JP6759492B2 - Carbide production equipment, carbide production methods, and carbide production systems - Google Patents

Description

The present invention relates to a carbide production apparatus, a carbide production method, and a carbide production system.

Conventionally, a carbonization furnace in which an organic substance is partially burned and the organic substance is carbonized by the combustion heat is known (see, for example, Patent Document 1).
In the carbonization furnace disclosed in Patent Document 1, a carbonized portion for carbonizing a solid content containing a large amount of carbide is formed above a region formed between a substantially cylindrical main body and a cylindrical body housed in the main body. A non-combustible part that extinguishes carbonized material is formed below.

Patent Document 1 focuses on the problem that the carbonization efficiency decreases when the atmospheric temperature of the carbonized portion decreases due to the air blown from the inside of the cylindrical body. Patent Document 1 has a double-walled structure in which a cylindrical body is provided with a preheating chamber inside, and air heated in the preheating chamber is supplied to the carbonized portion to prevent a decrease in the atmospheric temperature of the carbonized portion.

Japanese Patent No. 4226066

Organic matter such as waste wood has carbon, oxygen, hydrogen and nitrogen as the main elements, and also has a trace amount of inorganic components such as calcium. In order to obtain a carbide having a high carbon component content (hereinafter, also referred to as carbon content) and to increase the carbon component yield (hereinafter, also referred to as carbon yield) using such an organic substance as a raw material, the carbon component It is necessary to carry out a carbonization treatment that sufficiently removes other components while suppressing the amount of decrease in the amount of carbon.

However, if the organic substance is carbonized at a high temperature in order to remove components other than the carbon component, a part of the carbon component is completely burned and the carbon yield is lowered. Further, if the carbonization treatment of the organic substance is performed at a low temperature at which the carbon component is not completely burned in order to increase the carbon yield, the carbon content of the carbonized material is lowered because the components other than the carbon component are not sufficiently removed. ..
Patent Document 1 discloses that the cylindrical body has a double-walled structure in order to prevent a decrease in the atmospheric temperature of the carbonized portion, but does not disclose a structure that enhances both the carbon yield and the carbon content. ..

The present invention has been made in view of such circumstances, and is a carbide manufacturing apparatus capable of producing carbides in which carbon components other than carbon components are sufficiently removed while suppressing a decrease in carbon components contained in organic substances. , A carbide production method, and a carbide production system.

The present invention employs the following means in order to solve the above problems.
The charcoal-producing apparatus according to one aspect of the present invention is between a main body portion formed in a tubular shape extending along an axis and an inner peripheral surface of the main body portion formed in a tubular shape extending along the axis. A tubular portion having an outer peripheral surface that forms a gap for carbonizing the organic matter, an organic matter charging portion for charging the organic matter into the gap, and air for supplying combustion air for partially burning the organic matter deposited in the gap. The supply section, a carbide discharge section that discharges the carbonized substance obtained by carbonizing the organic substance from the gap, and the above-mentioned so that the organic substance is maintained in a predetermined temperature range in the gap and the organic substance is deposited in the gap over a predetermined time. A first temperature detection unit that includes a control unit that controls the carbonized state of the organic substance and detects the ambient temperature of the region where the partial combustion is performed, and a second temperature detection unit that detects the temperature of the organic substance deposited in the gap. In the third temperature detection unit that detects the temperature of the combustion gas of the combustion gas discharge unit that discharges the combustion gas of the organic substance, the accumulation amount detection unit that detects the accumulation amount of the organic substance accumulated in the gap, and the air supply unit. A primary air supply unit that supplies external air to burn organic matter, and a secondary air supply unit that supplies external air to burn the flammable gas contained in the combustion gas between the air supply unit and the combustion gas discharge unit. A rotating body provided in the air supply unit and the carbon dioxide discharge unit at a position facing the carbon dioxide discharge port and the lower end of the gap and rotating around the axis to guide the carbon dioxide from the lower end of the gap to the discharge port. The control unit has a drive unit that rotates the rotating body around the axis, and the control unit performs the following control with a control cycle of 3 seconds. When the detection temperature of the first temperature detection unit is lower than the predetermined first atmosphere temperature, the amount of air supplied from the primary air supply unit is increased. When the detection temperature of the second temperature detection unit is equal to or higher than the predetermined carbide temperature, the rotation speed of the rotating body is rotated at a second rotation speed lower than the first rotation speed of normal operation. When the detection temperature of the third temperature detection unit is lower than the predetermined first combustion gas temperature, the amount of air supplied from the secondary air supply unit is reduced. Further, the following control is performed. The amount of air supplied from the primary air supply unit when the detection temperature of the first temperature detection unit is equal to or higher than the first atmosphere temperature and further exceeds a predetermined second atmosphere temperature higher than the first atmosphere temperature. To reduce. When the detection temperature of the second temperature detection unit is lower than the predetermined carbide temperature, and when the detected accumulation amount of the accumulation amount detection unit is less than or equal to the predetermined accumulation amount, the rotation speed of the rotating body is set to the second rotation speed. When the amount of accumulation exceeds the predetermined amount, the rotating body is rotated at the first rotation speed. When the detection temperature of the third temperature detection unit is equal to or higher than the predetermined first combustion gas temperature and further exceeds the predetermined second combustion gas temperature higher than the first combustion gas temperature, the secondary air supply unit Increase the air supply of. As a result, the state related to carbide production can be maintained in a desired state.

