WO2017131235A1

WO2017131235A1 - Biomass power generation system, and return system for thermal decomposition furnace

Info

Publication number: WO2017131235A1
Application number: PCT/JP2017/003223
Authority: WO
Inventors: 光幸飯嶋; 佐藤　秀雄
Original assignee: 株式会社高橋製作所
Priority date: 2016-01-29
Filing date: 2017-01-30
Publication date: 2017-08-03
Also published as: JP6170579B1; JP2017132969A

Abstract

Provided is a safe and efficient biomass power generation system that improves the combustion efficiency of biomass and makes stable thermal decomposition possible, that prevents outflow of combustion gas, etc., and with which the composition ratio of water gas to be supplied to a downstream device does not vary. The system is provided with: a carbonization furnace for carbonizing biomass; a thermal decomposition furnace for generating thermal decomposition gas from combustion exhaust gas and carbides obtained in the carbonization furnace; and a power generation device for obtaining electric power using the water gas obtained by washing the thermal decomposition gas. The system is provided with an air supply control unit for controlling the amount of air to be supplied to the carbonization furnace. Combustion gas that is temperature-controlled by the supply amount of air is supplied to the thermal decomposition furnace.

Description

Biomass power generation system and pyrolysis furnace return system

The present invention relates to a biomass power generation system and a pyrolysis furnace return system, and in particular, thermally decomposes and gasifies biomass (organic waste such as waste wood), and efficiently generates power using a gas engine or the like using the obtained water gas. The present invention relates to a biomass power generation system, and also relates to a return system in a pyrolysis furnace.

In recent years, pyrolysis gasification of woody materials containing a large amount of biomass, particularly lignin, has great potential as a source of new energy resources, and attempts have been made to effectively use it. In order to pyrolyze and convert wood-based materials into pyrolysis gas, the raw wood biomass is recovered at a carbonization furnace temperature of 1000 to 1200 ° C., and then the carbides are heated to a high temperature in a pyrolysis furnace, so that high-temperature steam and aqueous React to produce water gas.

As an alternative energy resource to replace fossil fuels, a method of recovering energy from biomass and waste by thermochemical techniques has attracted attention. In addition to steam turbine power generation using boiler facilities, a gas engine with high power generation efficiency using generated gas as fuel gas The power generation efficiency is over 35%. In addition, since the synthesis gas obtained by gasification also becomes a raw material for liquid fuels such as methanol, synthetic light oil, and mixed alcohols, gasification technology is attracting attention as one of petroleum alternative combustion technologies.

In biomass power generation, a gas engine, a gas turbine engine, a steam turbine engine, or the like is used. Among them, the structure of a gas engine is the same as that of a gasoline engine, and it is more compact (about 50 to 4000 kW) than other engines, has high power generation efficiency, and is suitable for biomass power generation. However, the heat generation amount of the pyrolysis gas (water gas) is determined by the content ratio of the combustible gas (CO, H ₂ ) in the gas. That is, if the composition ratio of hydrogen (H ₂ ), carbon monoxide (CO), and carbon dioxide (CO ₂ ) in the water gas varies, the amount of generated heat changes, which affects the number of revolutions of the engine that rotates the generator. As a result, not only stable power is not obtained, but also overheating causes a failure, which is a problem. In addition, it is conceivable to supply steam generated in a conventional boiler directly to the pyrolysis gasifier, but there is a possibility that the temperature distribution in the gasification region may be blurred due to excess or shortage of heat or excessive gas such as methane gas may be generated. There is a problem that occurs.

Therefore, the applicant of the present invention does not reduce the temperature of the gasification region by heating the steam generated in the boiler and supplying the high-temperature superheated steam to the gasification region of the pyrolysis gasifier, and the high temperature of the carbonization furnace. Proposed a biomass power generation system that can stabilize the temperature distribution in the region by synergistic effects with the radiant heat of the exhaust gas, make the composition ratio of the water gas more uniform, and prevent the generation of methane gas, etc. in the water gas component. Patent application 1 has been filed.

Japanese Patent Laying-Open No. 2015-165019

As a carbonization furnace suitable for use in the biomass power generation system invented and proposed earlier, a solid content containing a large amount of carbides is carbonized above a region formed between a substantially circular main body and a cylindrical body accommodated in the main body. The carbonized part is formed, and the incombustible part that extinguishes the carbide is formed below, but the amount of air supplied to the upper combustion part fluctuates and the air suitable for burning the combustible gas If not, the combustion efficiency of combustible gas will deteriorate.

Also, as a pyrolysis gasification furnace (pyrolysis furnace), an outer cylinder and an inner cylinder are provided, carbide and a gasifying agent are supplied to the inner peripheral side of the inner cylinder, and a gap between the outer cylinder and the inner cylinder The combustion gas generated in the carbonization furnace is supplied to the cylinder, but the length varies along the vertical direction due to the thermal expansion of the inner cylinder. If there is a difference in thermal expansion between the inner cylinder and the outer cylinder, the combustion gas may flow out from the portion where the inner cylinder, the outer cylinder and the upper surface are in contact with each other.

Due to a decrease in combustion efficiency or outflow of combustion gas, the composition ratio of the water gas supplied to the downstream equipment may fluctuate, causing malfunctions in each device and system balance, resulting in a decrease in efficiency of the entire power generation system. Resulting in.

It is an object of the present invention to solve such problems and provide a safe and efficient biomass power generation system, and further to provide a return system in a pyrolysis furnace for generating water gas used for biomass power generation and the like. And

In order to solve the above-described problems, the present invention provides a carbonization furnace for carbonizing biomass, a pyrolysis furnace for generating pyrolysis gas from the carbide and combustion gas obtained in the carbonization furnace, and cleaning the pyrolysis gas. And a power generation device that obtains electric power using the obtained water gas, and is provided with an air supply control unit that controls the supply amount of air supplied to the carbonization furnace, and the combustion gas whose temperature is controlled by the supply amount of air The present invention provides a biomass power generation system characterized in that the is supplied to a pyrolysis furnace.

According to the present invention, an appropriate amount of air can be controlled, combustion efficiency can be maintained stably at a high level, and it can contribute to stabilization to a downstream apparatus.

The present invention also includes a carbonization furnace that carbonizes biomass, a pyrolysis furnace that generates pyrolysis gas using the carbide and combustion gas obtained in the carbonization furnace, and a water gas obtained by washing the pyrolysis gas. The pyrolysis furnace includes a cylindrical main body part, a reaction tube protruding from the upper end of the main body part inside the main body part, and an inner wall of the main body part, A space between the outer peripheral surfaces of the reaction tubes is used as a heating flow path, the inside of the reaction tube is used as a reaction part of a carbide and a gasifying agent, and the water gas is supplied to a power supply device using the obtained decomposition gas. A biomass power generation system is provided.

According to the present invention, the water gas (reactive gas) from the pyrolysis furnace does not flow out to the outside, and the system can be stabilized.

The present invention also includes a carbonization furnace that carbonizes biomass, a pyrolysis furnace that generates pyrolysis gas using the carbide and combustion gas obtained in the carbonization furnace, and a water gas obtained by washing the pyrolysis gas. And a power generation device that obtains electric power by using an air supply control unit that controls a supply amount of air supplied to the carbonization furnace, and the pyrolysis furnace includes a cylindrical main body part and an inner part of the main body part. A reaction tube protruding from the upper end of the main body, and supplying a combustion gas whose temperature is controlled by the amount of air supplied to the pyrolysis furnace in the carbonization furnace; in the pyrolysis furnace, the inner wall of the main body And the outer peripheral surface of the reaction tube as a heating flow path, the combustion exhaust gas from the carbonization furnace is input, and the carbide from the carbonization furnace is input into the reaction tube and obtained by reaction with the gasifying agent. Using the cracked gas It is intended to provide a biomass power generation system characterized by supplying gas to the power supply.

According to the present invention, water gas can be stably supplied using biomass as a raw material.

In the present invention, the pyrolysis furnace includes a cylindrical main body portion, and a reaction tube protruding from the upper end of the main body portion inside the main body portion, and an inner wall of the main body portion and an outer peripheral surface of the reaction tube. A system for obtaining a water gas by using the obtained cracked gas, wherein the inside of the reaction tube is a reaction part of a carbide and a gasifying agent, and the inside of the reaction tube is a reaction part of the heating tube. Recovery means for recovering the unreacted material after the reaction with the reaction means, and transport means for transporting the unreacted material from the recovery means to the upper part of the reaction tube of the pyrolysis furnace, and the unreacted material is returned to the pyrolysis furnace again. The present invention provides a return system for a pyrolysis furnace characterized in that it can be charged.

According to the present invention, the reaction efficiency of carbides can be increased, the amount of water gas to be purified can be increased, and the power generation system can be stably operated. Furthermore, further power generation efficiency can be achieved by applying the pyrolysis furnace of the present invention to a biomass power generation system.

According to the present invention, it is possible to improve the combustion efficiency of biomass and enable stable thermal decomposition, prevent outflow of water gas, etc., and there is no variation in the composition ratio as water gas to be supplied to the downstream device, A safe and efficient biomass power generation system can be provided.

Also, according to the present invention, it is possible to provide a return system for a pyrolysis furnace that can increase the reaction efficiency of carbides and increase the amount of purified water gas.

It is a block diagram of a biomass power generation system concerning one embodiment of the present invention. It is a schematic structure figure of a biomass power generation system concerning one embodiment of the present invention. It is a longitudinal cross-sectional view of the carbonization furnace which concerns on one Embodiment of this invention shown in FIG. It is a figure which shows the clinker crusher of the carbonization furnace which concerns on one Embodiment of this invention shown in FIG. 3, (a) is a top view, (b) is a CC arrow end surface figure of (a). FIG. 4 is an end view of the carbonization furnace according to the embodiment of the present invention shown in FIG. 3, (a) is an end view taken along arrow AA, and (b) is an end view taken along arrow BB. It is a longitudinal cross-sectional view which shows the 1st modification of the primary air supply part of the carbonization furnace which concerns on one Embodiment of this invention shown in FIG. It is a longitudinal cross-sectional view which shows the 2nd modification of the primary air supply part of the carbonization furnace which concerns on one Embodiment of this invention shown in FIG. It is a flowchart which shows the control method of the ventilation volume of the secondary combustion fan by the control part of the carbonization furnace which concerns on one Embodiment of this invention. It is a flowchart which shows the control method of the rotational speed of the turntable by the control part of the carbonization furnace which concerns on one Embodiment of this invention. It is a longitudinal cross-sectional view of the thermal decomposition furnace which concerns on one Embodiment of this invention shown in FIG. It is sectional drawing of the reaction tube of the thermal decomposition furnace which concerns on one Embodiment of this invention shown in FIG. 10, (a) is DD arrow sectional drawing, (b) is EE arrow end elevation. It is a principal part enlarged view of the thermal decomposition furnace which concerns on one Embodiment of this invention shown in FIG. It is a block diagram which shows the pyrolysis furnace, temperature reducer, cyclone, steam generator, and steam superheater which concern on one Embodiment of this invention shown in FIG. It is a block diagram of the return system of the pyrolysis furnace which concerns on other embodiment of this invention. It is a block diagram which shows the dryer which concerns on one Embodiment of this invention shown in FIG. It is a block diagram of the biomass power generation system which concerns on other embodiment of this invention.

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

A biomass power generation system according to an embodiment of the present invention is carbonized waste biomass (organic waste), carbonized to produce carbide by carbonization, and then superheated steam (hereinafter also referred to as “steam”). .) As a gasifying agent to produce a water gas (mixed gas mainly composed of hydrogen gas, carbon monoxide gas and carbon dioxide gas) by pyrolyzing the carbide, and this water gas is supplied to a gas engine or This is a system that supplies power to a gas turbine engine to obtain electric power.

