the gas pressure in the one chamber and the gas pressure in the other chamber is reduced. Can be displaced.

  Therefore, when it is desired to increase the temperature of the drying chamber side of the wet biomass incinerator, the opening degree of the second flow rate control valve is narrowed down from the opening degree of the first flow rate control valve, so that the flow medium and the biomass in the combustion chamber A portion can be moved into the drying chamber to increase the amount of fluid medium in the drying chamber with the amount of biomass. Therefore, by mixing the high-temperature fluid medium and biomass moving from the combustion chamber side to the drying chamber side with the fluid medium and biomass in the drying chamber, the drying of the biomass can be performed more quickly than the method of increasing the desiccant gas supply amount. It is possible to easily raise the temperature on the drying chamber side of the wet biomass incinerator while efficiently promoting the above.

  In addition, when it is desired to raise the temperature of the combustion chamber side of the wet biomass incinerator, the opening degree of the first flow rate control valve is narrower than that of the second flow rate control valve, so that the flow medium and the biomass in the drying chamber can be reduced. A portion can be moved into the combustion chamber to increase the amount of biomass in the combustion chamber with the amount of fluid medium. Therefore, by mixing the fluidizing medium and the biomass that have moved from the drying chamber side to the combustion chamber side with the fluidizing medium and the biomass in the combustion chamber, the combustion of the biomass can be efficiently burned more quickly than the method of increasing the supply amount of the combustion agent gas. The temperature on the combustion chamber side of the wet biomass incinerator can be easily increased while promoting well.

  Therefore, even if the moisture content of the biomass supplied to the wet biomass incinerator and the calorific value per unit weight of the solid content of the biomass fluctuate temporarily, the fluidized bed heights on the drying chamber side and the combustion chamber side are relatively changed. By displacing, the temperature of the drying chamber and the combustion chamber of the wet biomass incinerator can be easily adjusted quickly.

  A steam flow meter for measuring the steam flow rate of the dry exhaust gas discharged to the outside of the drying chamber may be further provided. Thereby, the water content of the biomass in the drying chamber can be easily confirmed from the measurement value of the steam flow meter.

  A combustion chamber thermometer disposed inside the combustion chamber may be further provided. Thereby, the calorific value per unit weight of the solid content of the biomass in the combustion chamber can be easily confirmed from the measurement value of the combustion chamber thermometer.

  A drying chamber thermometer disposed in the drying chamber may be further provided. Thereby, the temperatures of the biomass and the fluidized medium in the drying chamber can be easily confirmed from the measurement values of the drying chamber thermometer.

  The differential pressure change between the gas pressure of the one chamber and the pressure that extends downward from the upper side to the bottom of the fluidized bed on the side of the one chamber, and the gas pressure of the other chamber. Further, a differential pressure gauge for measuring the moving amount of the fluid medium and the biomass by at least one of the differential pressure change from the pressure that extends downward from the upper side to the bottom of the fluidized bed on the side of the other chamber You may prepare. Thereby, when the opening degree of one of the first flow rate adjusting valve and the second flow rate adjusting valve is narrower than the opening degree of the other valve, from the change in the measured value of the differential pressure gauge, It is possible to easily confirm the movement of the fluidized medium and the biomass between the drying chamber and the combustion chamber.

  A method for operating a wet biomass incinerator according to an aspect of the present invention includes a drying chamber and a combustion chamber, a fluidized bed including a fluidized medium that flows over a lower portion of the drying chamber and a lower portion of the combustion chamber, and A wet biomass incinerator having a partition wall that partitions the upper space of the fluidized bed and the upper space of the fluidized bed of the combustion chamber and has a lower end arranged in the fluidized bed, and the fluidized bed of the drying chamber side. From below, a desiccant gas supply path for supplying a desiccant gas for drying the biomass in the drying chamber while mixing the biomass with the fluid medium, and from below the fluidized bed on the combustion chamber side, A combustion agent gas supply path for supplying a combustion agent gas for burning the biomass dried in the drying chamber with the fluidized medium in the combustion chamber into the combustion chamber, and an upper space of the drying chamber. A first flow rate control valve provided in a dry exhaust gas discharge passage communicating with the first exhaust gas, for adjusting a flow rate of the dry exhaust gas discharged from the upper space of the drying chamber to the outside of the drying chamber, and a combustion communicating with the upper space of the combustion chamber. A first flow rate control valve in a wet biomass incineration system, comprising a second flow rate control valve that is provided in an exhaust gas discharge path and that controls a flow rate of combustion exhaust gas discharged from the space above the combustion chamber to the outside of the combustion chamber. And one of the drying chamber and the combustion chamber in which the one valve is provided by narrowing the opening of one valve of the second flow rate control valve more than the opening of the other valve. The fluidized bed height on the side, and the fluidized bed height on the other chamber side where the other valve is provided, the gas pressure in the upper space of the one chamber, and the upper space of the other chamber. The relative displacement is made in the direction in which the difference from the gas pressure is reduced.

  The moisture content value of the biomass in the drying chamber is a value larger than a predetermined first moisture content upper limit value, and the calorific value of the solid content of the biomass per unit weight is predetermined. When the value is equal to or more than the first heating value lower limit value, the one valve may be the second flow rate control valve.

  According to the above method, when the temperature of the drying chamber side of the wet biomass incinerator is low because the moisture content value of the biomass in the drying chamber is larger than the first moisture content upper limit value, The calorific value is relatively high because the calorific value is greater than or equal to the first calorific value lower limit value, and the high-temperature fluidized medium in the combustion chamber is dried with a part of the biomass burned at high temperature in the combustion chamber. By moving it into the room, it is possible to easily raise the temperature on the drying room side of the wet biomass incinerator while promptly and efficiently promoting the drying of the biomass in the drying room.

  A moisture content value of the biomass in the combustion chamber is less than or equal to a predetermined second moisture content upper limit value, and a calorific value of the solid content of the biomass per unit weight is a predetermined value. When the value is less than the lower limit value of 2 calorific values, the one valve may be the first flow rate control valve.

  According to the above method, since the calorific value of the solid content of biomass per unit weight is less than the second calorific value lower limit value, when the temperature on the combustion chamber side of the wet biomass incinerator is low, By moving a part of the biomass having a relatively low water content value due to the water content value being equal to or less than the second water content upper limit value into the combustion chamber together with a part of the fluidized medium in the drying chamber, The temperature on the combustion chamber side of the wet biomass incinerator can be easily increased while promptly and efficiently promoting the combustion of biomass.