According to the carbide manufacturing apparatus according to one aspect of the present invention, organic matter is charged from the organic matter charging portion into the gap formed between the inner peripheral surface of the main body portion and the outer peripheral surface of the tubular portion in the normal operation state of the carbonization furnace. Then, the organic matter charged from the organic matter charging portion is deposited from the lower side to the upper side of the gap along the axis. The organic matter on the upper layer side of the gap is partially burned by the combustion air supplied from the air supply unit and guided to the lower layer side of the gap. The organic matter on the lower layer side of the gap is blocked by the organic matter on the upper layer side, and the lower layer side of the gap is a carbide refining / cooling region where solids containing a large amount of carbon components are refined and cooled. In the carbide refining / cooling region, the solid content containing a large amount of carbon component is refined while being further carbonized in a state where the oxygen concentration is low, and is gradually cooled as it approaches the lower end of the gap. As a result, the temperature of the carbide discharged from the lower end of the gap can be lowered.

Further, according to the carbide production apparatus according to one aspect of the present invention, the carbonization state of the organic substance is controlled by the control unit so that the organic substance is maintained in a predetermined temperature range in the gap. Therefore, it is possible to suppress the problem that the organic matter becomes a high temperature and most of the carbon components are completely burned, and the organic matter becomes a low temperature in the gap and the other components other than the carbon component cannot be sufficiently removed. it can. Here, the predetermined temperature range is, for example, preferably 900 ° C. or higher and 1200 ° C. or lower, and more preferably 1000 ° C. or higher and 1100 ° C. or lower.

Further, according to the carbide production apparatus according to one aspect of the present invention, the control unit controls the organic matter to be deposited in the gap over a predetermined time. Therefore, it is possible to suppress a problem that the time for the organic substance to be deposited in the gap is shortened and the components other than the carbon component cannot be sufficiently removed from the organic substance. Here, the predetermined time is preferably in the range of, for example, 30 minutes or more and 50 minutes or less.
As described above, according to the carbide production apparatus according to one aspect of the present invention, it is possible to produce a carbide from which other components other than the carbon component are sufficiently removed while suppressing a decrease in the carbon component contained in the organic substance. ..

In the carbide production apparatus according to one aspect of the present invention, the control unit controls the supply amount of the combustion air supplied by the air supply unit so that the organic matter is maintained in the predetermined temperature range in the gap. and, in the configuration and to Rukoto said carbide discharging portion so that the organic material is deposited on the gap over a predetermined time to control the emissions of the carbide to be discharged, by controlling the supply amount of combustion air It is possible to maintain the organic matter in a predetermined temperature range in the gap, control the amount of carbide emitted so that the organic matter is deposited in the gap over a predetermined time, and produce a carbide having a high carbon content while increasing the carbon yield. it can.