Biomass (organic waste) is, for example, food waste, construction waste, shredder dust, livestock waste, wood waste such as thinned wood and pruned branches, sludge, and general waste discharged from households. Various organic wastes as exemplified above can be used as a raw material for generating water gas.

FIG. 1 shows a block diagram of a biomass power generation system according to an embodiment of the present invention, and FIG. 2 shows a schematic configuration diagram of the biomass power generation system according to an embodiment of the present invention. Note that, in contrast to the block diagram of FIG. 1, the schematic configuration diagram of FIG.

As shown in FIGS. 1 and 2, the biomass power generation system A according to an embodiment of the present invention is an organic material in which biomass (organic waste) that is a raw material is crushed into chips by a raw material crusher or the like and is fed into a dryer. Hopper 11 for storing waste, dryer 10 for drying the crushed organic waste, carbonization furnace 20 for generating carbide from the dried organic waste, and carbonization and gasification generated in the carbonization furnace 20 A pyrolysis furnace 30 that thermally decomposes the agent, a temperature reducer 40 that cools the water gas generated in the pyrolysis furnace 30, and a char recovery device 41 that collects unburned carbide discharged from the carbonization furnace 20. A cyclone 50 that removes the residue from the water gas supplied from the temperature reducer 40, a residue recovery device 51 that collects the residue removed by the cyclone 50, and an aqueous gas from which the residue has been removed by the cyclone 50 A water gas cooling device 60 that cools the water, a flare stack 71 that incinerates surplus water gas, and the like, and a power generation facility 72 that obtains electric power by supplying water gas to a gas engine, a gas turbine engine, or the like as fuel are provided. . Moreover, you may provide the hydrogen purification apparatus 73 which refine | purifies hydrogen gas from water gas.

Further, a steam generator 80 that generates saturated steam from water, a steam superheater 81 that superheats steam generated by the steam generator 80, a water supply device 82 that supplies water to the steam generator, and a biomass power generation system A A control device 90 for controlling the whole is provided.

Hereinafter, each part with which biomass power generation system A is provided is explained.

The dryer 10 is an apparatus that dries organic waste with combustion gas and supplies the dried organic waste to a carbonization furnace. The dryer 10 is supplied with organic waste from a hopper 11 that stores the organic waste through a raw material supply path 11a. Moreover, the combustion gas discharged | emitted from the steam generator 80 is supplied to the dryer 10 through the combustion gas flow path 200d as a heat source which dries organic waste.

The organic waste supplied from the hopper 11 to the dryer 10 is, for example, a wooden chip having a length of 5 mm or more and 60 mm or less. In addition, organic waste, for example, reduces moisture contained in organic waste to a weight ratio of about 15% by heating and drying wood chips containing water at a weight ratio of about 55%. is there.

The dryer 10 supplies the organic waste dried by the heat of the combustion gas to the metering feeder 12 through the raw material supply path 10a. Further, the dryer 10 supplies the combustion gas used as a heat source for drying the organic waste to the exhaust gas cooling and cleaning device 13 through the combustion gas channel 200e. The temperature of the combustion gas supplied from the dryer 10 to the exhaust gas cooling and cleaning device 13 is adjusted to be 150 ° C. or higher and 210 ° C. or lower.

The exhaust gas cooling and cleaning device 13 is a scrubber, for example, and is adjusted so that the temperature of the combustion gas discharged into the atmosphere is 120 ° C. or higher and 180 ° C. or lower. In the schematic configuration diagram of FIG. 2, an example of the exhaust gas cooling and cleaning device 13 includes a heat exchanger 13 a, an exhaust gas facility (bug dust collector) 13 b, a waste tower 13 c, and the like. The carbonization furnace 20 is an apparatus that generates carbide and combustion gas by partially burning dry organic waste. The carbonized furnace 20 is supplied with the dried organic waste through the raw material supply path 12a from the quantitative feeder 12 that supplies the organic waste to the carbonized furnace 20 while measuring the supply amount per unit time.

The carbonization furnace 20 supplies the carbide generated by the combustion of the organic waste to the pyrolysis furnace 30 through the carbide supply path 101. The carbide supply path 101 is provided with a clinker removing device (101b described later), a magnetic separator (101d described later), and the like.

Further, the carbonization furnace 20 supplies the combustion gas generated by the combustion of the organic waste to the pyrolysis furnace 30 through the combustion gas flow path 200a.

The pyrolysis furnace 30 is a device that generates water gas by heating the carbide generated by the carbonization furnace 20 together with superheated steam with a combustion gas to cause a thermal decomposition reaction. The pyrolysis furnace 30 is supplied with the carbide generated by the carbonization furnace 20 through the carbide supply path 101. The pyrolysis furnace 30 is supplied with superheated steam heated by the steam superheater 81 as a gasifying agent. The pyrolysis furnace 30 is supplied with combustion gas from the combustion gas channel 200a as a heat source for promoting the pyrolysis reaction.

The pyrolysis furnace 30 causes a pyrolysis reaction of the carbide and superheated steam to generate a water gas mainly composed of hydrogen gas, carbon monoxide gas, and carbon dioxide gas. The thermal decomposition reaction between carbide and superheated steam is a reaction mainly represented by the following formulas (1) and (2).
C + H ₂ O → CO + H ₂ (1)
CO + H ₂ O → CO ₂ + H ₂ (2)

The water gas reaction shown in Formula (1) is an endothermic reaction, and the water gas shift reaction shown in Formula (2) is an exothermic reaction. The endothermic amount of the endothermic reaction shown in formula (1) is larger than the exothermic amount of the exothermic reaction shown in formula (2). Therefore, the thermal decomposition reaction between the carbide and the superheated steam is an endothermic reaction as a whole.

The temperature of the carbide supplied to the pyrolysis furnace 30 is adjusted to be normal temperature (for example, 25 ° C.) or higher and 350 ° C. or lower. Moreover, the temperature of the superheated steam supplied to the pyrolysis furnace 30 is adjusted to be 730 ° C. or more and 830 ° C. or less. The temperature of the combustion gas supplied to the pyrolysis furnace 30 is adjusted to be 900 ° C. or higher and 1300 ° C. or lower. Moreover, the temperature of the water gas which the pyrolysis furnace 30 produces | generates is adjusted so that it may become 650 degreeC or more and 850 degrees C or less.

The pyrolysis furnace 30 supplies unreacted components and residues of the water gas and carbide generated by the pyrolysis reaction to the temperature reducer 40 via the water gas supply path 102. Further, the pyrolysis furnace 30 supplies the combustion gas used as a heat source for the pyrolysis reaction to the steam superheater 81 through the combustion gas channel 200b. The temperature of the combustion gas supplied to the steam superheater 81 is adjusted to be 820 ° C. or more and 920 ° C. or less.

The temperature reducer 40 is a device that lowers the temperature of the water gas supplied from the water gas supply path 102 by spraying liquid water. Water is supplied to the temperature reducer 40 from a water supply device 82 by a water supply pump (not shown). The temperature reducer 40 supplies the temperature-reduced water gas to the cyclone 50 through the water gas supply path 103. The temperature reducer 40 supplies unreacted carbide residues and residues supplied from the water gas supply path 102 to the char recovery device 41.

The temperature reducer 40 adjusts the amount of water sprayed so that the water gas adjusted in the thermal decomposition furnace 30 is 750 ° C. or higher and 900 ° C. or lower, and is 220 ° C. or higher and 280 ° C. or lower.

The char recovery device 41 is a device that recovers an unreacted portion of the carbide and supplies it to the pyrolysis furnace 30 again.

By providing the char recovery device 41, it is avoided that unreacted carbide is not used for generating water gas and discarded. Therefore, by providing the char recovery device 41, the yield of water gas from the carbide is improved.

As a further invention, it is possible to provide a return system for the pyrolysis furnace 30 using the char recovery device 41, which is suitable for a power generation system and a hydrogen supply system, and which has improved the aqueous reaction of water gas with high efficiency. Details of this return system will be described later.

The cyclone 50 is a device that removes residues contained in the water gas supplied via the water gas supply path 103. The cyclone 50 turns the water gas supplied through the water gas supply path 103 inside to centrifuge the residue contained in the water gas, guide it downward, and supply it to the residue collecting device 51. Further, the cyclone 50 guides the water gas from which the residue has been removed upward and supplies the water gas to the water gas cooling device 60 through the water gas supply path 104.

The water gas cooling device 60 is a device that lowers the temperature of the water gas supplied from the water gas supply path 104 by spraying liquid water. The water gas cooling device 60 circulates the cooling water so that the cooling water sprayed in the water gas is recovered and sprayed again into the water gas by a circulation pump (not shown).

The water gas cooling device 60 supplies the cooled water gas to the water gas holder 70. The water gas cooling device 60 is provided with a temperature sensor (not shown) for detecting the temperature of the water gas supplied to the water gas holder 70 and is circulated by a circulation pump (not shown) so that the detected temperature matches the target temperature. Control the amount of cooling water. The water gas cooling device 60 adjusts the spray amount of water so that the water gas adjusted by the temperature reducer 40 is 220 ° C. or more and 280 ° C. or less, and the water gas is 30 ° C. or more and 50 ° C. or less.

The water gas holder 70 is a device that stores the water gas supplied from the water gas cooling device 60. The water gas holder 70 can supply the stored water gas individually to the flare stack 71, the power generation facility 72, and the hydrogen purifier 73. Note that the hydrogen purifier 73 is not directly related to the power generation facility, and may be provided as appropriate.

The flare stack 71 is an apparatus for incineration when excess water gas is generated, such as when the amount of water gas holder 70 stored becomes excessive. The flare stack 71 is always combusted by a fuel such as liquefied natural gas. Therefore, when water gas is supplied to the flare stack 71, the water gas is incinerated.

The power generation facility 72 is a facility that obtains a power generation output by driving a generator by operating water gas as a fuel. As the power source for driving the generator by the power generation facility 72, for example, a gas engine that operates by burning water gas is used. Moreover, as shown in FIG. 2, you may provide the auxiliary fuel tank 72a which stores the collect | recovered water gas.

The hydrogen purifier 73 is an apparatus that purifies high-purity hydrogen gas (for example, hydrogen gas having a purity of 99.995% or more) by removing components such as carbon monoxide gas and carbon dioxide cord gas contained in the water gas. It is. The hydrogen purifier 73 is an adsorption tower filled with an adsorbent (suitable for removing components such as carbon monoxide gas and carbon dioxide gas) by pressurizing water gas to a predetermined pressure with a compressor (not shown). (Not shown). The hydrogen purifier 73 opens and closes a valve (not shown) for controlling the conduction with the outside air provided in the adsorption tower and depressurizes the adsorption tower to atmospheric pressure, so that the carbon monoxide gas is removed from the adsorbent. Then, components such as carbon dioxide gas are removed, and high purity hydrogen gas is purified.

The steam generator 80 is an apparatus that generates saturated steam by vaporizing water by heating with combustion gas. Water is supplied to the steam generator 80 from the water supply device 82 via a water supply pump (not shown). Further, the combustion gas discharged from the steam superheater 81 is supplied to the steam generator 80 via the combustion gas flow path 200c. The temperature of the combustion gas supplied to the steam generator 80 is adjusted to be 750 ° C. or higher and 850 ° C. or lower.

The saturated steam generated by the steam generator 80 is supplied to the steam superheater 81. The combustion gas used as a heat source for vaporizing water in the steam generator 80 is supplied to the dryer 10 through the combustion gas flow path 200d. The temperature of the combustion gas supplied to the dryer 10 is adjusted to be 540 ° C. or higher and 640 ° C. or lower.

The steam superheater 81 is a device that generates superheated steam from saturated steam by heating the saturated steam with combustion gas. The steam superheater 81 is supplied with saturated steam generated by the steam generator 80. Further, the combustion gas discharged from the pyrolysis furnace 30 is supplied to the steam superheater 81 through the combustion gas flow path 200b. The temperature of the combustion gas supplied to the steam superheater 81 is adjusted to be 820 ° C. or more and 920 ° C. or less.