  The water content of the biomass in the drying chamber may be confirmed by a steam flow meter that measures the steam flow rate of the dry exhaust gas discharged outside the drying chamber.

  The temperature in the combustion chamber may be measured by a combustion chamber thermometer arranged in the combustion chamber.

  The temperature in the drying chamber may be measured by a drying chamber thermometer arranged in the drying chamber.

  The differential pressure change between the gas pressure of the one chamber and the pressure that extends downward from the upper side to the bottom of the fluidized bed on the side of the one chamber, and the gas pressure of the other chamber. , Using a differential pressure gauge for measuring the moving amount of the fluid medium and the biomass by at least one of the differential pressure change from the pressure applied from the upper side to the lower side of the bottom of the fluidized bed on the side of the other chamber Then, the movement of the fluidized medium and the biomass due to the relative displacement may be confirmed.

  According to each aspect of the present invention, in an internal circulation fluidized bed type wet biomass incinerator having a drying chamber and a combustion chamber, per unit weight of the moisture content of biomass or the solid content of biomass supplied to the wet biomass incinerator. Even if the calorific value fluctuates temporarily, the temperatures of the drying chamber and the combustion chamber of the wet biomass incinerator can be easily adjusted quickly.

1 is an overall view of a wet biomass incineration system according to an embodiment. It is a figure which illustrates the operating method according to the relationship between the calorific value and the water content of the biomass of the wet biomass incinerator of FIG. It is a figure which shows the process of the 1st operating method of the wet biomass incinerator of FIG. It is a figure which shows a mode that the fluidized bed height of the drying chamber side and the combustion chamber side was relatively displaced when the wet biomass incinerator of FIG. 1 is operated by the first operating method. It is a figure which shows the process of the 2nd operating method of the wet biomass incinerator of FIG. It is a figure which shows a mode that the fluidized bed height of the drying chamber side and the combustion chamber side was relatively displaced when the wet biomass incinerator of FIG. 1 was operated by the second operating method. It is a figure which shows the process of the 3rd operating method of the wet biomass incinerator of FIG.

  Hereinafter, embodiments of the present invention will be described with reference to the drawings.

[Configuration of wet biomass incineration system 1]
FIG. 1 is an overall view of a wet biomass incineration system 1 according to an embodiment. As shown in FIG. 1, the wet biomass incineration system 1 includes a wet biomass incinerator 2, a biomass supply path R1, a desiccant gas supply path R2, a combustion agent gas supply path R3, a dry exhaust gas discharge path R4, and a combustion exhaust gas discharge path R5. , A combustion ash discharge passage R6, an auxiliary fuel supply passage R7, a first flow rate control valve V1, a second flow rate control valve V2, and a control device 3.

  The wet biomass incinerator 2 includes a drying chamber 2a, a combustion chamber 2b, a partition wall 2c, a hearth floor 2d, a plurality of nozzles 2e, a fluidized bed 2f, wind boxes 2g and 2h, upper spaces 15 and 16, a steam flow meter D1, and drying. It has a chamber thermometer D2, a combustion chamber thermometer D3, a drying chamber differential pressure gauge D4, and a combustion chamber differential pressure gauge D5.

  The drying chamber 2a and the combustion chamber 2b are provided inside the wet biomass incinerator 2 with a partition wall 2c therebetween. In the drying chamber 2a, the biomass 25 supplied from the outside via the biomass supply port 2a1 provided above the drying chamber 2a is dried. In the combustion chamber 2b, the biomass 25 dried in the drying chamber 2a is burned.

  During operation of the wet biomass incinerator 2, the temperature in the drying chamber 2a is set to a value in a temperature range suitable for drying the biomass 25, and the temperature in the combustion chamber 2b is set to burn the biomass 25. It is set to a value within a suitable temperature range. At this time, the temperature in the drying chamber 2a and the temperature in the combustion chamber 2b can be set appropriately.

  The partition wall 2c partitions the upper space 15 of the fluidized bed 2f on the drying chamber 2a side from the upper space 16 of the fluidized bed 2f on the combustion chamber 2b side. The lower end of the partition wall 2c is arranged in the fluidized bed 2f. As a result, the upper spaces (freeboards) 15 and 16 are isolated from each other.

  The hearth floor 2d is arranged below the drying chamber 2a and the combustion chamber 2b. The plurality of nozzles 2e are arranged on the upper surface of the hearth 2d in a distributed manner over the drying chamber 2a side and the combustion chamber 2b side. The fluidized bed 2f is arranged above the hearth 2d and below the drying chamber 2a and below the combustion chamber 2b. The fluidized bed 2f includes a fluidized medium (particulate matter) 20 that flows over the lower portion of the drying chamber 2a and the lower portion of the combustion chamber 2b. The fluid medium 20 is, for example, silica sand, but is not limited to this. During operation of the wet biomass incinerator 2, for example, the temperature of the fluidized bed 2f in the drying chamber 2a is preferably set to a value in a temperature range equal to or lower than the thermal decomposition temperature of the biomass 25, and the flow in the combustion chamber 2b is reduced. More preferably, the temperature of the floor 2f is set to a value in the temperature range of 500 ° C or higher and 800 ° C or lower. The wind boxes 2g and 2h are box bodies having a hollow inside. The wind box 2g is provided below the hearth 2d on the drying chamber 2a side. The wind box 2h is provided below the hearth 2d on the combustion chamber 2b side.

  The biomass supply path R1 supplies the biomass 25 into the drying chamber 2a from the outside. The biomass supply path R1 is connected to the biomass supply port 2a1. The desiccant gas supply path R2 supplies a desiccant gas for drying the biomass 25 while mixing the biomass 25 with the fluid medium 20 in the drying chamber 2a into the drying chamber 2a. The desiccant gas supply path R2 is connected to the wind box 2g. The desiccant gas is, but is not limited to, superheated steam. The combustion agent gas supply path R3 supplies the combustion agent gas for combustion while mixing the biomass 25 dried in the drying chamber 2a with the fluid medium 20 in the combustion chamber 2b into the combustion chamber 2b. The combustion agent gas supply path R3 is connected to the wind box 2h. The combustor gas is air, but is not limited to this.