In carbide manufacturing apparatus having the above structure, the front Symbol controller, in Rukoto Gyosu braking control period of 3 seconds, while increasing the carbon MotoOsamuritsu can be produced with a high carbon content carbide.

In the carbide production apparatus according to one aspect of the present invention, the carbide discharged from the carbide discharge unit is thermally decomposed with water vapor to generate water gas, and the carbide is discharged from the thermal decomposition unit. It may be configured to include a carbide recovery unit for recovering the carbide.
By doing so, it is possible to recover unreacted carbides while generating water gas by thermally decomposing the carbides having a high carbon content and water vapor in the thermal decomposition section. This unreacted carbide is washed with steam to remove components other than the carbon component. Therefore, it is possible to obtain a carbide having a high carbon content in which components other than the carbon component are satisfactorily removed.

The method for producing carbonized matter according to one aspect of the present invention is between a main body portion formed in a tubular shape extending along an axis and an inner peripheral surface of the main body portion formed in a tubular shape extending along the axis. Using a carbonized material manufacturing apparatus including a tubular portion having an outer peripheral surface for forming a gap for carbonizing the organic substance, an organic substance charging step of charging the organic substance into the gap and a combustion air being supplied to the gap are used. An air supply step of partially burning the organic matter deposited in the gap, a carbonization discharge step of discharging carbonized matter obtained by carbonizing the organic matter from the gap, and a carbonized matter discharging step in which the organic matter is maintained in a predetermined temperature range in the gap and the organic matter is maintained for a predetermined time. A first temperature detection step of detecting the atmospheric temperature of the region where the partial combustion is performed after the organic matter charging step, which comprises a control step of controlling the carbonized state of the organic matter so as to be deposited in the gap. A second temperature detection step of detecting the temperature of the organic substance deposited in the gap, a third temperature detection step of detecting the temperature of the combustion gas in the combustion gas discharging portion of the organic substance, and an amount of the organic substance deposited in the gap. The deposition amount detection step for detecting the above, the primary combustion air supply step for supplying external air for burning organic matter in the air supply step, and the flammable gas contained in the combustion gas after the air supply step. The secondary combustion air supply step of supplying external air for burning is provided at a position facing the lower end of the gap in the carbonization discharge step, and the lower end of the gap is provided by a rotating body rotating around the axis. It has a carbonization discharge step of guiding the carbonization from the discharge port to the discharge port, and in the control step, the following control is performed in a control cycle of 3 seconds. When the detection temperature of the first temperature detection step is lower than the predetermined first atmosphere temperature, the amount of air supplied from the primary air supply step is increased. When the detection temperature in the second temperature detection step is equal to or higher than the predetermined carbide temperature, the rotation speed of the rotating body is rotated at a second rotation speed lower than the first rotation speed in normal operation. When the detection temperature of the third temperature detection step is lower than the predetermined first combustion gas temperature, the amount of air supplied from the secondary air supply step is reduced. Further, the following control is performed. The amount of air supplied from the primary air supply step when the detection temperature in the first temperature detection step is equal to or higher than the first atmospheric temperature and further higher than the first atmospheric temperature to a predetermined second atmospheric temperature or lower. To reduce. When the detection temperature in the second temperature detection step is lower than the predetermined carbide temperature, and when the detection deposit amount in the deposit amount detection step is equal to or less than the predetermined deposit amount, the rotation speed of the rotating body is set to the second rotation speed. When the amount of accumulation exceeds the predetermined amount, the rotating body is rotated at the first rotation speed. From the secondary air supply step when the detection temperature in the third temperature detection step is equal to or higher than the predetermined first combustion gas temperature and further exceeds the predetermined second combustion gas temperature higher than the first combustion gas temperature. Increase the air supply of.