The superheated steam generated by the steam superheater 81 is supplied to the pyrolysis furnace 30 as a gasifying agent. Further, the combustion gas used as a heat source for generating superheated steam in the steam superheater 81 is supplied to the steam generator 80 via the combustion gas flow path 200c.

The control device 90 is a device that controls the biomass power generation system A. The control device 90 can communicate with a control unit (not shown) included in each unit constituting the biomass power generation system A. The control device 90 can control each unit by transmitting a control command to a control unit included in each unit constituting the biomass power generation system A. Moreover, the control apparatus 90 can receive the signal which shows the state of each part, such as temperature and pressure, from each part which comprises the biomass power generation system A.

The control device 90 can cause each unit constituting the biomass power generation system A to execute a desired operation by reading and executing a control program stored in a storage unit (not shown).

In the biomass power generation system A shown in FIG. 1, the combustion gas generated in the carbonization furnace 20 circulates as follows through the combustion gas flow path including the combustion

gas flow paths

200a, 200b, 200c, 200d, and 200e.

1stly, the combustion gas which the carbonization furnace 20 produced | generated is supplied to the thermal decomposition furnace 30 by the combustion gas flow path 200a.

Second, the combustion gas discharged from the pyrolysis furnace 30 is supplied to the steam superheater 81 through the combustion gas channel 200b.

Third, the combustion gas discharged from the steam superheater 81 is supplied to the steam generator 80 through the combustion gas flow path 200c.

Fourth, the combustion gas discharged from the steam generator 80 is supplied to the dry operation machine 10 through the combustion gas flow path 200d.

Fifth, the combustion gas discharged from the dryer 10 is supplied to the exhaust gas cooling and cleaning device 13 through the combustion gas flow path 200e.

Sixth, the flue gas detoxified by the exhaust gas cooling and cleaning device 13 is discharged into the atmosphere by the exhaust gas cooling and cleaning device 13.

As shown in FIG. 2, the exhaust gas cooling and cleaning device 13 includes, for example, a heat exchanger 13a, a bag dust collector 13b, an exhaust tower 13c, and the like.

Here, the combustion gas generated by the carbonization furnace 20 is supplied to the pyrolysis furnace 30 without performing heat exchange with other heat medium. The reason is that the combustion gas maintained at a high temperature is used for the pyrolysis furnace. This is because the thermal decomposition reaction at 30 is promoted to improve the yield of water gas from the carbide. Compared to the case where the combustion gas generated by the carbonization furnace 20 is supplied to the pyrolysis furnace 30 after heat exchange with another heat medium, the inside of the pyrolysis furnace 30 can be maintained at a high temperature. The reaction is accelerated and the yield of water gas from the carbide is improved.

Next, the carbonization furnace 20 of the present embodiment will be described with reference to FIGS.

3 is a longitudinal sectional view of the carbonization furnace according to one embodiment of the present invention shown in FIG. 2, and FIG. 4 is a view showing a clinker crusher of the carbonization furnace according to one embodiment of the present invention shown in FIG. (A) is a plan view and (b) is an end view taken along the line CC of (a). 5 is an end view of the carbonization furnace according to one embodiment of the present invention shown in FIG. 3, wherein (a) is an end view taken along the line AA, and (b) is an end view taken along the line BB. is there.

3, an axis X indicates a vertical direction (gravity direction) orthogonal to an installation surface (not shown) on which the carbonization furnace 20 is installed.

As shown in FIG. 3, the carbonization furnace 20 includes a main body part 21, a cylindrical part 22 (cylinder part), an organic waste input part 23 (input part), a carbide discharge part 24, and a primary air supply part 25. Secondary air supply unit 26, combustion gas discharge unit 27, temperature sensor 28a (temperature detection unit), temperature sensor 28b (temperature detection unit), temperature sensor 28c (temperature detection unit), and level sensor 28d ( A deposition amount detection unit), an ignition burner 20c, and a carbonization furnace control unit 29 (control unit).

The main body 21 is a member that is formed in a substantially cylindrical shape extending along the axis X and is an exterior of the carbonization furnace 20. The main body 21 forms a primary combustion region R2 in which organic waste is partially combusted and a secondary combustion region R4 in which combustible gas contained in the combustion gas generated from the organic waste is combusted. Yes.

The main body 21 is attached to a metal (for example, iron) housing 21a that forms the exterior of the carbonization furnace 20, a heat insulating material 21b that is attached to the inner peripheral surface of the housing 21a, and an inner peripheral surface of the heat insulating material 21b. Refractory material 21c.

The cylindrical portion 22 is a member formed in a substantially cylindrical shape extending along the axis X. The cylindrical portion 22 has an outer peripheral surface 22a that forms a gap 20a between the inner peripheral surface 21d of the main body portion 21 and combusting organic waste to generate carbides. Since the cylindrical part 22 becomes high temperature by combustion of organic waste, it is preferable to form the cylindrical part 22 from a heat-resistant material (for example, a metal material such as stainless steel).

As shown in FIG. 3, the inside of the cylindrical portion 22 is a hollow closed space, and this closed space is not in communication with other spaces. Therefore, the cylindrical portion 22 can store a certain amount of heat and is not easily affected by an external temperature change.

The cylindrical portion 22 is attached to a turntable 24a, which will be described later, and rotates around the axis X in response to the turntable 24a rotating around the axis X. As the cylindrical portion 22 rotates about the axis X, the gap 20a and the organic waste existing above the gap 20a are guided along the gap 20a from above to below.

The organic waste supplied to the gap 20a is partially combusted by the primary combustion air supplied from the primary air supply unit 25 in the primary combustion region R2, and burns containing solids containing a large amount of carbides and combustible gas. Gas is generated. The solid content containing a large amount of carbide is guided to the lower carbide refining / cooling region R1 along the gap 20a, and the combustion gas containing combustible gas is guided to the secondary combustion region R4.

The carbide refining / cooling region R1 is a region where the upper portion is closed with organic waste and the primary combustion air from the primary air supply unit 25 is not supplied. Therefore, the carbide is refined while being cooled in the carbide refinement / cooling region R1.

The organic waste input unit 23 is an opening that is provided in the main body 21 and inputs organic waste (not shown) supplied from the quantitative supply device 12 via the raw material supply path 12 a into the main body 21. . An inclined surface 23a is formed below the organic waste throwing portion 23. The inclined surface 23a is inclined downward from above as it approaches the axis X. The organic waste supplied from the organic waste input part 23 is guided to the upper surface 22b of the cylindrical part 22 and the gap 20a along the inclined surface 23a.

As shown in FIG. 3, the region where the organic waste charging unit 23 is disposed is a raw material charging region R3. In the raw material charging region R3, an inspection window 20b is provided on the side opposite to the organic waste charging unit 23 with respect to the axis X. The inspection window 20b makes the inside of the carbonization furnace 20 visible.

The carbide discharge unit 24 is a mechanism for discharging carbide generated by partial combustion of organic waste in the gap 20 a to the carbide supply path 101. The carbide discharged from the carbide discharge unit 24 to the carbide supply path 101 is supplied to the pyrolysis furnace 30.

As shown in FIG. 3, the carbide discharge part 24 has a turntable 24a (rotary body), a drive part 24b, and a carbide discharge port 24c.

The turntable 24a is a member provided at a position facing the lower end in the axis X direction of the gap 20a, and is an annular rotator extending in the circumferential direction around the axis X. The turntable 24a rotates around the axis X by the driving force transmitted from the driving unit 24b.

The surface of the turntable 24a facing the lower end of the gap 20a is an inclined surface that is inclined downward as it differs from the axis X. Therefore, a gap is formed between the lower end of the gap 20a and the inclined surface of the turntable 24a.

Carbide (not shown) existing at the lower end of the gap 20a moves downward along the inclined surface of the turntable 24a as the turntable 24a rotates about the axis X, and is guided to the carbide discharge port 24c. . Therefore, as the rotational speed of the turntable 24a increases, the amount of carbide guided from the lower end of the gap 20a to the carbide discharge port 24c increases. Similarly, as the rotational speed of the turntable 24a decreases, the amount of carbide guided from the lower end of the gap 20a to the carbide discharge port 24c decreases.

The driving unit 24b is a device that transmits driving force to the turntable 24c and rotates the turntable 24b about the axis X. The drive unit 24b includes a drive motor 24e, a speed reducer 24f, a drive belt 24g, and a drive shaft 24h.

The drive motor 24e is an inverter motor whose rotation speed is controlled by a control signal transmitted from the carbonization furnace control unit 29. The rotational power of the drive motor 24e is transmitted to the speed reducer 24f by the drive belt 24g.

The speed reducer 24f is a device that increases the torque while reducing the rotational speed of the rotational power transmitted from the drive motor 24e by the drive belt 24g. The speed reducer 24f transmits the rotational power with increased torque to the drive shaft 24h extending around the axis X.

The turntable 24a is connected to the drive shaft 24h. Therefore, the turntable 24a rotates about the axis X as the drive shaft 24h rotates about the axis X.

The carbide discharge port 24 c is an opening for discharging carbide to the carbide supply path 101. The carbide discharged from the carbide discharge port 24 c to the carbide supply path 101 is supplied to the pyrolysis furnace 30 through the carbide supply path 101.

The clinker crusher 24d is a member for crushing a clinker that is a lump larger than a gap formed between the lower end of the gap 20a and the inclined surface of the turntable 24a. Here, the clinker is obtained by melting the combustion ash generated by the combustion of the organic waste in the primary combustion region R2 into a lump.

As shown in FIG. 4A, the clinker crusher 24d is a substantially annular member arranged around the axis X, and claws 24i protruding radially inward at a plurality of positions in the circumferential direction. Is provided.

As shown in (b) of FIG. 4 (a), the claw 24i has a shape bent upward along the inclined surface of the turntable 24a.

As shown in FIG. 3, the clinker crusher 24d is attached to the main body 21 by fastening bolts. The clinker crusher 24d remains fixed to the main body 21 even when the turntable 24a rotates about the axis X. Therefore, when the clinker moves as the turntable 24a rotates, the clinker collides with the claws 24i of the clinker crusher and is crushed.

Next, the primary air supply unit 25 will be described.

The primary air supply unit 25 is a device that supplies primary combustion air that partially burns organic waste toward the organic waste accumulated in the gap 20a. The primary air supply unit 25 includes a primary combustion fan 25a (air blowing unit), a cover unit 25b, and an air supply port 25c.

The primary combustion fan 25a is a device that blows air (atmosphere) introduced from the outside, and includes an inverter motor (not shown) and a fan (not shown) driven by the inverter motor. The primary combustion fan 25a can adjust the air volume to blow by controlling the rotation speed of the inverter motor.

The cover portion 25b is a member that forms a closed space 25d in which air blown from the primary combustion fan 25a is introduced and air is supplied to the air supply port 25c.

FIG. 5A shows an end view of the carbonization furnace 20 shown in FIG. 3 along the line AA. As shown in the figure, the cover portion 25b is disposed around the axis X between the outer peripheral surface 21e of the main body portion 21 and the cover portion 25b. An extended closed space 25d is formed.

The air supply port 25c is a flow path for supplying air blown from the primary combustion fan 25a to the closed space 25d to the primary combustion region R2 inside the main body 21 from the closed space 25d.

As shown in FIG. 3, the air supply ports 25c are provided at a plurality of locations in the vertical direction along the axis X in the primary combustion region R2 where the organic waste is partially combusted by the primary combustion air.

Further, as shown in FIG. 5A, the air supply ports 25c are provided in the main body 21 at equal intervals along the circumferential direction around the axis X (30 ° intervals in FIG. 5A). . As shown in FIG. 5A, the air supply port 25c is a linear flow path extending from the outer peripheral surface 21e of the main body 21 toward the axis X.