  The dry exhaust gas discharge path R4 discharges the dry exhaust gas generated by drying the biomass 25 in the upper space 15 to the outside of the drying chamber 2a. The dry exhaust gas discharge path R4 is connected to the drying chamber 2a. The combustion exhaust gas discharge path R5 discharges the combustion exhaust gas generated by the combustion of the biomass 25 in the upper space 16 to the outside of the combustion chamber 2b. The combustion exhaust gas discharge path R5 is connected to the combustion chamber 2b. The combustion ash discharge path R6 discharges the combustion ash generated by the combustion of the biomass 25 to the outside of the combustion chamber 2b. The combustion ash discharge passage R6 is connected to the combustion chamber 2b. The auxiliary fuel supply path R7 supplies the auxiliary fuel for assisting the combustion of the biomass 25 into the combustion chamber 2b. The auxiliary fuel supply passage R7 is connected to the wall portion of the combustion chamber 2b. The auxiliary fuel is flammable gas, but is not limited thereto.

  The first flow rate control valve V1 controls the flow rate of the dry exhaust gas discharged from the upper space 15 to the outside of the drying chamber 2a. The first flow control valve V1 is provided so as to communicate with the upper space 15. The first flow rate control valve V1 is provided in the middle of the dry exhaust gas discharge passage R4 and adjusts the flow rate of the dry exhaust gas flowing through the dry exhaust gas discharge passage R4. The first flow rate control valve V1 may be provided directly on the wall portion of the drying chamber 2a, for example. The first flow rate control valve V1 is set to the fully open state in the setting of the wet biomass incineration system 1. The gas pressure in the upper space 15 (hereinafter referred to as the dry chamber freeboard pressure) increases when the dry exhaust gas flow rate of the first flow rate control valve V1 is reduced and decreases when it is opened.

  The second flow rate control valve V2 controls the flow rate of the combustion exhaust gas discharged from the upper space 16 to the outside of the combustion chamber 2b. The second flow rate control valve V2 is provided in communication with the upper space 16. The second flow rate control valve V2 is provided in the middle of the combustion exhaust gas discharge passage R5 and adjusts the flow rate of the combustion exhaust gas flowing through the combustion exhaust gas discharge passage R5. The second flow rate control valve V2 may be directly provided on the wall portion of the combustion chamber 2b, for example. The second flow rate control valve V2 is set to the fully open state in the setting of the wet biomass incineration system 1. The gas pressure in the upper space 16 (hereinafter referred to as the combustion chamber freeboard pressure) rises when the combustion exhaust gas flow rate of the second flow rate control valve V2 is reduced and decreases when it is opened.

  The vapor flow meter D1 measures the vapor flow rate of the dry exhaust gas discharged from the upper space 15 to the outside of the drying chamber 2a. In the present embodiment, the steam flow meter D1 is arranged at a position downstream of the position where the first flow rate control valve V1 of the dry exhaust gas discharge passage R4 is arranged, and the steam flow rate of the dry exhaust gas flowing through the dry exhaust gas discharge passage R4. To measure.

  The drying chamber thermometer D2 is arranged in the drying chamber 2a and measures the temperature in the drying chamber 2a. The combustion chamber thermometer D3 is arranged in the combustion chamber 2b and measures the temperature in the combustion chamber 2b. The drying chamber thermometer D2 is arranged on the wall portion exposed to the upper space 15 of the drying chamber 2a, and measures the representative temperature in the drying chamber 2a. The combustion chamber thermometer D3 is arranged on the wall portion exposed to the upper space 16 of the combustion chamber 2b, and measures the representative temperature in the combustion chamber 2b. Each of the drying chamber thermometer D2 and the combustion chamber thermometer D3 may be arranged to measure the maximum or minimum temperature in the chamber.

  The wet biomass incineration system 1 includes a dry chamber freeboard pressure and a differential pressure change between a pressure applied to the bottom of the fluidized bed 2f on the drying chamber 2a side from above to below, a combustion chamber freeboard pressure, and a combustion chamber. A differential pressure gauge is provided at the bottom of the fluidized bed 2f on the 2b side to measure the amount of movement of the fluidized medium 20 and the biomass 25 by at least one of changes in the differential pressure with respect to the pressure extending from the upper side to the lower side.

  In the present embodiment, the wet biomass incineration system 1 has a drying chamber differential pressure gauge D4 and a combustion chamber differential pressure gauge D5 as the differential pressure gauges. The drying chamber differential pressure gauge D4 measures the differential pressure change between the drying chamber freeboard pressure and the pressure that extends from the upper side to the lower side of the bottom of the fluidized bed 2f on the drying chamber 2a side. The combustion chamber differential pressure gauge D5 measures the differential pressure change between the combustion chamber freeboard pressure and the pressure that extends from the upper side to the lower side of the bottom portion of the fluidized bed 2f on the combustion chamber 2b side.

  The control device 3 is, for example, a computer including a CPU, a ROM, a RAM, and the like, and controls the respective flow rates of the first flow rate control valve V1 and the second flow rate control valve V2. A predetermined control program is stored in the ROM. The control device 3 monitors the detection values of the steam flow meter D1, the thermometers D2 and D3, and the differential pressure gauges D4 and D5, based on the control program, and determines the first flow rate control valve V1 and the second flow rate control valve. Each flow rate with V2 is adjusted at a predetermined timing.

  As shown in FIG. 1, during operation of the wet biomass incinerator 2, the desiccant gas that has passed through the desiccant gas supply path R2 is dried from each nozzle 2e arranged on the drying chamber 2a side via the wind box 2g. It is ejected into the chamber 2a. The desiccant gas is mixed in the fluidized medium 20 and the biomass 25 as a plurality of bubbles. The biomass 25 is dried while being mixed with the fluid medium 20 by the desiccant gas ejected from each nozzle 2e. The biomass 25 dried by this moves together with the fluidized medium 20 from the drying chamber 2a side to the combustion chamber 2b side. The dry exhaust gas in the upper space 15 flows through the dry exhaust gas discharge path R4 and the first flow rate control valve V1 and is discharged to the outside of the drying chamber 2a. When a non-oxidizing gas such as superheated steam is used as the desiccant gas, the biomass 25 does not burn in the drying chamber 2a, and the dry exhaust gas is prevented from containing an oxygen component.

  Further, during operation of the wet biomass incinerator 2, the combustion agent gas that has passed through the combustion agent gas supply path R3 from each nozzle 2e arranged on the combustion chamber 2b side enters the combustion chamber 2b via the wind box 2h. Erupted. The combustion agent gas is mixed in the fluidized medium 20 and the biomass 25 as a plurality of bubbles. The biomass 25 is burned while being mixed with the fluid medium 20 by the combustion agent gas ejected from each nozzle 2e. The combustion exhaust gas in the upper space 16 is discharged to the outside of the combustion chamber 2b via the combustion exhaust gas discharge passage R5 and the second flow rate control valve V2, and the combustion ash flows through the combustion ash discharge passage R6 to the outside of the combustion chamber 2b. Is discharged. The heat generated by the combustion of the biomass 25 in the combustion chamber 2b moves together with the fluidized medium 20 from the combustion chamber 2b side to the drying chamber 2a side and is used for drying the biomass 25 in the drying chamber 2a.