According to the carbide production method according to one aspect of the present invention, the carbonization state of the organic substance is controlled by the control step so that the organic substance is maintained in a predetermined temperature range in the gap. Therefore, it is possible to suppress the problem that the organic matter becomes a high temperature and most of the carbon components are completely burned, and the organic matter becomes a low temperature in the gap and the components other than the carbon component cannot be sufficiently removed. it can.
Further, according to the carbide production method according to one aspect of the present invention, the organic matter is controlled to be deposited in the gap over a predetermined time by the control step. Therefore, it is possible to suppress a problem that the time for the organic substance to be deposited in the gap is shortened and the components other than the carbon component cannot be sufficiently removed from the organic substance.
As described above, according to the carbide production method according to one aspect of the present invention, it is possible to produce a carbide from which other components other than the carbon component are sufficiently removed while suppressing a decrease in the carbon component contained in the organic substance. ..

In the carbide production method according to one aspect of the present invention, the control step controls the supply amount of the combustion air supplied by the air supply step so that the organic matter is maintained in the predetermined temperature range. organic matter in configuration and be Rukoto said carbide discharging process to deposit in the gap over a predetermined time to control the emissions of the carbide to be discharged, the clearance organics by controlling the supply amount of combustion air It is possible to produce carbides having a high carbon content while maintaining a predetermined temperature range and controlling the amount of carbides emitted so that organic substances are deposited in the gaps over a predetermined time to increase the carbon yield.

In the carbide manufacturing method of the above-described configuration, pre-SL control step, in Rukoto Gyosu braking control period of 3 seconds, while increasing the carbon MotoOsamuritsu can be produced with a high carbon content carbide.

The charcoal product manufacturing system according to one aspect of the present invention includes the charcoal product manufacturing apparatus according to any one of the above, a heat exchange unit for heat exchange between the combustion gas discharged from the charcoal product manufacturing apparatus and a heat medium, and the above. It is provided with a power generation unit that obtains power from a heat medium heated by the heat exchange unit to generate electricity.
By doing so, the heat of the combustion gas discharged from the carbide manufacturing apparatus can be recovered as the power of the power generation unit, and the energy efficiency of the entire system can be increased.

The carbide production system according to one aspect of the present invention may include a drying section for drying the organic substance charged from the organic substance charging section by the combustion gas exchanged with heat in the heat exchange section.
By doing so, the heat of the combustion gas discharged from the carbide production apparatus can be used for drying the organic matter, and the heat of the combustion gas can be further effectively utilized.

According to the present invention, it is possible to provide a carbide production apparatus, a carbide production method, and a carbide production system capable of producing a carbide from which a component other than carbon is sufficiently removed while suppressing a decrease in a carbon component contained in an organic substance. it can.

It is an overall block diagram which shows one Embodiment of the water gas generation system. It is a vertical sectional view of the carbonization furnace shown in FIG. It is an enlarged view of the main part of the carbonization furnace shown in FIG. It is an end view of the carbonization furnace shown in FIG. 2, (a) is the end view of the arrow AA, and (b) is the end view of the arrow BB. It is a flowchart which shows the control method of the air volume of the primary combustion fan by a carbonization furnace control part. It is a flowchart which shows the control method of the air volume of a secondary combustion fan by a carbonization furnace control part. It is a flowchart which shows the control method of the rotation speed of a turntable by a carbonization furnace control part. It is a vertical sectional view of the pyrolysis furnace shown in FIG. It is a block diagram which shows the pyrolysis furnace, a warmer, a cyclone, a steam generator, and a steam superheater shown in FIG. It is a block diagram which shows the dryer shown in FIG. It is a figure which shows the image which image | photographed the carbide obtained by the water gas generation system with a scanning electron microscope. It is an overall block diagram which shows the carbide manufacturing system of 2nd Embodiment.

<First Embodiment>
Hereinafter, the water gas generation system (carbide production apparatus; carbide production system) 100 of the first embodiment of the present invention will be described with reference to the drawings.
In the water gas generation system 100 of the present embodiment, after carbonizing organic waste which is a waste containing carbon to generate carbide, superheated steam (hereinafter, also referred to as “steam”) is used as a gasizing agent. This is a system that produces water gas (mixed gas containing hydrogen gas, carbon monoxide gas, and carbon dioxide gas as the main components) by thermally decomposing carbides.
In addition, the water gas generation system 100 of the present embodiment is also a carbide production system capable of producing carbides in which components other than carbon components are sufficiently removed while suppressing a decrease in carbon components contained in organic waste. ..