In the example shown in FIG. 5A, the air supply ports 25c are arranged at intervals of 30 ° along the circumferential direction around the axis X, but other intervals (for example, 20 °, 45 °, etc.) Alternatively, they may be arranged at arbitrary intervals instead of at equal intervals.

The primary air supply unit 25 shown in FIG. 3 has a heating unit (not shown) for heating the air blown from the primary combustion fan 25a. The air supply port 25c supplies the air heated by the heating unit to the air supply port 25c. Therefore, compared with the case where the air blown from the primary combustion fan 25a is not heated, the atmospheric temperature of the primary combustion region R2 can be maintained at a high temperature.

As the heating unit provided in the primary air supply unit 25, the radiation fins 25e shown in FIGS. 6 and 7 may be employed. 6 is a longitudinal sectional view showing a first modification of the primary air supply unit of the carbonization furnace according to the embodiment of the present invention shown in FIG. 3, and FIG. 7 is a second modification of the primary air supply unit. It is a longitudinal cross-sectional view which shows an example.

The modification of the primary air supply part 25 shown in FIG.6 and FIG.7 uses the air transmitted from the gap | interval 20a of the carbonization furnace 20 via the main-body part 21, and the air ventilated from the primary combustion fan 25a is used. The heat dissipating fins 25e are provided.

6 and 7, the heat radiation fin 25e is an annular member that contacts the outer peripheral surface 21e of the main body 21 and extends around the axis X along the outer peripheral surface 21e. The radiation fins 25e are provided at a plurality of locations along the axis X. The radiation fin 25e is attached to the outer peripheral surface 21e of the main body 21 by welding or the like.

The cover part 25b of the primary air supply part 25 shown in FIG. 3 is provided only at substantially the same position in the axis X direction as the air supply port 25c. On the other hand, in the first modification of the primary air supply unit 25 in FIG. 6, the cover portion 25b of the primary air supply unit 25 supplies air in addition to substantially the same position in the axis X direction as the air supply port 25c. It is provided so as to include a position below the opening 25c.

6 is a heat transfer member to which the ambient temperature of the gap 20a is transferred through the outer peripheral surface 21e of the main body 21. The heat dissipation fin 25e shown in FIG. The outer peripheral surface 21e of the main body 21 is heated to about 50 ° C. to 70 ° C., although the housing 21a is protected by the refractory material 21c and the heat insulating material 21b so as not to be overheated. Therefore, the air (atmosphere) blown from the primary combustion fan 25a can be heated by the radiation fin 25e.

As shown in FIG. 6, the primary combustion fan 25a blows air introduced from the outside toward the outer peripheral surface 21e of the main body portion 21 located on the outer peripheral side below the gap 20a. This is because the outer peripheral surface 21e of the main body 21 located on the outer peripheral side below the gap 20a is cooled by air introduced from the outside.

As shown in FIG. 6, below the gap 20a is a carbide refining / cooling region R1. The carbide refining / cooling region R1 is a region in which the carbide generated in the primary combustion region R2 is refined while being cooled, and therefore it is desirable to maintain the temperature at a certain low level. Therefore, in the present embodiment, the position where the primary combustion fan 25a blows air is set so that the carbide refining / cooling region R1 is cooled.

On the other hand, in the 2nd modification of the primary air supply part 25 shown in FIG. 7, the thickness of the heat insulating material 21b in the position where the radiation fin 25e is arrange | positioned, and the position of the outer peripheral surface 21e of the main-body part 21 are different from FIG. ing. About another point, it is the same as that of the 1st modification shown in FIG.

As shown in FIG. 7, the distance from the inner peripheral surface 21d of the main body 21 to the outer peripheral surface 21e at the position where the air supply port 25c is arranged is a distance D1. On the other hand, the distance from the inner peripheral surface 21d of the main body 21 to the outer peripheral surface 21e at the position where the radiation fin 25e is disposed is the distance D2. As shown in FIG. 7, the distance D2 is shorter than the distance D1.

According to the second modification of the primary air supply unit 25 shown in FIG. 7, compared with the first modification of the primary air supply unit 25 shown in FIG. 6, the atmosphere of the gap 20a at the position where the radiation fins 25e are arranged. The temperature is easily transmitted to the outer peripheral surface 21e. Therefore, according to the second modification, the radiating fins 25e are heated to a higher temperature than in the first modification. Therefore, according to the primary air supply unit 25 of the second modification, the air blown by the primary combustion fan 25a can be supplied to the air supply port 25c while being heated to a higher temperature.

In addition, although the radiation fin 25e shown to FIG. 6 and FIG. 7 shall be the cyclic | annular member extended around the axis line X, another aspect may be sufficient. For example, the heat dissipating fin 25e may be in contact with the outer peripheral surface 21e of the main body 21 and may be configured to form a spiral flow path that pivots from below to above around the axis X along the outer peripheral surface 21e. Good.

Next, the secondary air supply unit 26 will be described.

The secondary air supply unit 26 is a device that supplies secondary combustion air for burning the combustible gas contained in the combustion gas generated by the combustion of the organic waste in the primary combustion region R2 to the inside of the main body 21. is there. As shown in FIG. 3, the secondary air supply unit 26 is provided in the secondary combustion region R4 and supplies secondary combustion air toward the secondary combustion region R4.

The secondary air supply unit 26 includes a secondary combustion fan 26a, a cover unit 26b, and an air supply port 26c.

The secondary combustion fan 26a is a device that blows air (atmosphere) introduced from the outside, and includes an inverter motor (not shown) and a fan (not shown) driven by the inverter motor. The secondary combustion fan 26a can adjust the air volume to blow by controlling the rotation speed of the inverter motor.

The cover portion 26b is a member that forms a closed space 26d that introduces air blown from the secondary combustion fan 26a and supplies air to the air supply port 26c.

As shown in FIG. 5B as an end view taken along the line BB of the carbonization furnace 20 shown in FIG. 3, the cover portion 26b is a closed space extending around the axis X between the outer peripheral surface 21e of the main body portion 21. 26d is formed.

The air supply port 26c is a flow path for supplying air blown from the secondary combustion fan 26a to the closed space 26d to the secondary combustion region R4 inside the main body 21 from the closed space 26d.

As shown in FIG. 3, the air supply ports 26 c are provided at a plurality of locations in the vertical direction along the axis X in the secondary combustion region R <b> 4 where the combustible gas contained in the combustion gas is combusted by the secondary combustion air. ing.

Further, as shown in FIG. 5B, the air supply ports 26c are provided in the main body portion 21 at equal intervals along the circumferential direction around the axis X (30 ° intervals in FIG. 5B). . Further, as shown in FIG. 5B, the air supply port 26 c is a linear flow path extending from the outer peripheral surface 21 e of the main body 21 toward the axis X.

In the example shown in FIG. 5B, the air supply ports 26c are arranged at intervals of 30 ° along the circumferential direction around the axis X, but other intervals (for example, 20 °, 45 °, etc.) Or may be arranged at an arbitrary interval instead of at equal intervals.

The combustion gas discharge unit 27 is an exhaust port that discharges the combustion gas generated in the primary combustion region R2 and combusted with the combustible gas component in the secondary combustion region R4 to the combustion gas channel 200a. The combustion gas discharged to the combustion gas flow path 200a is supplied to the pyrolysis furnace 30 for use as a heat source for the pyrolysis reaction.

The temperature sensor 28 a is a sensor that detects the temperature of the combustion gas discharged from the combustion gas discharge unit 27. The temperature sensor 28 a transmits a temperature detection signal indicating the detected temperature to the carbonization furnace control unit 29.

As shown in FIG. 3, the temperature sensor 28a is disposed in a region close to the combustion gas flow path 200a in the secondary combustion region R4. Therefore, the combustion gas temperature Tg detected by the temperature sensor 28a is substantially the same as the temperature of the combustion gas discharged to the combustion gas flow path 200a.

The temperature sensor 28b is a sensor that detects the ambient temperature of the primary combustion region R2. The temperature sensor 28 b transmits a temperature detection signal indicating the detected temperature to the carbonization furnace control unit 29.

The temperature sensor 28c is a sensor that detects a carbide temperature Tc that is a temperature of carbide deposited on the lower end side of the gap 20a. The temperature sensor 28 b transmits a temperature detection signal indicating the detected carbide temperature Tc to the carbonization furnace control unit 29.

The level sensor 28d is a sensor that detects the amount of organic waste deposited in the gap 20a. The level sensor 28d detects the amount of organic waste accumulated in the direction of the axis Y shown in FIG. 3 by obtaining an output signal corresponding to the amount of accumulation in the primary combustion region R2.

The level sensor 28d may be a reflective sensor that detects the amount of deposition by receiving reflection of emitted light, ultrasonic waves, or the like. Further, the level sensor 28d may be a transmission type sensor in which a receiving part for receiving emitted X-rays or the like is provided in the cylindrical part 22.

As will be described later, the level sensor 28d detects that the amount of organic waste deposited in the gap 20a has decreased, such as when the introduction of new organic waste from the organic waste input unit 23 is stopped. Sensor. Therefore, the level sensor 28d detects the amount of deposition along the axis Y directed downward from the mounting position in the vertical direction. When the carbonization furnace control unit 29 outputs a detection signal indicating that the deposition amount Ao, which is the deposition amount of the organic waste detected by the level sensor 28d, is 0 (zero), the deposition amount of the organic waste present in the gap 20a. Is determined to have decreased to a predetermined first deposition amount Ao1 or less.

The ignition burner 20c is a device used to ignite organic waste when starting combustion of organic waste in the carbonization furnace 20. As shown in FIG. 3, the ignition burner 20c is provided on the lower end side of the gap 20a. In addition, as shown in FIG. 3, the ignition burners 20 c are arranged at two locations facing the axis X.

The ignition burner 20c burns organic waste accumulated on the lower end side of the gap 20a by generating a flame using ignition fuel such as kerosene. The ignition burner 20c generates a flame when starting combustion of organic waste in the carbonization furnace 20 in accordance with a control command from the carbonization furnace control unit 29. Further, the ignition burner 20c stops the generation of flame at a predetermined timing in accordance with a control command from the carbonization furnace control unit 29.

The carbonization furnace control unit 29 is a device that controls each part by receiving a detection signal indicating the state of each part from each part of the carbonization furnace 20 and transmitting the control signal to each part based on the detection signal. The carbonization furnace control unit 29 is a device that transmits a signal indicating the state of the carbonization furnace 20 to the control device 90 and controls the carbonization furnace 20 in response to a control signal transmitted from the control device 90.

The carbonization furnace control unit 29 receives a temperature detection signal indicating the temperature detected by each of the

temperature sensors

28a, 28b, and 28c, and a deposition amount detection signal indicating the deposition amount Ao of the organic waste detected by the level sensor 28d. . Further, the carbonization furnace control unit 29 transmits a control signal for controlling the blown amount of the primary combustion fan 25 a to the primary air supply unit 25. Further, the carbonization furnace control unit 29 transmits a control signal for controlling the blown amount of the secondary combustion fan 26 a to the secondary air supply unit 26. In addition, when the carbonization furnace control unit 29 transmits a control signal to the ignition burner 20c to start combustion of organic waste, it generates a flame and transmits a control signal at a predetermined timing to stop the generation of the flame. Let Moreover, the carbonization furnace control unit 29 transmits a control signal for controlling the rotation speed of the turntable 24a to the drive motor 24e.

Next, a method for controlling the blowing amount of the primary combustion fan 25a by the carbonization furnace control unit 29 will be described.

The carbonization furnace control unit 29 controls the amount of air blown by the primary combustion fan 25a based on the atmospheric temperature of the primary combustion region R2 detected by the temperature sensor 28b. The amount of air blown by the primary combustion fan 25a coincides with the amount of primary combustion air supplied from the air supply port 25c to the primary combustion region R2 of the carbonization furnace 20. Therefore, the carbonization furnace control unit 29 can adjust the amount of primary combustion air blown to the primary combustion region R2 by controlling the amount of air blown by the primary combustion fan 25a. .