  Here, in the wet biomass incinerator 2, the drying chamber freeboard pressure is adjusted by the first flow rate control valve V1 with the lower end of the partition wall 2c disposed inside the fluidized bed 2f, and the combustion chamber freeboard pressure is adjusted to the first level. It is controlled by the two flow rate control valve V2. Accordingly, in the wet biomass incinerator 2, the opening degree of one of the first flow rate control valve V1 and the second flow rate control valve V2 is narrower than the opening degree of the other valve, so that the drying chamber 2a and Of the combustion chamber 2b, the fluidized bed height of the fluidized bed 2f (the height position of the upper surface of the fluidized bed 2f) on the side of one chamber where the one valve is provided and the other chamber where the other valve is provided. The fluidized bed height of the fluidized bed 2f on the side is adjusted so as to be relatively displaced in a direction in which the difference between the gas pressure in the upper space of the one chamber and the gas pressure in the upper space of the other chamber is reduced. It

  Since the fluidized medium 20 and the biomass 25 have high fluidity as a whole, the first flow rate control valve V1 or the second flow rate control valve V2 is adjusted to control the gas pressure in either the upper space 15 or 16. For example, by raising the pressure by about several kPa compared to that during normal operation, the respective fluidized bed heights on the drying chamber 2a side and the combustion chamber 2b side of the fluidized bed 2f can be smoothly and relatively displaced.

[Operation method of wet biomass incinerator 2]
An operation method of the wet biomass incinerator 2 will be exemplified. FIG. 2 is a diagram illustrating an operating method according to the relationship between the calorific value and the water content of the biomass 25 of the wet biomass incinerator 2 of FIG. As shown in FIG. 2, the calorific value per unit weight of the solid content of the biomass 25 (hereinafter, simply referred to as the calorific value of the biomass 25) is a value equal to or higher than the lower limit value of the reference range of the calorific value, Moreover, when the moisture content value of the biomass 25 in the drying chamber 2a is a value equal to or lower than the upper limit value of the reference range of the moisture content, the wet biomass incinerator 2 includes the first flow rate control valve V1 and the second flow rate control valve V2. Is operated by the normal operation method set to the fully open state.

  The calorific value of the biomass 25 is a value equal to or higher than the lower limit value of the reference range of the calorific value, and the moisture content value of the biomass 25 in the drying chamber 2a is larger than the upper limit value of the reference range of the moisture content. In some cases, the wet biomass incinerator 2 is operated by the first operation method described below by adjusting the second flow rate control valve V2.

  The calorific value of the biomass 25 is less than the lower limit of the reference range of the calorific value, and the moisture content of the biomass 25 in the drying chamber 2a is less than or equal to the upper limit of the reference range of the moisture. In this case, the wet biomass incinerator 2 is operated by the second operation method described below by adjusting the first flow rate control valve V1.

  When the calorific value of the biomass 25 is less than the lower limit of the reference range of calorific value and the moisture content value is larger than the upper limit of the reference range of moisture content, the wet biomass incineration is performed. The furnace 2 is operated by the third operation method described below using the auxiliary fuel.

  As described above, in the wet biomass incineration system 1, by changing the operation method of the wet biomass incinerator 2 according to the relationship between the calorific value and the water content of the biomass 25, the drying chamber 2a and the combustion chamber 2b of the wet biomass incinerator 2 are changed. The temperature is efficiently stabilized.

  Next, the first operation method of the wet biomass incinerator 2 will be specifically exemplified. FIG. 3 is a diagram showing a process of a first operation method of the wet biomass incinerator 2 of FIG. FIG. 4 is a diagram showing a relative displacement of the fluidized bed heights of the fluidized bed 2f on the drying chamber 2a side and the combustion chamber 2b side when the wet biomass incinerator 2 of FIG. 1 is operated by the first operation method. .. In FIG. 4, broken line L indicates the height of each fluidized bed of the fluidized bed 2f on the drying chamber 2a side and the combustion chamber 2b side during the normal operation of the wet biomass incinerator 2.

  As shown in FIG. 3, in the first operating method, the control device 3 first sets the first flow rate control valve V1 and the second flow rate control valve V2 to the fully open state based on the control program (step S1). In this state, the control device 3 monitors each measurement value of the steam flow meter D1, the drying chamber thermometer D2, and the combustion chamber thermometer D3 while controlling the wet biomass incinerator 2 to normally operate.

Since the measurement value of the steam flow meter D1 is larger than the steam flow rate upper limit value F _MAX which is the upper limit value of the standard range of the steam flow rate, the control device 3 determines that the moisture content value of the biomass 25 in the drying chamber 2a is high. Is greater than a predetermined first moisture content upper limit value (in this embodiment, the moisture content upper limit value M _{MAX in} the reference range of the moisture content), and from the measurement value of the drying chamber thermometer D2. When it is determined that the temperature in the drying chamber 2a is lower than the lower limit temperature Q _MIN of the reference temperature range, the temperature in the drying chamber 2a of the wet biomass incinerator 2 is temporarily increased because the moisture content of the biomass 25 is temporarily increased. It is difficult to raise the temperature, and it is determined that the temperature on the drying chamber 2a side of the wet biomass incinerator 2 needs to be increased. Further, the control device 3 determines from the measurement value of the combustion chamber thermometer D3 that the temperature in the combustion chamber 2b is equal to or higher than the lower limit temperature T _MIN of the reference temperature range, so that the calorific value of the biomass 25 is predetermined. It is determined that the value is equal to or larger than the first lower limit value of heat generation amount (lower limit value C _MIN of heat generation amount in the reference range of heat generation amount in the present embodiment) (step S2).