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. Although various organic wastes as exemplified above can be used as raw materials for producing water gas, it is particularly preferable to use wood waste materials (also referred to as “woody biomass”). Further, in the present embodiment, organic waste is used, but organic matter that should not be discarded may be used as a raw material for carbide.

As shown in the overall configuration diagram of FIG. 1, the water gas generation system 100 includes a dryer (drying unit) 10 for drying organic waste, a hopper 11 for storing organic waste to be charged into the dryer 10, and drying. A hopper 12 for storing organic waste dried by the machine 10, a carbonization furnace 20 for producing carbonized products from the dried organic waste, and a pyrolysis reaction between the carbonized products produced in the carbonizing furnace 20 and a gas agent. Pyrolysis furnace (pyrolysis unit) 30 to generate water gas, a thermostat 40 to cool the water gas generated in the pyrolysis furnace 30, and char to recover carbonized matter discharged from the pyrolysis furnace 30. The recovery device (carbonization recovery unit) 41, the cyclone 50 that removes unreacted carbonization and residues from the water gas supplied from the thermostat 40, and the residue that recovers the unreacted carbonization and residues removed by the cyclone 50. It is provided with a recovery device (carbonized material recovery unit) 51.

Further, the water gas generation system 100 includes a water gas cooling device 60 for cooling the water gas from which carbides and residues have been removed by the cyclone 50, a water gas holder 70 for storing the water gas cooled by the water gas cooling device 60, and the water gas holder 70. A flare stack 71 that incinerates excess water gas and the like, a power generation facility 72 that uses water gas as fuel, a hydrogen purification device 73 that purifies water gas from water gas, and a steam generator 80 that generates saturated steam from water. , A steam superheater 81 that superheats the steam generated by the steam generator 80, a water supply device 82 that supplies water to the steam generator 80, and a control device 90 that controls the entire water gas generation system 100. ..
Hereinafter, each part included in the water gas generation system 100 will be described.

The dryer 10 is a device that dries the organic waste with combustion gas and supplies the dried organic waste to the carbonization furnace 20. Organic waste is supplied to the dryer 10 from the hopper 11 that stores the organic waste via the raw material supply path 11a. Further, the combustion gas discharged from the steam generator 80 is supplied to the dryer 10 via the combustion gas flow path 200d as a heat source for drying the organic waste.

The organic waste supplied from the hopper 11 to the dryer 10 is, for example, woody biomass crushed by a crusher (not shown) to a length of 5 mm or more and 60 mm or less. Further, as the organic waste, for example, one containing water in a weight ratio of about 55% is used. The dryer 10 heats and dries the woody biomass containing water at a weight ratio of about 55%, thereby reducing the water content of the organic waste to a weight ratio of about 15%.

The dryer 10 supplies the organic waste dried by the heat of the combustion gas to the hopper 12 via 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 / cleaning device 13 via the combustion gas flow path 200e. The temperature of the combustion gas supplied by the dryer 10 to the exhaust gas cooling / cleaning device 13 is adjusted to be 150 ° C. or higher and 210 ° C. or lower.

The exhaust gas cooling / cleaning device 13 is a device that detoxifies the combustion gas by removing harmful substances such as sulfur oxides (SO _x ), sulfuric acid (H ₂ SO ₄ ), and hydrochloric acid (HCl) contained in the combustion gas. The exhaust gas cooling / cleaning device 13 cools the combustion gas (exhaust gas) from which harmful substances have been removed while detoxifying it, and then discharges it into the atmosphere.
The exhaust gas cooling / cleaning device 13 is, for example, a scrubber, 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.

The carbonization furnace 20 is a device that produces carbonized matter and combustion gas by partially burning dry organic waste. The carbonization furnace 20 is supplied with dried organic waste from a hopper 12 that stores organic waste via a raw material supply path 12a.
The carbide furnace 20 supplies the carbides produced by partial combustion of organic waste to the pyrolysis furnace 30 via the carbide supply path 101. Further, the carbonization furnace 20 supplies the combustion gas generated by the partial combustion of the organic waste to the pyrolysis furnace 30 via the combustion gas flow path 200a.