The carbonization furnace control unit 29 performs primary combustion based on the atmospheric temperature in the primary combustion region R2 detected by the temperature sensor 28b so that the combustion state suitable for carbonizing the organic waste accumulated in the gap 20a is maintained. The amount of air blown by the fan 25a is controlled. Specifically, the carbonization furnace control unit 29 controls the amount of air blown by the primary combustion fan 25a so that the ambient temperature of the primary combustion region R2 is within the range of 1000 ° C. or more and 1200 ° C. or less.

Next, a method for controlling the blowing amount of the secondary combustion fan 26a by the carbonization furnace control unit 29 will be described with reference to the flowchart of FIG.

The carbonization furnace control unit 29 controls the amount of air blown by the secondary combustion fan 26a based on the combustion gas temperature Tg detected by the temperature sensor 28a. The amount of air blown by the secondary combustion fan 26a matches the amount of air for secondary combustion supplied to the secondary combustion region R4 of the carbonization furnace 20 from the air supply port 26c. Therefore, the carbonization furnace control unit 29 can adjust the air amount of the secondary combustion air blown to the secondary fuel burner region R4 by controlling the amount of air blown by the secondary combustion fan 26a. .

Based on the combustion gas temperature Tg detected by the temperature sensor 28a so that the combustion state suitable for burning the combustible gas contained in the combustion gas in the secondary combustion region R4 is maintained. The amount of air blown by the next combustion fan 26a is controlled. Specifically, the carbonization furnace control unit 29 controls the amount of air blown by the secondary combustion fan 26a according to the flowchart shown in FIG.

Each process in the flowchart shown in FIG. 8 is a process performed when a calculation unit (not shown) included in the carbonization furnace control unit 29 executes a control program stored in a storage unit (not shown).

Prior to the processing shown in the flowchart of FIG. 8, when the carbonization furnace control unit 29 starts combustion of the organic waste in the carbonization furnace 20, the organic waste is generated by the ignition burner 20 c and accumulated in the gap 20 a. Start burning. Thereafter, the carbonization furnace control unit 29 starts blowing external air (atmosphere) by the secondary combustion fan 26a. The carbonization furnace control unit 29 controls the secondary combustion fan 26a so that the air flow rate is constant until the combustion gas temperature Tg detected by the temperature sensor 28a becomes equal to or higher than the first combustion gas temperature Tg1. After the combustion gas temperature Tg detected by the temperature sensor 28a becomes equal to or higher than the first combustion gas temperature Tg1, the processes shown in the flowchart of FIG. 8 are started.

The amount of secondary combustion air blown by the secondary combustion fan 26a before the combustion gas temperature Tg becomes equal to or higher than the first combustion gas temperature Tg1 is assumed to exist in the secondary combustion region R4. It is an amount obtained by adding a certain surplus amount to the amount necessary to completely burn the fuel.

In step S800, the carbonization furnace control unit 29 receives the temperature detection signal transmitted from the temperature sensor 28a, and thereby detects the combustion gas temperature Tg that is the temperature of the combustion gas discharged from the combustion gas discharge unit 27.

In step S801, the carbonization furnace control unit 29 determines whether or not the combustion gas temperature Tg detected by the temperature sensor 28a is lower than the first combustion gas temperature Tg1. When determining that the combustion gas temperature Tg is lower than the first combustion gas temperature Tg1, the carbonization furnace control unit 29 advances the process to step S802, and otherwise advances the process to step S803.

In step S802, the carbonization furnace control unit 29 transmits a control signal for reducing the blown amount of the secondary combustion fan 26a to the secondary combustion fan 26a. The secondary combustion fan 26a reduces the blown air volume in response to receiving the control signal from the carbonization furnace control unit 29.

Here, when it is determined that the combustion gas temperature Tg is lower than the first combustion gas temperature Tg1, the blowing amount of the secondary combustion fan 26a is decreased for the following reason.

The amount of secondary combustion air supplied by the secondary air supply unit 26 to the secondary combustion region R4 is a constant amount than the amount of combustible gas contained in the combustion gas existing in the secondary combustion region R4. The amount is preferably as large as possible. That is, the excess air ratio in the secondary combustion region R4 is preferably set to a constant value larger than 1.0.

However, the amount of combustible gas present in the secondary combustion region R4 generally varies depending on factors such as the properties of the organic waste and the combustion state of the organic waste in the primary combustion region R2. Therefore, if the amount of secondary combustion air supplied from the secondary air supply unit 26 to the secondary combustion region R4 is kept constant, an air amount suitable for complete combustion of the combustible gas cannot be maintained.

When the amount of secondary combustion air is excessively large relative to the amount of complete combustion of the combustible gas, a large amount of surplus air that is not used for combusting the combustible gas is supplied to the secondary combustion region R4. It will be. Since the temperature of the air (atmosphere) blown by the secondary combustion fan 26a is lower than the atmospheric temperature in the secondary combustion region R4, the atmospheric temperature in the secondary combustion region R4 is lowered by a large amount of excess air.

Then, the combustion efficiency of the combustible gas in the secondary combustion region R4 is deteriorated, and the combustion gas containing a large amount of the combustible gas is discharged from the combustion gas discharge unit 27. The combustible gas contains polymer hydrocarbons which are components that solidify to become tar. Therefore, if a large amount of components that solidify into combustible gas and become tar is contained, the carbonization furnace 20 and equipment installed downstream thereof may be damaged. For this reason, it is desirable that a large amount of components that solidify into the combustion gas and become tar are not included, and damage to the carbonization furnace 20 and equipment installed downstream thereof is desirably suppressed.

Therefore, when the carbonization furnace control unit 29 determines that the combustion gas temperature Tg is lower than the first combustion gas temperature Tg1, the secondary combustion is performed in order to reduce the amount of surplus air supplied to the secondary combustion region R4. The air volume of the fan 26a is reduced.

In step S803, the carbonization furnace control unit 29 determines whether or not the combustion gas temperature Tg detected by the temperature sensor 28a is higher than the second combustion gas temperature Tg2. When determining that the detected combustion gas temperature Tg is higher than the second combustion gas temperature Tg2, the carbonization furnace control unit 29 advances the process to step S804, and if not, advances the process to step S801.

In step S804, the carbonization furnace control unit 29 transmits a control signal for increasing the blowing amount of the secondary combustion fan 26a to the secondary combustion fan 26a. The secondary combustion fan 26a increases the blown air volume in response to receiving the control signal from the carbonization furnace control unit 29.

The carbonization furnace control unit 29 starts execution of the process shown in FIG. 8 again when the process of the flowchart shown in FIG. 8 is completed.

Here, when it is determined that the combustion gas temperature Tg is higher than the second combustion gas temperature Tg2, the blowing amount of the secondary combustion fan 26a is increased for the following reason.

When the carbonization furnace 20 is operated without setting an upper limit on the combustion gas temperature Tg, the assumed maximum combustion gas temperature is assumed, and the carbonization furnace 20 and the heat resistance are sufficiently maintained even at the fuel gas temperature. It is necessary to design the combustion gas flow path 200a. In this case, it is necessary to manufacture the carbonization furnace 20 or the like using an expensive member having high heat resistance, and the manufacturing cost of the carbonization furnace 20 or the like increases. In order not to increase the manufacturing cost of the carbonization furnace 20 or the like, it is preferable that the combustion gas temperature Tg be equal to or lower than a predetermined upper limit temperature.

Therefore, the carbonization furnace control unit 29 increases the blowing amount of the secondary combustion fan 26a when it is determined that the combustion gas temperature Tg is higher than the second combustion gas temperature Tg2. As described above, when a large amount of surplus air is supplied to the secondary combustion region R4 by increasing the amount of air blown from the secondary combustion fan 26a, the atmospheric temperature in the secondary combustion region R4 is lowered.

As described above, the carbonization furnace control unit 29 controls the amount of air blown by the secondary combustion fan 26a based on the combustion gas temperature Tg detected by the temperature sensor 28a, so that the combustion gas temperature Tg becomes the first value. The first combustion gas temperature Tg1 or higher and the second combustion gas temperature Tg2 or lower are set.

Here, as the first combustion gas temperature Tg1 and the second combustion gas temperature Tg2, for example, the first combustion gas temperature Tg1 can be set to 900 ° C., and the second combustion gas temperature Tg2 can be set to 1300 ° C.

The reason why the first combustion gas temperature Tg1 is set to 900 ° C. is that most of the polymer hydrocarbons can be removed from the combustion gas by maintaining the temperature of the secondary combustion region R4 at 900 ° C. or higher. . The polymer hydrocarbon is a component that solidifies into a tar in the combustible gas contained in the combustion gas. Therefore, by removing most of the polymer hydrocarbon from the combustion gas, damage to the carbonization furnace 20 and equipment installed downstream thereof can be suppressed.

Further, as the first combustion gas temperature Tg1 and the second combustion gas temperature Tg2, for example, the first combustion gas temperature Tg1 may be set to 1000 ° C., and the second combustion gas temperature Tg2 may be set to 1200 ° C.

Further, for example, both the first combustion gas temperature Tg1 and the second combustion gas temperature Tg2 may be set to 1100 ° C. In this case, the carbonization furnace control unit 29 decreases the blowing amount when the combustion gas temperature Tg is lower than the first combustion gas temperature Tg1, and increases the blowing amount when the combustion gas temperature Tg is higher than the second combustion gas temperature Tg2. The secondary combustion fan 26a is controlled so as to cause this to occur.

Next, a method for controlling the rotational speed of the turntable 24a by the carbonization furnace control unit 29 will be described with reference to the flowchart of FIG.

Each process in the flowchart shown in FIG. 9 is a process performed when a calculation unit (not shown) included in the carbonization furnace control unit 29 executes a control program stored in a storage unit (not shown).

In the flowchart shown in FIG. 9, the carbonization furnace control unit 29 controls the discharge amount of the carbide discharged by the carbide discharge unit 24. In the present embodiment, the amount of carbide discharged by the carbide discharge unit 24 is controlled because the input of the organic waste from the organic waste input unit 23 to the gap 20a is stopped. This is to prevent the temperature of the carbide discharged from 24 from rising.

When the amount of organic waste deposited in the gap 20a gradually decreases, the carbide refining / cooling region R1 for extinguishing the carbide gradually decreases. In this case, if the rotation speed of the turntable 24a is maintained constant, the carbide is discharged from the lower end of the gap 20a in a state where the carbide is not sufficiently cooled. This is because the carbide that has been carbonized in the primary combustion region R2 to a high temperature is not sufficiently cooled in the carbide refining / cooling region R1.

Therefore, the carbonization furnace control unit 29 adjusts the temperature of the carbide discharged by the carbide discharge unit 24 by controlling the discharge amount of the carbide discharged by the carbide discharge unit 24.

In the present embodiment, the carbonization furnace control unit 29 adjusts the temperature of the carbide discharged by the carbide discharge unit 24 using both the temperature sensor 28c and the level sensor 28d. The former is a sensor that directly detects the temperature of the carbide, and the latter is a sensor that indirectly detects a state in which the temperature of the carbide is high from the amount of deposited carbide.

Hereinafter, each step of the flowchart of FIG. 9 will be described.

In step S900, the carbonization furnace control unit 29 receives the temperature detection signal transmitted from the temperature sensor 28c, thereby detecting the carbide temperature Tc, which is the temperature of the carbide deposited on the lower end side of the gap 20a.

In step S901, the carbonization furnace control unit 29 receives the accumulation amount detection signal transmitted from the level sensor 28d, and thereby detects the accumulation amount Ao that is the accumulation amount of the organic waste accumulated in the gap 20a.