  In this way, the moisture content value of the biomass 25 in the drying chamber 2a is a value larger than the predetermined first moisture content upper limit value, and the calorific value of the biomass 25 is the first predetermined value. When the value is equal to or higher than the lower limit value of the heat generation amount, the control device 3 sets the one valve to the second flow rate control valve V2. Specifically, the control device 3 controls the second flow rate adjusting valve V2 and adjusts the opening degree of the second flow rate adjusting valve V2 so that the opening degree of the second flow rate adjusting valve V2 becomes a predetermined amount. The opening is narrower than the opening of V1 (step S3). Here, for example, the control device 3 holds the first flow rate control valve V1 in a fully open state, and the combustion flow rate of the second flow rate control valve V2 is controlled so that the combustion exhaust gas flow rate value falls within a predetermined range. Reduce the opening. The combustion exhaust gas flow rate value at this time can be adjusted as appropriate, but for example, a value in the range of 60% or more and 98% or less of the fully opened state of the second flow rate control valve V2 is desirable, and in the range of 70% or more and 95% or less. Is more desirable, and values in the range of 80% to 90% are even more desirable.

  Here, the desiccant gas that has circulated through the desiccant gas supply path R2 is continuously supplied into the drying chamber 2a, and the combustion agent gas that has circulated through the combustion agent gas supply path R3 continues within the combustion chamber 2b. Is being supplied to the public. Therefore, the control device 3 can make the combustion chamber freeboard pressure higher than the drying chamber freeboard pressure by narrowing the opening degree of the second flow rate regulating valve V2 smaller than the opening degree of the first flow rate regulating valve V1. it can. Thereby, the control device 3 utilizes the fluidity of the fluid medium 20 to determine the fluidized bed height of the fluidized bed 2f on the drying chamber 2a side and the fluidized bed height of the fluidized bed 2f on the combustion chamber 2b side in a drying chamber-free manner. The relative displacement is promptly performed in the direction in which the difference between the board pressure and the combustion chamber freeboard pressure is reduced. As shown in FIG. 4, specifically, the control device 3 narrows the opening degree of the second flow rate adjusting valve V2 to be smaller than the opening degree of the first flow rate adjusting valve V1, so that the fluidized medium 20 and the biomass in the combustion chamber 2b are reduced. A part of 25 is quickly moved from the combustion chamber 2b side to the drying chamber 2a side, and the fluidized bed height h1 on the drying chamber 2a side is displaced higher than the fluidized bed height h2 on the combustion chamber 2b side.

  The control device 3 determines that the fluidized medium 20 and the biomass 25 have moved due to the relative displacement by a differential pressure gauge arranged below the fluidized bed 2f in at least one of the drying chamber 2a and the combustion chamber 2b. (Step S4). Specifically, the control device 3 determines that the measurement value of the drying chamber differential pressure gauge D4 is larger than a predetermined measurement value as compared with before the control of the second flow rate control valve V2 in step S3, or the combustion chamber differential pressure gauge. By determining that the measured value of D5 is lower than the predetermined measured value, it is determined that part of the fluidized medium 20 and the biomass 25 in the combustion chamber 2b has moved to the drying chamber 2a.

  As described above, in the first operation method, the temperature of the wet biomass incinerator 2 on the drying chamber 2a side is low because the moisture amount value of the biomass 25 in the drying chamber 2a is larger than the first moisture amount upper limit value. In the above, since the calorific value of the biomass 25 is a value equal to or higher than the first lower calorific value, the calorific value is relatively high, and a part of the biomass 25 burned at a high temperature in the combustion chamber 2b is By moving a part of the high temperature fluidized medium 20 in 2b into the drying chamber 2a, the drying chamber 2a side of the wet biomass incinerator 2 is promoted while promoting the drying of the biomass 25 in the drying chamber 2a quickly and efficiently. Makes it easier to raise the temperature.

  Specifically, when it is desired to increase the temperature of the drying chamber 2a side of the wet biomass incinerator 2, the opening degree of the second flow rate control valve V2 should be narrower than that of the first flow rate control valve V1. By adjusting the 2 flow rate control valve V2, a part of the fluidized medium 20 and the biomass 25 in the combustion chamber 2b is moved into the drying chamber 2a, and the amount of the biomass 25 in the drying chamber 2a is changed to the amount of the fluidized medium 20. Can increase with Therefore, the high temperature fluidized medium 20 and the biomass 25 that have moved from the combustion chamber 2b side to the drying chamber 2a side are mixed with the fluidized medium 20 and the biomass 25 in the drying chamber 2a, while efficiently promoting the drying of the biomass 25. The temperature of the drying chamber 2a side of the wet biomass incinerator 2 can be quickly and easily increased. As a result, the resistance of the wet biomass incinerator 2 to temperature fluctuations is increased.

  Further, by keeping the moving speed of the fluidized medium 20 and the biomass 25 moving from the drying chamber 2a side to the combustion chamber 2b side through the lower end of the partition wall 2c constant, the second flow rate control valve V2 is set as described above. By adjusting, the residence time of the high temperature fluidized medium 20 and the biomass 25 moved from the combustion chamber 2b side to the drying chamber 2a side can be increased in the drying chamber 2a, and the drying chamber 2a of the wet biomass incinerator 2 can be increased. The drying time of the biomass on the side can be lengthened.

The control device 3 determines that the water content value of the biomass 25 has become the water content upper limit value M _MAX or less, since the measured value of the steam flow meter D1 becomes the steam flow value upper limit value F _MAX or less. From the measurement value of the drying chamber thermometer D2, it is determined that the temperature in the drying chamber 2a is equal to or higher than the lower limit temperature Q _MIN . As a result, the control device 3 determines that the property of the biomass 25 has returned to the proper state (step S5).

  After that, the control device 3 gently returns the opening degree of the second flow rate control valve V2 to the fully opened state (step S6). As a result, the difference between the fluidized bed height h1 on the drying chamber 2a side and the fluidized bed height h2 on the combustion chamber 2b side is reduced, and the state of the wet biomass incinerator 2 is shifted to the normal operation state.

In addition, if the calorific value of the biomass 25 is low to some extent, it is possible that the temperature in the drying chamber 2a is unlikely to rise even if step S3 is started. In this case, the control device 3 extends the time from the start of step S3 until it is determined in step S5 that the temperature in the drying chamber 2a has become equal to or higher than the lower limit temperature Q _MIN from the measurement value of the drying chamber thermometer D2. This can be handled by setting to.

In addition, it takes a long time after the control device 3 performs step S3 and confirms in step S5 that the temperature in the drying chamber 2a is equal to or higher than the lower limit temperature Q _{MIN based on} the measurement value of the drying chamber thermometer D2. In this case, the control device 3 may supply the auxiliary fuel into the combustion chamber 2b from the auxiliary fuel supply passage R7 to raise the temperature of the combustion chamber 2b. In this case, the control device 3 determines that the part of the fluidized medium 20 and the biomass 25 in the combustion chamber 2b has moved from the side of the combustion chamber 2b to the side of the drying chamber 2a. When it is determined that the temperature in 2a has become _{equal to} or higher than the lower limit temperature Q _MIN , the supply of auxiliary fuel is stopped and the state of the wet biomass incinerator 2 is shifted to the state of normal operation.