The entire amount of the carbides produced in the carbonization furnace 20 may be supplied to the pyrolysis furnace 30, or a part of the carbides produced in the carbonization furnace 20 may be recovered by a recovery device (not shown). May be good. When a part of the carbide is recovered by the recovery device, the carbide itself can be obtained as a product of the water gas generation system 100.

The thermal decomposition furnace 30 is an apparatus for generating water gas by heating the carbides produced by the carbonization furnace 20 together with superheated steam with combustion gas and causing a thermal decomposition reaction. The carbide produced by the carbonization furnace 20 is supplied to the pyrolysis furnace 30 via the carbide supply path 101. Further, the superheated steam generated by the steam superheater 81 is supplied to the pyrolysis furnace 30 as a gasifying agent. Further, the combustion gas is supplied to the thermal decomposition furnace 30 from the combustion gas flow path 200a as a heat source for promoting the thermal decomposition reaction.

The pyrolysis furnace 30 causes a pyrolysis reaction between the carbide and the superheated steam to generate an aqueous gas containing hydrogen gas, carbon monoxide gas, and carbon dioxide gas as main components. The pyrolysis reaction between carbides and superheated steam is mainly the reaction 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 represented by the formula (1) is an endothermic reaction, and the water gas shift reaction represented by the formula (2) is an exothermic reaction. The endothermic reaction represented by the formula (1) has a larger heat absorption than the exothermic reaction represented by the formula (2). Therefore, the pyrolysis reaction between the carbide and the superheated steam becomes an endothermic reaction as a whole.

The temperature of the carbides supplied to the pyrolysis furnace 30 is adjusted to be equal to or higher than normal temperature (for example, 25 ° C) and lower than 350 ° C. Further, the temperature of the superheated steam supplied to the pyrolysis furnace 30 is adjusted to be 730 ° C. or higher and 830 ° C. or lower. Further, 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. Further, the temperature of the water gas generated by the pyrolysis furnace 30 is adjusted to be 650 ° C. or higher and 850 ° C. or lower.

The pyrolysis furnace 30 supplies the water gas produced by the pyrolysis reaction with unreacted carbides and residues to the cooler 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 via 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 higher and 920 ° C. or lower.

The heater 40 is a device that lowers the temperature of the water gas supplied from the water gas supply path 102 by spraying water which is a liquid. Water is supplied to the heater 40 from the water supply device 82 by a water supply pump (not shown). The heater 40 supplies the cooled water gas to the cyclone 50 via the water gas supply path 103. Further, the heater 40 supplies the unreacted portion and the residue of the carbide supplied from the water gas supply path 102 to the char recovery device 41.
The cooler 40 adjusts the amount of water spray adjusted by the pyrolysis furnace 30 so as to be 650 ° C. or higher and 750 ° C. or lower, and to 220 ° C. or higher and 280 ° C. or lower.

The char recovery device 41 is a device that recovers the unreacted portion of carbide and supplies it to the pyrolysis furnace 30 again.
By providing the char recovery device 41, it is possible to prevent unreacted carbides from being discarded without being used for producing water gas. Therefore, by providing the char recovery device 41, the yield of the water gas from the carbide is improved.

In FIG. 1, the unreacted carbide recovered by the char recovery device 41 is supplied to the pyrolysis furnace 30 again, but the unreacted carbide recovered by the char recovery device 41 is supplied to the pyrolysis furnace 30. It may not be supplied to. In this case, the carbide itself recovered by the char recovery device 41 can be obtained as a product of the water gas generation system 100.
The unreacted carbide recovered by the char recovery apparatus 41 is washed with superheated steam (steam) inside the pyrolysis furnace 30 to remove components other than the carbon component. Therefore, in the char recovery device 41, it is possible to obtain a carbide having an extremely high carbon content in which components other than the carbon component are satisfactorily removed.