In step S902, the carbonization furnace control unit 29 determines whether the carbide temperature Tc detected by the temperature sensor 28c is equal to or higher than the first carbide temperature Tc1. When determining that the detected carbide temperature Tc is equal to or higher than the first carbide temperature Tc1, the carbonization furnace control unit 29 proceeds to step S903, and otherwise proceeds to step S904.

Here, as the first carbide temperature Tc1, for example, an arbitrary temperature in the range of 250 ° C. or higher and 300 ° C. or lower can be set.

In step S903, the carbonization furnace control unit 29 controls the drive unit 24b to rotate the rotation speed of the turntable 24a at the second rotation speed Rs2. The second rotation speed Rs2 is lower than the first rotation speed Rs1 described later.

Here, the first rotation speed Rs1 is a speed for discharging the amount of carbide necessary for the carbonization furnace 20 to maintain the normal operation state from the carbide discharge section 24. In step S903, the rotational distance of the turntable 24a is set so that the temperature of the carbide discharged by the carbide discharge unit 24 decreases when the carbide temperature Tc detected by the temperature sensor 28c is equal to or higher than the first carbide temperature Tc1. The second rotational speed Rs2 is lower than the first rotational speed Rs1. By reducing the rotation speed of the turntable 24a, the time for which the carbide stays in the carbide refining / cooling region R1 becomes longer, and accordingly, the temperature of the carbide discharged by the carbide discharge portion 24 decreases.

In step S904, the carbonization furnace control unit 29 determines whether or not the deposition amount Ao detected by the level sensor 28d is equal to or less than the first deposition amount Ao1. When determining that the detected deposition amount Ao is equal to or less than the first deposition amount Ao1, the carbonization furnace control unit 29 advances the process to step S905, and otherwise advances the process to step S906.

In step S905, the carbonization furnace control unit 29 controls the drive unit 24b to rotate the rotation speed of the turntable 24a at the second rotation speed Rs2. The second rotation speed Rs2 is lower than the first rotation speed Rs1 described later. In step S905, the rotation speed of the turntable 24a is set to the first speed so that the temperature of the carbide discharged by the carbide discharge unit 24 is lowered when the accumulation amount Ao detected by the level sensor 28d is equal to or less than the first accumulation amount Ao1. The second rotation speed Rs2 is lower than the rotation speed Rs1.

In step S906, the carbonization furnace control unit 29 controls the drive unit 24b to rotate the rotation speed of the turntable 24a at the first rotation speed Rs1. As described above, the first rotation speed Rs1 is a speed for discharging the amount of carbide necessary for the carbonization furnace 20 to maintain the normal operation state from the carbide discharge section 24. Since the carbide temperature Tc is lower than the first carbide temperature Tc1 and the deposition amount Ao is larger than the first deposition amount Ao1 in step S906, the carbonization furnace control unit 29 has an amount necessary for maintaining the operation state. The drive unit 24b is controlled to discharge the carbide from the carbide discharge unit 24.

The carbonization furnace control unit 29 starts execution of the process shown in FIG. 9 again when the process of the flowchart shown in FIG. 9 is completed. In this way, the carbonization furnace control unit 29 is configured so that the drive unit 24b rotates the turntable 24a based on the carbide temperature Tc detected by the temperature sensor 28c and the organic waste accumulation amount Ao detected by the level sensor 28d. To control.

In the flowchart shown in FIG. 9 described above, the rotation speed of the turntable 24a is switched between two stages depending on whether or not the carbide temperature Tc detected by the temperature sensor 28c is equal to or higher than the first carbide temperature Tc1. Other embodiments may be used.

For example, the rotation speed of the turntable 24c may be switched in two or more stages according to the carbide temperature Tc. Further, for example, the rotational speed of the turntable 24a may be controlled so as to be in inverse proportion to the carbide temperature Tc detected by the temperature sensor 28c without switching the rotational speed of the turntable 24a stepwise.

Further, in the flowchart shown in FIG. 9, the rotation speed of the turntable 24a is switched in two steps depending on whether or not the accumulation amount Ao detected by the level sensor 28d is equal to or more than the first accumulation amount Ao1. However, other embodiments may be used.

For example, the rotational speed of the turntable 24a may be switched in two or more stages according to the accumulation amount Ao. For example, the rotational speed of the turntable 24a may be controlled so that the rotational speed of the turntable 24a is proportional to the deposition amount Ao detected by the level sensor 28d without switching the rotational speed of the turntable 24a stepwise. .

In the flowchart shown in FIG. 9, the rotational speed of the turntable 24a is controlled using both the carbide temperature Tc detected by the temperature sensor 28c and the accumulation amount Ao detected by the repel sensor 28d. May be other embodiments.

For example, the rotational speed of the turntable 24a may be controlled using either the carbide temperature Tc detected by the temperature sensor 28c or the deposition amount Ao detected by the level sensor 28d.

Next, the pyrolysis furnace 30 of the present embodiment will be described with reference to FIGS.

FIG. 10 is a longitudinal sectional view of the pyrolysis furnace according to one embodiment of the present invention shown in FIG. 2, FIG. 11 is a sectional view of the reaction tube of the pyrolysis furnace shown in FIG. DD is a sectional view taken along the arrow D, and (b) is an end view taken along the arrow EE. FIG. 12 is an enlarged view of a main part of the pyrolysis furnace shown in FIG.

10, the axis Z indicates the vertical direction (gravity direction) orthogonal to the installation surface (not shown) on which the pyrolysis furnace 30 is installed.

As shown in FIG. 10, the pyrolysis furnace 30 of the present embodiment includes a main body 31, a reaction tube 32, a reaction tube head 33 (supply portion), a water gas outlet nozzle 34 (water gas outlet portion), Combustion gas supply part 35 (heating gas supply part), combustion gas discharge part 36 (heating gas discharge part), gland packing 37 (first seal part), gland packing 38 (second seal part), And a gland packing 39 (third seal portion).

The main body 31 is a member formed in a substantially cylindrical shape extending along the axis Z. The main body 31 forms a space for accommodating the reaction tube 32 therein.

The main body 31 is a metal (for example, iron) housing 31a that forms the exterior of the pyrolysis furnace 30, a heat insulating material 31b that is attached to the inner peripheral surface of the housing 31a, and an inner peripheral surface of the heat insulating material 31b. And a heat-resistant material 31c to be attached.

The upper surface of the substantially cylindrical main body 31 is composed of an upper plate 31d that is annular in plan view, and the bottom surface of the main body 31 is composed of a bottom plate 31e that is annular in plan view.

An upper end flange 31g (first flange portion) is provided at the upper end of the side surface 31f of the main body 31, and a lower end flange 31i (second flange portion) is provided at the lower end of the side surface 31f of the main body 31. Yes.

The upper plate 31d and the upper end flange portion 31g are a fastening bolt 31h (fastening member) in a state where a gasket (fourth seal portion) (not shown) is sandwiched between the upper plate 31d and the upper end flange portion 31g at a plurality of positions around the axis Z. ).

Similarly, the bottom plate 31e and the lower end flange 31i are a fastening bolt 31j (fastening member) in a state where a gasket (fifth seal portion) (not shown) is sandwiched between the bottom plate 31e and the lower end flange 31i at a plurality of locations around the axis Z. It is concluded by

The reaction tube 32 is a mechanism formed in a substantially cylindrical shape extending along the axis Z. The reaction tube 32 has an outer peripheral surface 32 d that forms a combustion gas flow path 30 a for allowing a combustion gas (heating gas) to flow between the inner peripheral surface of the main body 31.

The reaction tube 32 includes a center pipe 32a (tubular member), an upper end flange 32b (third flange portion), a plurality of first inclined plates 32f, a plurality of second inclined plates 32g, and a plurality of holding rods 32h (holding portions). ).

As shown in FIG. 10, the upper end flange 32b of the reaction tube 32 and the end of the center pipe 32a on the upper end flange 32b side protrude upward from the upper plate 31d (upper surface) of the main body 31.

The lower end 32c of the reaction tube 32 protrudes downward from the bottom plate 31e (bottom surface) of the main body 31.

The center pipe 32a is a member formed in a cylindrical shape extending along the axis Z. Inside the center pipe 32a is housed a thermal decomposition promotion mechanism including a plurality of first inclined plates 32f, a plurality of second inclined plates 32g, and a plurality of holding rods 32h (holding portions).

The thermal decomposition promotion mechanism promotes the thermal decomposition reaction of the carbide and superheated steam (gasification agent) by guiding the carbide stepwise from the upper end side to the lower end side of the center pipe 32a and retaining the carbide in the reaction tube 32. It is a mechanism to make.

As shown in FIG. 10 and FIG. 11, the plurality of first inclined plates 32f and the plurality of second inclined plates 32g are held by four holding bars 32h at a plurality of locations along the axis Z. Further, the first inclined plates 32f and the second inclined plates 32g are alternately arranged along the axis Z.

The upper ends of the four holding rods 32 h are attached to the lower surface of the lower end flange 33 a of the reaction tube head 33. By releasing the fastening between the upper end flange 32b of the reaction tube 32 and the lower end flange 33a of the reaction tube head 33, the thermal decomposition promoting mechanism can be removed (detached) upward from the center pipe 32a.

The first inclined plate 32f shown in FIG. 11 (a) is configured such that the carbide is changed from one end of the inner peripheral surface 32e of the reaction tube 32 (the left end in FIG. 11 (a)) to the other end ((a) of FIG. ) Are arranged so as to form a first inclined surface that is inclined so as to be led to the first opening 32i provided at the right end).

Further, the second inclined plate 32f shown in FIG. 11 (b) has one end portion (in FIG. 11) from the other end portion (the right end portion in FIG. 11 (b)) of the carbide to the carbide. The second inclined surface is formed so as to be inclined so as to be led to the second opening 32j provided at the left end portion in (b).

As shown in FIG. 10, the first inclined surface formed by the first inclined plate 32f is inclined so as to guide the carbide falling from the second opening 32j downward, and the second inclined plate 32g forms the second inclined surface. The inclined surface is inclined so as to guide the carbide falling from the first opening 32i downward.

In this manner, the thermal decomposition promoting mechanism guides the carbide stepwise from the upper end side to the lower end side of the center pipe 32a using the first inclined plates 32f and the second inclined plates 32g that are alternately arranged along the axis Z. be able to.

The inclination angle of the first inclined surface and the second inclined surface with respect to the plane orthogonal to the axis Z can be arbitrarily set according to the properties of the carbide, but in order to reliably move the carbide along the inclined surface, the carbide It is preferable that the angle be equal to or greater than the angle of repose. On the other hand, if the inclination angle is too large, the residence time of the carbide in the reaction tube 32 is shortened, and the thermal decomposition reaction is not sufficiently promoted.

Therefore, it is particularly preferable that the inclination angle of the first inclined surface and the second inclined surface with respect to the plane orthogonal to the axis Z is determined to be equal to or greater than the repose angle of the carbide in the range of 20 ° to 60 °.

The reaction tube head 33 is attached to the reaction tube 32 and supplies carbide and superheated steam (gasification agent) to the inside of the reaction tube 32 to generate water gas inside the reaction tube 32.

The reaction tube head 33 includes a lower end flange 33a (fourth flange) attached to the reaction tube 32, an upper end flange 33b attached to the carbide supply passage 101, and a flow path (not shown) through which superheated steam is supplied from the steam superheater 81. ) And a side flange 33c attached thereto.

The lower end flange 33a of the reaction tube head 33 and the upper end flange 32b of the reaction tube 32 are fastened by fastening bolts 33d with a gasket (sixth seal portion) (not shown) sandwiched between them at a plurality of locations around the axis Z. ing.