  Next, the second operation method of the wet biomass incinerator 2 will be specifically exemplified. FIG. 5: is a figure which shows the process of the 2nd operating method of the wet biomass incinerator 2 of FIG. FIG. 6 is a diagram showing a relative displacement of each fluidized bed height of the fluidized bed 2f on the drying chamber 2a side and the combustion chamber 2b side when the wet biomass incinerator 2 of FIG. 1 is operated by the second operation method. .. Similar to FIG. 4, in FIG. 6, the fluidized bed heights of the fluidized bed 2f on the drying chamber 2a side and the combustion chamber 2b side during the normal operation of the wet biomass incinerator 2 are indicated by broken lines L.

  As shown in FIG. 5, in the second operation method, the control device 3 first sets the first flow rate control valve V1 and the second flow rate control valve V2 to the fully open state, as in step S1 (S11). In this state, the control device 3 monitors each measurement value of the steam flow meter D1 and the combustion chamber thermometer D3 while controlling the wet biomass incinerator 2 to normally operate.

Since the measurement value of the steam flow meter D1 is a value equal to or lower than the steam flow rate upper limit value F _MAX , the control device 3 determines that the moisture content value of the biomass 25 in the combustion chamber 2b is the second moisture content upper limit value set in advance. (In this embodiment, when it is determined that the water content is the upper limit value M _MAX or less) and the temperature in the combustion chamber 2b is determined to be less than the lower limit temperature T _MIN from the measurement value of the combustion chamber thermometer D3. Since the calorific value of the biomass 25 is temporarily below the predetermined second calorific value lower limit value (the calorific value lower limit value C _{MIN in the} present embodiment) of the wet biomass incinerator 2, It is difficult to raise the temperature in the combustion chamber 2b, and it is determined that the temperature on the combustion chamber 2b side of the wet biomass incinerator 2 needs to be increased (step S12).

  As described above, the moisture content value of the biomass 25 in the combustion chamber 2b is equal to or less than the predetermined second moisture content upper limit value, and the calorific value of the biomass 25 is equal to the predetermined second heat generation value. When the value is less than the amount lower limit value, the control device 3 sets the one valve to the first flow rate control valve V1. Specifically, the control device 3 controls the first flow rate control valve V1, and controls the opening degree of the first flow rate control valve V1 so that the opening degree of the first flow rate control valve V1 becomes a predetermined amount. The aperture is narrowed down from the opening of V2 (step S13). Here, the control device 3, for example, keeps the second flow rate control valve V2 in a fully open state, and controls the first flow rate control valve V1 so that the dry exhaust gas flow rate value of the first flow rate control valve V1 is within a predetermined range. Reduce the opening. The dry exhaust gas flow rate value at this time can be appropriately adjusted, but for example, a value in the range of 55% or more and 93% or less of the fully opened state of the first flow rate control valve V1 is desirable, and a value of 65% or more and 90% or less Is more desirable, and a value in the range of 75% to 85% is even more desirable.

  The control device 3 makes the opening amount of the first flow rate control valve V1 smaller than the opening amount of the second flow rate control valve V2 to increase the dry chamber freeboard pressure as compared with the combustion chamber freeboard pressure. As shown in FIG. 6, as a result, the control device 3 causes the fluidized medium 20 and a part of the biomass 25 in the drying chamber 2a to quickly move from the drying chamber 2a side to the combustion chamber 2b side, contrary to the first operation method. The fluidized bed height h2 on the combustion chamber 2b side is displaced higher than the fluidized bed height h1 on the drying chamber 2a side.

  The control device 3 determines that the measured value of the combustion chamber differential pressure gauge D5 is larger than the predetermined value as compared with before the control of the first flow rate control valve V1 in step S13, or the measured value of the dry chamber differential pressure gauge D4 is By determining that it has become smaller than the predetermined value, it is determined that part of the fluidized medium 20 and the biomass 25 in the drying chamber 2a has moved to the combustion chamber 2b (step S14).

  As described above, in the second operation method, when the temperature of the combustion chamber 2b side of the wet biomass incinerator 2 is low because the calorific value of the biomass 25 is less than the second calorific value lower limit value, the inside of the drying chamber 2a is low. Part of the biomass 25 having a relatively low water content value due to the water content value being less than or equal to the second water content upper limit value is moved into the combustion chamber 2b together with part of the fluidized medium 20 in the drying chamber 2a. By doing so, the temperature of the combustion chamber 2b side of the wet biomass incinerator 2 can be easily increased while promptly and efficiently promoting the combustion of the biomass 25 in the combustion chamber 2b.

  Specifically, when it is desired to increase the temperature of the combustion chamber 2b side of the wet biomass incinerator 2, the first flow rate is adjusted so that the opening degree of the first flow rate adjusting valve V1 is narrower than that of the second flow rate adjusting valve V2. By adjusting the control valve V1, a part of the fluidized medium 20 and the biomass 25 in the drying chamber 2a is moved into the combustion chamber 2b, and the amount of the biomass 25 in the combustion chamber 2b increases with the amount of the fluidized medium 20. it can. Therefore, the fluidized medium 20 and the biomass 25 that have moved from the drying chamber 2a side to the combustion chamber 2b side are mixed with the fluidized medium 20 and the biomass 25 in the combustion chamber 2b to efficiently promote the combustion of the biomass 25 and wet biomass. The temperature on the combustion chamber 2b side of the incinerator 2 can be easily increased quickly. As a result, the resistance of the wet biomass incinerator 2 to temperature fluctuations is increased.

The control device 3 determines from the measurement value of the combustion chamber thermometer D3 that the temperature in the combustion chamber 2b is equal to or higher than the lower limit temperature T _MIN , so that the calorific value of the biomass 25 is equal to or higher than the lower limit value C _{MIN of the} calorific value. It is determined that the value has been reached. As a result, the control device 3 determines that the property of the biomass 25 has returned to the proper state (step S15).

  After that, the control device 3 gently returns the opening degree of the first flow rate control valve V1 to the fully open state (step S16), and sets the fluidized bed height h1 on the drying chamber 2a side and the fluidized bed height h2 on the combustion chamber 2b side. The difference is reduced to shift the state of the wet biomass incinerator 2 to the state of normal operation.