The cyclone 50 is an apparatus for removing carbides and residues contained in the water gas supplied through the water gas supply path 103. The cyclone 50 centrifuges the carbides and the residue contained in the water gas by internally swirling the water gas supplied through the water gas supply path 103, guides it downward, and supplies it to the residue recovery device 51. Further, the cyclone 50 guides the water gas from which carbides and residues have been removed upward and supplies it to the water gas cooling device 60 via the water gas supply path 104. The carbides recovered by the residue recovery device 51 are manufactured by the water gas generation system 100.

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 water which is a liquid. The water gas cooling device 60 collects the cooling water sprayed in the water gas and circulates the cooling water so as to be sprayed into the water gas again 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) that detects 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 gas adjusted by the heater 40 so as to be 220 ° C. or higher and 280 ° C. or lower, and 30 ° C. or higher and 50 ° C. or lower.

The water-based gas holder 70 is a device for storing the water-based gas supplied from the water-based gas cooling device 60. The water-based gas holder 70 can individually supply the stored water-based gas to each of the flare stack 71, the power generation facility 72, and the hydrogen purification device 73.

The flare stack 71 is a device for incineration when a surplus of water gas is generated, such as when the storage amount of the water gas holder 70 is excessive. The flare stack 71 is constantly burned by a fuel such as liquefied natural gas. Therefore, when the water gas is supplied to the flare stack 71, the water gas is incinerated.

The power generation facility 72 is a facility that operates a water gas as fuel to drive a generator and obtain a power generation output. As a 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.

The hydrogen purification device 73 is a device for purifying 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 gas contained in the water gas. is there. The hydrogen purification apparatus 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). Supply to (not shown). The hydrogen purification apparatus 73 opens and closes a valve (not shown) for controlling conduction with the outside air provided in the adsorption tower to reduce the pressure to atmospheric pressure, thereby converting the adsorbent to carbon dioxide gas. , Carbon dioxide gas and other components are removed to purify high-purity hydrogen gas.

The steam generator 80 is a device that vaporizes water to generate saturated steam by heating it 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. Further, the combustion gas used as a heat source for vaporizing water in the steam generator 80 is supplied to the dryer 10 via 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 saturated steam with combustion gas. Saturated steam generated by the steam generator 80 is supplied to the steam superheater 81. Further, the combustion gas discharged from the pyrolysis furnace 30 is supplied to the steam superheater 81 via 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 higher and 920 ° C. or lower.
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 water gas generation system 100. The control device 90 can communicate with a control unit (not shown) included in each unit constituting the water gas generation system 100. The control device 90 can control each unit by transmitting a control command to the control unit included in each unit constituting the water gas generation system 100. Further, the control device 90 can receive signals indicating the states of each part such as temperature and pressure from each part constituting the water gas generation system 100.
The control device 90 can make each unit constituting the water gas generation system 100 execute a desired operation by reading and executing the control program stored in the storage unit (not shown).

In the water gas generation system 100 shown in FIG. 1, the combustion gas generated in the carbonization furnace 20 is circulated as follows by the combustion gas flow path including the combustion gas flow paths 200a, 200b, 200c, 200d, 200e.
First, the combustion gas generated by the carbonization furnace 20 is supplied to the pyrolysis 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 by the combustion gas flow path 200b.
Third, the combustion gas discharged from the steam superheater 81 is supplied to the steam generator 80 by the combustion gas flow path 200c.
Fourth, the combustion gas discharged from the steam generator 80 is supplied to the dryer 10 by the combustion gas flow path 200d.
Fifth, the combustion gas discharged from the dryer 10 is supplied to the exhaust gas cooling / cleaning device 13 by the combustion gas flow path 200e.
Sixth, the combustion gas detoxified by the exhaust gas cooling / cleaning device 13 is discharged into the atmosphere by the exhaust gas cooling / cleaning device 13.