The water gas outlet nozzle 34 is a substantially cylindrical member attached to the lower end portion 32 c of the reaction tube 32. The water gas outlet nozzle 34 is used to reduce the temperature of the water gas generated by the pyrolysis reaction of the carbide in the reaction tube 32, the unreacted part of the carbide, the ash, and the like through the water gas supply path 102. Lead to.

The combustion gas supply unit 35 is an opening that is provided above the main body 31 and supplies the combustion gas guided from the combustion gas channel 200a to the combustion gas channel 30a.

The combustion gas discharge unit 36 is an opening that is provided below the main body 31 and discharges the combustion gas from the combustion gas channel 30a to the combustion gas channel 200b.

The combustion gas supplied from the combustion gas supply part 35 to the combustion gas flow path 30a flows from the upper end side to the lower end side of the center pipe 32a while heating the outer peripheral surface 32d of the center pipe 32a, and is discharged from the combustion gas discharge part 36. Is done.

The gland packing 37 is a member that blocks the combustion gas in the combustion gas flow path 30a from flowing out from the upper plate 31d of the main body 31 to the outside. The gland packing 37 is an annular member that is provided in contact with the lower surface of the upper plate 31 d of the main body 31 and has an inner peripheral surface 37 d that contacts the outer peripheral surface 32 d of the reaction tube 32.

The gland packing 37 is configured in a state where the ceramic board 37a, the ceramic board 37b, and the ceramic fiber 37c are in close contact with each other. By using the ceramic fiber 37c, which is a woven material that can be deformed relatively easily, the sealing performance at the portion in contact with the heat insulating material 31b and the heat resistant material 31c is enhanced.

The gland packing 38 is a member that blocks combustion gas in the combustion gas passage 30a from flowing out from the bottom surface 31e of the main body 31 to the outside. The gland packing 38 is an annular member that is provided in contact with the upper surface of the bottom plate 31 e of the main body 31 and has an inner peripheral surface 38 d that contacts the outer peripheral surface 32 d of the reaction tube 32.

The gland packing 38 is configured in a state where the ceramic board 38a, the ceramic board 38b, and the ceramic fiber 38c are in close contact with each other. By using the ceramic fiber 38c, which is a fibrous material that can be deformed relatively easily, the sealing performance at the portion in contact with the heat insulating material 31b and the heat resistant material 31c is enhanced.

As shown in FIG. 12, the gland packing 39 is a member that blocks outflow of water gas from the mounting position at the mounting position of the lower end portion 32 c of the reaction tube 32 and the water gas outlet nozzle 34. The gland packing 39 is an annular member in plan view having an inner peripheral surface 39d that contacts each of the outer peripheral surface 32d of the reaction tube 32 and the outer peripheral surface 34a of the water gas outlet nozzle 34.

As shown in FIG. 12, the gland packing 39 includes an annular packing member 39a, an annular packing member 39b, and a packing pressing member 39c. By fastening the packing holding member 39c to the bottom plate 31e with fastening bolts, the packing member 39a and the packing member 39b contract in the axis Z direction and expand in the radial direction perpendicular to the axis Z. When the gland packing 39 expands in the radial direction, the inner circumferential surface 39d of the gland packing 39 comes into contact with the outer circumferential surface 32d of the reaction tube 32 and the outer circumferential surface 34a of the water gas outlet nozzle 34 to form a sealing region.

Next, the pyrolysis furnace 30, the temperature reducer 40, the cyclone 50, the steam generator 80, the steam superheater 81, and peripheral devices according to this embodiment will be described with reference to FIG. 13.

As shown in FIG. 13, the carbide supply path 101 includes a screw conveyor 101a, a clinker removing device 101b, a belt conveyor 101c, a magnetic separator 101d, a screw conveyor 101e, and a screw conveyor 101f.

The screw conveyor 101a is a device that conveys the carbide discharged from the carbonization furnace 20. The screw conveyor 101a accommodates a screw in a linearly extending cylindrical body. The screw conveyor 101a conveys the carbide along the extending direction of the cylinder by rotating the screw inside the cylinder by the driving force of the motor.

The clinker removing device 101b is a device that removes a clinker having a particle size of a certain size or more from the carbide discharged from the screw conveyor 101a with a net or the like. The carbide from which the clinker has been removed is transported to the magnetic separator 101d by the belt conveyor 101c.

The magnetic separator 101d is a device that removes an iron layer such as a nail contained in the carbide with a magnet, and the carbide from which the iron scrap has been removed is supplied to the screw conveyor 101e.

The screw conveyor 101e and the screw conveyor 101f are apparatuses for conveying carbides, respectively. The screw conveyor 101f supplies the carbide to the nitrogen replacement unit 30b included in the pyrolysis furnace 30. In addition, since the structure of the screw conveyor 101e and the screw conveyor 101f is the same as that of the screw conveyor 101a, description is abbreviate | omitted.

The screw conveyor 101e and the screw conveyor 101f carry the carbide to the upper side of the pyrolysis furnace 30 because the carbide is supplied from above the pyrolysis furnace 30 and in the reaction tube 32 of the pyrolysis furnace 30 by its own weight. This is to allow carbide to pass through. By passing the reaction tube 32 of the pyrolysis furnace 30 through the dead weight of the carbide, the entire region from the upper end to the lower end of the reaction tube 32 can be used as a region for promoting the pyrolysis reaction. Further, since the carbide is passed through the reaction tube 32 by its own weight, no special power for moving the carbide is required.

Carbide is transported in two stages, screw conveyor 101e and screw conveyor 101f, because each screw conveyor requires an expensive motor with a large driving force by reducing the power required to rotate the screw. This is to avoid the above.

The nitrogen replacer 30b is a device that constitutes the pyrolysis furnace 30, and is a device for replacing oxygen contained in the air supplied from the screw conveyor 101f together with the carbide with inert nitrogen gas.

The nitrogen purger 30b is disposed on each of an upper side connected to the screw conveyor 101f and a lower side connected to the reaction tube head 33, and an electric control valve (for example, an open / closed state is controlled by the control device 90) Ball valve).

The control device 90 supplies carbide to the inside of the nitrogen purger 30b by opening the upper control valve and closing the lower control valve. When the amount of carbide supplied to the inside of the nitrogen purger 30b reaches a certain amount, the control device 90 stops the transportation of the carbide by the screw conveyor 101f and closes the control valve above the nitrogen purger 30b. .

Nitrogen gas is always supplied to the nitrogen replacer 30b from a device that generates nitrogen gas such as an air separation device. Therefore, when a certain amount of time has elapsed with the control valves above and below the nitrogen purger 30b being opened, the air supplied to the interior of the nitrogen purger 30b together with the carbide is discharged to the outside and the interior is replaced with nitrogen gas. It becomes a state.

After the inside of the nitrogen purger 30b has been replaced with nitrogen gas, the control device 90 switches the control valve below the nitrogen purger 30b to the open state and transfers the nitrogen purger 30b to the reaction tube head 33. Supply carbide.

The controller 90 supplies carbide to the reaction tube head 33 from the nitrogen purger 30b, and then closes the control valve below the nitrogen purger 30b. Further, the control device 90 then opens the control valve above the nitrogen purger 30b and supplies new carbide into the nitrogen purger 30b.

As described above, the control device 90 controls the opening and closing of the control valves above and below the nitrogen purger 30b, so that the gas supplied to the reaction tube head 33 together with the carbide is nitrogen gas. This nitrogen gas is an inert gas that does not react with the water gas generated in the reaction tube 32. Therefore, it is possible to suppress the air containing oxygen together with the carbide from being supplied to the reaction tube 32 and causing the reaction between oxygen and the water gas to reduce the yield of the water gas.

The char collection device 41 includes a nitrogen purger 41a and a char collection unit 41b.

The nitrogen replacer 41a is a device for replacing the water gas supplied from the temperature reducer 40 together with the unreacted portion of the carbide with inert nitrogen gas.

The char recovery unit 41b is a device that recovers an unreacted portion of the carbide and supplies it to the nitrogen replacement device 30b from a supply path (not shown). Details of this will be described later as a return system.

The chamber replacer 41a is disposed on the upper side connected to the temperature reducer 40 and the lower side connected to the char recovery unit 41b, and is an electric control valve (open / close state controlled by the control device 90). For example, a ball valve).

The control device 90 opens the upper control valve and closes the lower control valve to supply unreacted carbide to the inside of the nitrogen purger 41a. When the unreacted amount of the carbide supplied into the nitrogen purger 41a reaches a certain amount, the control device 90 closes the control valve above the nitrogen purger 41a.

Nitrogen gas is always supplied to the nitrogen replacer 41a from a device that generates nitrogen gas such as an air separation device. Therefore, when the upper and lower control valves of the nitrogen purger 41a are closed and a certain time elapses, the water gas supplied into the nitrogen purger 41a together with the unreacted portion of the carbide is discharged to the outside, and the interior is filled with nitrogen. The gas is replaced. The water gas discharged from the nitrogen purger 41a is supplied to the flare stack 71.

After the inside of the nitrogen purger 41a is replaced with nitrogen gas, the control device 90 switches the control valve below the nitrogen purger 41a to the open state, and the carbide is transferred from the nitrogen purger 41a to the char recovery unit 41b. The unreacted portion is supplied.

The control device 90 closes the control valve below the nitrogen purger 41a after supplying the unreacted portion of the carbide from the nitrogen purger 41a to the char recovery unit 41b. In addition, the control device 90 then opens the control valve above the nitrogen purger 41a and supplies new unreacted carbon carbide into the nitrogen purger 41a.

As described above, the control device 90 controls the opening and closing of the control valves above and below the nitrogen purger 41a, so that the water gas supplied to the char recovery unit 41b together with the unreacted carbide is supplied to the char recovery unit 41b. It is prevented from being supplied.

The residue collection device 51 has a nitrogen purger 51a and a residue collection unit 51b.

The nitrogen replacer 51a is a device for replacing the water gas supplied from the cyclone 50 together with the residue with inert nitrogen gas.

The residue collection unit 51b is a device that collects the residue discharged from the nitrogen purger 51a.

The nitrogen purger 51a is disposed on each of an upper side connected to the cyclone 50 and a lower side connected to the residue collecting unit 51b, and an electric control valve (for example, a ball valve) whose opening / closing state is controlled by the control device 90 is provided. Valve). Nitrogen gas is always supplied to the nitrogen replacer 51a from a device that generates nitrogen gas such as an air separation device.

The control device 90 controls the control valve of the nitrogen purger 51a in the same manner as the control valve of the nitrogen purger 41a, and prevents water gas from being supplied to the residue recovery unit 51b. . The method by which the control device 90 controls the control valve of the nitrogen purger 51a is the same as the method by which the control device 90 controls the control valve of the nitrogen purger 41a, and the description thereof is omitted.

The steam generator 80 includes a steam generation unit 80a and a steam circulation tank 80b.

The steam generating unit 80a is provided in a heat transfer tube (not shown) that circulates water that exchanges heat with combustion gas, and a jacket (not shown) that circulates water inside the tube formed to cover the heat transfer tube. ). Water is supplied to the heat transfer tube and the jacket from the steam circulation tank 80b.

The steam circulation tank 80b is supplied with water from the water supply device 82 and supplies water to the heat transfer tube and the jacket of the steam generation unit 80a. The hot water heated by the jacket and the steam generated by heating the heat transfer tube with the combustion gas are respectively collected in the steam circulation tank 80b.

The steam circulation tank 80b supplies the steam (saturated steam) supplied from the heat transfer tube of the steam generation unit 80a to the steam superheater 81.

A new and improved system of the pyrolysis furnace in the biomass power generation system described above will be described with reference to FIG.

FIG. 14 is a configuration diagram of a return system for a pyrolysis furnace according to another embodiment of the present invention. This return system is related to the char recovery device 41 described with reference to FIG. 1, and a part of the return system has been described, but is configured in cooperation with the char recovery device. Further, the pyrolysis furnace 30 shown in FIG. 14 is basically the same as the configuration of FIG. 10 shown as an embodiment of the pyrolysis furnace 30 of FIGS. The same applies to each device described in FIG. 13 as the peripheral equipment of the pyrolysis furnace 30 of the present embodiment. Accordingly, in FIG. 14, the same reference numerals as those used in the respective drawings described above have the same functions.