It should be noted that if the amount of water in the biomass 25 is large to some extent, it may be difficult for the temperature in the combustion chamber 2b to rise even after starting step S13. In this case, in step S15, increase the time from when the control device 3 starts step S13 to when it is determined from the measurement value of the combustion chamber thermometer D3 that the temperature in the combustion chamber 2b becomes equal to or higher than the lower limit temperature T _MIN. This can be handled by setting to.

  Next, the third operating method of the wet biomass incinerator 2 will be specifically exemplified. FIG. 7: is a figure which shows the process of the 3rd operating method of the wet biomass incinerator 2 of FIG. As shown in FIG. 7, in the third operating method, the control device 3 first sets the first flow rate control valve V1 and the second flow rate control valve V2 to the fully open state (step S21) and wets, as in step S1. While controlling the biomass incineration system 1 to operate, each measurement value of the steam flow meter D1 and the combustion chamber thermometer D3 is monitored.

Since the measurement value of the steam flow meter D1 is larger than the steam flow rate upper limit value F _MAX , the control device 3 determines that the water content value of the biomass 25 in the drying chamber 2a is the predetermined third water content. It is determined that the value is larger than the value (water content upper limit value M _{MAX in the} present embodiment), and it is determined from the measurement value of the combustion chamber thermometer D3 that the temperature in the combustion chamber 2b is lower than the lower limit temperature T _MIN. By doing so, it is determined that the value of the calorific value of the biomass 25 is less than a predetermined third calorific value lower limit value (the calorific value lower limit value C _{MIN in the} present embodiment). Thereby, the control device 3 determines that the calorific value of the biomass 25 is less than the calorific value lower limit value C _MIN and the moisture content value is larger than the moisture content upper limit value M _MAX , so that the combustion chamber 2b. It is difficult to raise the internal temperature, and it is determined that the temperature on the combustion chamber 2b side of the wet biomass incinerator 2 needs to be increased (step S22).

The control device 3 supplies the auxiliary fuel from the auxiliary fuel supply path R7 into the combustion chamber 2b, promotes the combustion of the biomass 25, and raises the temperature in the combustion chamber 2b (step S23). The control device 3 determines from the measurement value of the combustion chamber thermometer D3 that the temperature in the combustion chamber 2b is equal to or higher than the lower limit temperature T _MIN , and thus determines that the property of the biomass 25 has returned to an appropriate state (step S24). After that, the control device 3 stops the supply of the auxiliary fuel from the auxiliary fuel supply passage R7 into the combustion chamber 2b, and shifts the state of the wet biomass incinerator 2 to the normal operating state (step S25).

Here, the lower limit temperature Q _MIN , T _MIN , the vapor flow rate upper limit value F _MAX , the moisture content upper limit value M _MAX , and the calorific value lower limit value C _MIN are the wet biomass incinerator 2 in the normal operating state of the wet biomass incinerator 2. Can be appropriately set according to the reference temperature ranges of the drying chamber 2a and the combustion chamber 2b, the respective volumes of the drying chamber 2a and the combustion chamber 2b, the characteristics of the biomass 25, and the like. The water content upper limit value M _MAX can be set to, for example, a value larger than the water content upper limit value at which the biomass 25 can self-combust in the combustion chamber 2b. Further, the lower limit value of calorific value C _MIN is, for example, a calorific value value at which the temperature in the combustion chamber 2b does not fall below 800 ° C. when the biomass 25 having a moisture content upper limit value M _MAX or less is combusted in the combustion chamber 2b. Can be set.

  As described above, since the wet biomass incinerator 2 can be operated by the first operation method or the second operation method in addition to the normal operation method or the third operation method, it is supplied to the wet biomass incinerator 2. Even if the water content of the biomass 25 and the calorific value of the biomass 25 temporarily fluctuate, the wet bed biomass is relatively displaced by relatively displacing the fluidized bed heights of the fluidized bed 2f on the drying chamber 2a side and the combustion chamber 2b side. The temperature of the drying chamber 2a and the combustion chamber 2b of the incinerator 2 can be easily adjusted quickly. Therefore, the wet biomass incinerator 2 can be driven at a stable temperature, the running cost is low, and the wet biomass incinerator system 1 can be operated with good combustion efficiency.

  Further, since the wet biomass incineration system 1 is equipped with the steam flow meter D1, the water content of the biomass 25 in the drying chamber 2a can be easily confirmed from the measurement value of the steam flow meter D1. Further, since the wet biomass incineration system 1 includes the combustion chamber thermometer D3, the calorific value of the biomass 25 in the combustion chamber 2b can be easily confirmed from the measurement value of the combustion chamber thermometer D3. Moreover, since the wet biomass incineration system 1 includes the drying chamber thermometer D2, the temperatures of the biomass 25 and the fluidized medium 20 in the drying chamber 2a can be easily confirmed from the measurement values of the drying chamber thermometer D2.

  Moreover, since the wet biomass incineration system 1 includes the differential pressure gauge (the drying chamber differential pressure gauge D4 and the combustion chamber differential pressure gauge D5 in the present embodiment), among the first flow rate control valve V1 and the second flow rate control valve V2, When the gas flow rate of one valve becomes lower than a predetermined value, the movement of the fluidized medium 20 and the biomass 25 between the drying chamber 2a and the combustion chamber 2b can be easily confirmed from the change in the measured value of the differential pressure gauge. ..

  The present invention is not limited to the above-mentioned embodiment, and its configuration can be changed, added, or deleted without departing from the spirit of the present invention. At least two of the first water content, the second water content, and the third water content may have different values. Further, at least one of the first flow rate control valve V1 and the second flow rate control valve V2 may be manually controlled by the operator of the wet biomass incineration system 1.

C _MIN calorific value lower limit value (first calorific value lower limit value, second calorific value lower limit value)
D1 Steam flow meter D2 Drying room thermometer (thermometer)
D3 Combustion chamber thermometer (thermometer)
D4 Drying chamber differential pressure gauge (differential pressure gauge)
D5 Combustion chamber differential pressure gauge (differential pressure gauge)
M _MAX water content upper limit value (first water content upper limit value, second water content upper limit value)
R2 desiccant gas supply path R3 combustion agent gas supply path R4 dry exhaust gas discharge path R5 combustion exhaust gas discharge path V1 First flow rate control valve V2 Second flow rate control valve 1 Wet biomass incinerator 2 Wet biomass incinerator 2a Drying room 2b Combustion chamber 2c Partition wall 2f Fluidized bed 15, 16 Upper space 20 Fluidized medium 25 Biomass

Claims (12)

A drying chamber and a combustion chamber, a fluidized bed containing a fluidized medium that flows over the lower part of the drying chamber and the lower part of the combustion chamber, a space above the fluidized bed of the drying chamber and above the fluidized bed of the combustion chamber. A wet biomass incinerator having a space and a partition wall having a lower end arranged in the fluidized bed,
From the lower side of the fluidized bed on the drying chamber side, a desiccant gas supply path for supplying a desiccant gas for drying biomass in the drying chamber while mixing with the fluid medium into the drying chamber,
Combustion agent gas for supplying, into the combustion chamber, a combustion agent gas for burning the biomass dried in the drying chamber while mixing with the fluidized medium in the combustion chamber, from below the fluidized bed on the combustion chamber side. Supply channel,
A first flow rate control valve which is provided in a dry exhaust gas discharge passage communicating with the upper space of the drying chamber and which controls a flow rate of the dry exhaust gas discharged from the upper space of the drying chamber to the outside of the drying chamber;
A second flow rate control valve that is provided in a combustion exhaust gas discharge path communicating with the upper space of the combustion chamber and that controls a flow rate of the combustion exhaust gas discharged from the upper space of the combustion chamber to the outside of the combustion chamber;
Of the first flow rate control valve and the second flow rate control valve, the opening degree of one valve is narrower than the opening degree of the other valve, so that one of the drying chamber and the combustion chamber is opened. The fluidized bed height of the fluidized bed on one chamber side provided with a valve and the fluidized bed height of the fluidized bed on the other chamber side provided with the other valve are the upper space of the one chamber. And the gas pressure of the other chamber is adjusted to be relatively displaced in a direction in which the difference between the gas pressure of the upper space is reduced ,
The moisture content value of the biomass in the drying chamber is a value larger than a predetermined first moisture content upper limit value, and the calorific value of the solid content of the biomass per unit weight is predetermined. If a first heating value lower limit value greater than the the one of the valves ing a second flow control valve, wet biomass incineration system. A moisture content value of the biomass in the combustion chamber is less than or equal to a predetermined second moisture content upper limit value, and a calorific value of the solid content of the biomass per unit weight is a predetermined value. The wet biomass incineration system according to claim 1, wherein the one valve serves as the first flow rate control valve when the calorific value is less than the lower limit value of the two calorific values . The wet biomass incineration system according to claim 1, further comprising a steam flow meter that measures a steam flow rate of the dry exhaust gas discharged to the outside of the drying chamber . Further comprising a combustion chamber thermometer disposed in the combustion chamber, the wet biomass incineration system according to any one of claims 1 to 3. The wet biomass incineration system according to claim 1, further comprising a drying chamber thermometer disposed in the drying chamber . The differential pressure change between the gas pressure of the one chamber and the pressure that extends downward from the upper side to the bottom of the fluidized bed on the side of the one chamber, and the gas pressure of the other chamber. , A differential pressure gauge for measuring the moving amount of the fluid medium and the biomass by at least one of the differential pressure change with the pressure that extends downward from the bottom of the fluidized bed on the side of the other chamber. The wet biomass incineration system according to any one of claims 1 to 5, further comprising: A drying chamber and a combustion chamber, a fluidized bed containing a fluidized medium that flows over the lower part of the drying chamber and the lower part of the combustion chamber, a space above the fluidized bed of the drying chamber and above the fluidized bed of the combustion chamber. A wet biomass incinerator having a space and a partition wall having a lower end arranged in the fluidized bed,
From the lower side of the fluidized bed on the drying chamber side, a desiccant gas supply path for supplying a desiccant gas for drying biomass in the drying chamber while mixing with the fluid medium into the drying chamber,
Combustion agent gas for supplying, into the combustion chamber, a combustion agent gas for burning the biomass dried in the drying chamber while mixing with the fluidized medium in the combustion chamber, from below the fluidized bed on the combustion chamber side. Supply channel,
A first flow rate control valve which is provided in a dry exhaust gas discharge passage communicating with the upper space of the drying chamber and which controls a flow rate of the dry exhaust gas discharged from the upper space of the drying chamber to the outside of the drying chamber;
A second flow rate control valve that is provided in a combustion exhaust gas discharge path communicating with the upper space of the combustion chamber and that controls a flow rate of the combustion exhaust gas discharged from the upper space of the combustion chamber to the outside of the combustion chamber. In the biomass incineration system,
Of the first flow rate control valve and the second flow rate control valve, the opening degree of one valve is narrower than the opening degree of the other valve, so that the one valve of the drying chamber and the combustion chamber is closed. The height of the fluidized bed of the fluidized bed on the side of one chamber provided with and the height of the fluidized bed of the fluidized bed on the side of the other chamber where the other valve is provided are Relative displacement in a direction in which the difference between the gas pressure and the gas pressure in the upper space of the other chamber is reduced,
The moisture content value of the biomass in the drying chamber is a value larger than a predetermined first moisture content upper limit value, and the calorific value of the solid content of the biomass per unit weight is predetermined. A method of operating a wet biomass incinerator in which the one valve is the second flow rate control valve when the value is equal to or higher than the first lower limit value of the calorific value . A moisture content value of the biomass in the combustion chamber is less than or equal to a predetermined second moisture content upper limit value, and a calorific value of the solid content of the biomass per unit weight is a predetermined value. The method for operating a wet biomass incinerator according to claim 7 , wherein when the value is less than the lower limit value of the two calorific values, the one valve is the first flow control valve. The method for operating a wet biomass incinerator according to claim 7 or 8 , wherein the moisture content of the biomass in the drying chamber is confirmed by a steam flow meter that measures a steam flow rate of the dry exhaust gas discharged to the outside of the drying chamber. The temperature of the combustion chamber, said measured by combustion chamber disposed combustion chamber thermometer, a method of operating wet biomass incinerator according to any one of claims 7-9. The method for operating a wet biomass incinerator according to claim 7 , wherein the temperature in the drying chamber is measured by a drying chamber thermometer arranged in the drying chamber. The differential pressure change between the gas pressure of the one chamber and the pressure that extends downward from the upper side to the bottom of the fluidized bed on the side of the one chamber, and the gas pressure of the other chamber. , Using a differential pressure gauge for measuring the moving amount of the fluid medium and the biomass by at least one of the differential pressure change from the pressure applied from the upper side to the lower side of the bottom of the fluidized bed on the side of the other chamber The method of operating the wet biomass incinerator according to claim 7 , wherein movement of the fluidized medium and the biomass due to the relative displacement is confirmed.

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