The present invention focuses on the unreacted portion of the carbide discharged from the pyrolysis furnace 30 and will be described in detail below with reference to FIG.

14, a temperature reducer 40 and a char recovery device 41 are arranged at the lower stage of the pyrolysis furnace 30, and a carbide receiving hopper 30 c and a nitrogen purger 30 b are arranged at the upper stage of the pyrolysis furnace 30. The char recovery device 41 includes a nitrogen purger 41a, a char recovery unit 41b, a carbide transport unit 41c, a carbide recovery unit 41d, and the like. An unreacted material conveyance path 30d is provided between the carbide conveyance unit 41c and the receiving hopper 30c. The transport unit 41c, the transport path 30d, and the like can be configured by a conveyor, a lifter, or the like and literally become a transport path.

By selectively switching the carbide discharged from the char recovery unit 41b to the carbide transfer unit 41c, the unreacted portion can be input again into the pyrolysis furnace 30 through the transfer path 30d. This collection / conveyance means constitutes a return system for the pyrolysis furnace.

With this return system, the unreacted portion of the carbide can be repeatedly charged into the pyrolysis furnace 30, and the residence time in the reaction tube 33 can be lengthened.

<Example>
As a result of the implementation verification by the inventors, the residence time in the reaction tube is increased several times by adopting the return system of the pyrolysis furnace of the present invention, so that the aqueous reaction rate is 75% to 80% to 90% to Increased to 95%. As a result, it was found that the amount of water gas increased from 1.19 times to 1.27 times.

(Example)
・ Installed a return system that can return 50% to 200% of the unreacted part. ・ Residence time in the reaction tube of the pyrolysis furnace: 1.5 to 3 times, so that the aqueous reaction rate can be reduced from 75% to 80%. Increased to 90-95%.

(1) In the case of power transmission If the return system is not adopted is assumed to be 100 KW, transmission of 119 KW to 127 KW is possible when the return system is installed.
When the raw material (wood waste) is 2 To / h (water content 15 wt%), the transmission amount increases from 1200 KWH to 1430 KWH to 1520 KWH.

(2) In the case of hydrogen supply If the return system is not adopted is 100 Nm3 / h, hydrogen of 119 Nm3 / h to 127 Nm3 / h can be supplied when the return system is installed.
When the raw material (wood waste) is 2 To / h (water content 15 wt%), the amount of hydrogen increases from 660 Nm3 / h to 790 Nm3 / h to 838 Nm3 / h (99.999 V% hydrogen).

Next, the dryer 10 of this embodiment is demonstrated using FIG.

FIG. 15 is a block diagram of the dryer according to the embodiment of the present invention shown in FIG.

The dryer 10 is a dry kiln of a type called a rotary kiln, and includes a combustion gas introduction unit 10b, a rotating body 10c, and a discharge unit 10d.

The combustion gas introduction unit 10b introduces the combustion gas supplied from the combustion gas passage 200d into the dryer 10 and guides the introduced combustion gas into the rotating body 10c.

The rotating body 10c is a cylindrical member formed in a direction extending along the axis W, and rotates around the axis W when it receives rotational power from a drive motor.

Further, organic waste is supplied into the rotating body 10c from the raw material supply path 11a. The organic waste supplied to the inside of the rotating body 10c is guided toward the discharge unit 10d while being dried by the combustion gas guided from the combustion gas introduction unit 10b.

The organic waste is directly heated by the combustion gas while being stirred by the rotation of the rotating body 10c, and is conveyed by the flow of the combustion gas from one end to the other end of the rotating body 10c.

The discharge unit 10d collects the dried organic waste while being conveyed by the rotating body 10c, and supplies it to the raw material supply path 10a. The organic waste supplied to the raw material supply path 10 a is supplied to the carbonization furnace 20 via the fixed amount supply device 12.

Further, the discharge unit 10d supplies the combustion gas introduced from the combustion gas introduction unit 10b through the inside of the rotating body 10c to the combustion gas channel 200e. The combustion gas supplied to the combustion gas flow path 200e is supplied to the exhaust gas cooling and cleaning device 13.

Next, a biomass power generation system according to another embodiment of the present invention will be described with reference to FIG. The biomass power generation system shown in FIG. 16 has the same basic configuration as the biomass power generation system using water gas via the carbonization furnace and the pyrolysis furnace according to the present invention shown in FIG. 1, and a part of the description is omitted.

In the biomass power generation system B shown in FIG. 16, the raw material biomass crusher 10 a, the dryer 10, the carbonization furnace 20, the pyrolysis furnace 30, the temperature reducer 40, the char recovery device 41, the water gas holder 70, and the power generation facility 72 are aqueous. The series leading to the first power supply for generating power by supplying gas is substantially the same as the biomass power generation system A of the first embodiment described above. The second embodiment of the present invention differs from the first embodiment in that the combustion gas generated in the carbonization furnace 20 is supplied in the order of the pyrolysis furnace 30, the steam generator 80, and the boiler 76, and the heat source of each device. Then, saturated steam is recovered by the boiler 76, supplied to the steam turbine power generation facility 75, generated, and transmitted to the second power supply, and part of the steam recovered by the boiler 76 is supplied to the steam generator 80 and overheated. The steam is generated and supplied to the pyrolysis furnace 30. In this way, the first power supply for generating power by supplying to the power generation facility 72 by the gas engine or the like using the original pyrolysis gas, and the second power supply for generating power by supplying to the steam turbine power generation facility 75 by the saturated steam recovered from the boiler 76. It is excellent in thermal efficiency in terms of combined cycle power generation, so-called hybrid power generation. Further, the saturated steam generated in the process boiler 76 of the second power supply system is supplied to the steam turbine power generation facility 75, and the steam used in the steam turbine power generation facility 75 is returned to the soft water tank 78 by the condenser 77 and is pumped by the pump 79. By forming a circulation line to be supplied to the process boiler 76, the waste water discharged to the outside is reduced as much as possible, and the use efficiency of water is improved.

The biomass power generation system B according to the embodiment of the present invention supplies combustion exhaust gas generated in the carbonization furnace 20 to the pyrolysis furnace 30, and promotes the pyrolysis reaction between the carbide and superheated steam in the pyrolysis furnace 30. By using it as a heat source, it has a feature in improving the thermal efficiency of the biomass power generation system B as a whole. Since the temperature or heat energy required to superheat the steam generated by the boiler 76 with the superheated steam generator 80 is higher than the temperature or heat energy required to generate the steam with the boiler 76, In the embodiment of the invention, in order to improve the thermal efficiency of the biomass power generation system B as a whole, the combustion gas generated in the carbonization furnace 20 is supplied in the order of the pyrolysis furnace 30, the superheated steam generator 80, and the boiler 76, and the heat source of each device. Therefore, the thermal efficiency of the biomass power generation system B as a whole can be improved.

Each embodiment described above is illustrated for the understanding of the present invention, and the present invention is not limited to these embodiments, but is defined by the description of the scope of claims. Further, unless it departs from the technical idea of the present invention, those equivalent to the configurations described in the claims are also included in the scope of protection of the present invention.

The biomass power generation system according to the present invention increases the combustion efficiency by controlling the temperature of the carbonization furnace, enables the pyrolysis furnace to be sealed, increases the gasification efficiency, and keeps the composition ratio of the generated water gas constant. Impurities such as nitrogen, sulfur and tar are removed by the carbonization furnace and the pyrolysis gasifier, so that high power generation efficiency can be obtained, and safe and efficient power can be supplied. Effective use of biomass is extremely useful for energy saving, natural environment protection and economics.

DESCRIPTION OF SYMBOLS 10 ... Dryer 13 ... Exhaust gas cooling washing device 20 ... Carbonization furnace 20a ... Gap 21 ... Main body part 22 ... Cylindrical part 23 ... Organic waste input part 24 ... Carbide discharge part 25 ... Primary air supply part 26 ... Secondary air supply Part 27 ... Combustion

gas discharge part

28a, 28b, 28c ... Temperature sensor (temperature detection part)
28d ... Level sensor (deposition amount detector)
29 ... Carbonization furnace control section (control section)
DESCRIPTION OF SYMBOLS 30 ... Pyrolysis furnace 31 ... Main-body part 32 ... Reaction tube 32f ... 1st inclination board 32g ... 2nd inclination board 34 ... Water gas outlet nozzle 35 ... Combustion gas supply part 36 ... Combustion gas discharge part 40 ... Temperature reducer 41 ... Char recovery device 50 ... cyclone 60 ... water gas cooling device 70 ... water gas holder 72 ... power generation facility 80 ... steam generator 81 ... steam superheater 82 ... water supply device

Claims

Electric power generation using a carbonization furnace that carbonizes biomass, a pyrolysis furnace that generates pyrolysis gas from the carbide and combustion gas obtained in the carbonization furnace, and water gas obtained by cleaning the pyrolysis gas With the device,
An air supply control unit that controls the amount of air supplied to the carbonization furnace is provided,
A biomass power generation system, characterized in that combustion gas whose temperature is controlled by the supply amount of air is supplied to a pyrolysis furnace.
Electric power generation using a carbonization furnace that carbonizes biomass, a pyrolysis furnace that generates pyrolysis gas from the carbide and combustion gas obtained in the carbonization furnace, and water gas obtained by cleaning the pyrolysis gas With the device,
The pyrolysis furnace includes a cylindrical main body, and a reaction tube that protrudes from the upper end of the main body inside the main body.
Between the inner wall of the main body and the outer peripheral surface of the reaction tube is a heating flow path, the reaction tube is a reaction part of carbide and gasifying agent, and the water gas is supplied to the power supply device using the obtained decomposition gas A biomass power generation system characterized by
Electric power generation using a carbonization furnace that carbonizes biomass, a pyrolysis furnace that generates pyrolysis gas from the carbide and combustion gas obtained in the carbonization furnace, and water gas obtained by cleaning the pyrolysis gas With the device,
An air supply control unit that controls the amount of air supplied to the carbonization furnace is provided,
The pyrolysis furnace includes a cylindrical main body, and a reaction tube that protrudes from the upper end of the main body inside the main body.
In the carbonization furnace, the combustion gas whose temperature is controlled by the supply amount of the air is supplied to the pyrolysis furnace,
In the pyrolysis furnace, a heating flow path is provided between the inner wall of the main body and the outer peripheral surface of the reaction tube, and combustion exhaust gas from the carbonization furnace is input and carbide from the carbonization furnace is input into the reaction tube. A biomass power generation system, characterized in that the water gas is supplied to a power supply device using the cracked gas obtained by reaction with a gasifying agent.
Recovery means for recovering unreacted material after the reaction between the carbide and the gasifying agent in the pyrolysis furnace, and transporting the unreacted material from the recovery means to the upper part of the reaction tube of the pyrolysis furnace. A conveying means for
The biomass power generation system according to any one of claims 1 to 3, wherein the unreacted material can be input again into the pyrolysis furnace.
The pyrolysis furnace includes a cylindrical main body portion and a reaction tube protruding from the upper end of the main body portion inside the main body portion, and a heating flow path between the inner wall of the main body portion and the outer peripheral surface of the reaction tube. And the reaction tube interior is a reaction part of carbide and gasifying agent, and a water gas is obtained using the obtained cracked gas,
A recovery means for recovering the unreacted material after the reaction between the carbide and the gasifying agent in the pyrolysis furnace, and a transport means for transporting the unreacted material from the recovery means to the upper part of the reaction tube of the pyrolysis furnace,
A return system for a pyrolysis furnace, wherein the unreacted material can be charged again into the pyrolysis furnace.