Here, the combustion gas generated by the carbonization furnace 20 is supplied to the pyrolysis furnace 30 without exchanging heat with another heat medium by using the pyrolysis gas maintained in a high temperature state. This is to promote the thermal decomposition reaction in No. 30 and improve the yield of water gas from carbonized products. Compared with the case where the combustion gas generated by the carbonization furnace 20 is heat-exchanged with another heat medium and then supplied to the pyrolysis furnace 30, the inside of the pyrolysis furnace 30 can be maintained at a high temperature, so that the pyrolysis can be carried out. The reaction is promoted and the yield of water gas from the carbonized material is improved.

Next, the carbonization furnace 20 of the present embodiment will be described in detail.
FIG. 2 is a vertical sectional view of the carbonization furnace 20 shown in FIG. In FIG. 2, the 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. 2, the carbonization furnace 20 of the present embodiment has a main body portion 21, a cylindrical portion 22, an organic waste input portion 23, a carbide discharge portion 24, a primary air supply portion 25, and a secondary portion. Air supply unit 26, combustion gas discharge unit 27, temperature sensor 28a, temperature sensor 28b (first temperature detection unit), temperature sensor 28c (second temperature detection unit), level sensor 28d (deposit 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 serves as an exterior of the carbonization furnace 20. The main body 21 forms a primary combustion region R2 for partially combusting organic waste and a secondary combustion region R4 for combusting combustible gas contained in the combustion gas generated from the organic waste. There is.
The main body 21 is attached to a metal (for example, iron) housing 21a forming the exterior of the carbonization furnace 20, a heat insulating material 21b attached to the inner peripheral surface of the housing 21a, and an inner peripheral surface of the heat insulating material 21b. It has a 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 the inner peripheral surface 21d for burning organic waste to generate carbides. Since the cylindrical portion 22 becomes hot due to combustion of organic waste, it is preferably formed of a heat-resistant material (for example, a metal material such as stainless steel).
As shown in FIG. 2, the inside of the cylindrical portion 22 is a hollow closed space, and this closed space is in a state of not communicating with other spaces. Therefore, the cylindrical portion 22 can store a certain amount of heat and is less susceptible to external temperature changes.

The cylindrical portion 22 is attached to the turntable 24a shown in FIG. 3, and rotates around the axis X as the turntable 24a rotates about the axis X. By rotating the cylindrical portion 22 around the axis X, the gap 20a and the organic waste existing above the gap 20a are guided from above to below along the gap 20a.

The organic waste supplied to the gap 20a is partially burned by the primary combustion air supplied from the primary air supply unit 25 in the primary combustion region R2, and is burned containing a solid content containing a large amount of carbide and a flammable gas. Gas is produced. 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 in which the upper part is blocked with organic waste and the primary combustion air is not supplied from the primary air supply unit 25. Therefore, the carbide is refined while being cooled in the carbide refining / cooling region R1.

The organic waste charging section 23 is provided in the main body section 21 and is provided in the main body section 21 and into an opening and an opening for throwing organic waste (not shown) supplied from the hopper 12 through the raw material supply path 12a into the main body section 21. It is provided with a transport unit (not shown) for transporting organic waste. An inclined surface 23a that inclines downward from above is formed below the organic waste input portion 23 as it approaches the axis X. The amount of organic waste charged into the opening by the organic waste charging unit 23 is adjusted by the control device 90 controlling the transport speed of the transport unit. The organic waste supplied from the organic waste input unit 23 is guided to the upper surface 22b and the gap 20a of the cylindrical portion 22 along the inclined surface 23a.

As shown in FIG. 2, the region where the organic waste input unit 23 is arranged is the raw material input region R3. In the raw material input region R3, an inspection window 20b is provided on the side opposite to the organic waste input 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 the carbides produced by the partial combustion of the organic waste in the gap 20a 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 FIGS. 2 and 3, the carbide discharge unit 24 has a turntable 24a (rotating body), a drive unit 24b, and a carbide discharge port 24c.

As shown in FIG. 3, the turntable 24a is a member provided at a position facing the lower end of the gap 20a in the axis X direction, and is an annular rotating body extending in the circumferential direction around the axis X. The turntable 24a rotates about the axis X by the driving force transmitted from the driving unit 24b.
As shown in FIG. 3, the surface of the turntable 24a facing the lower end of the gap 20a is an inclined surface that inclines downward as the distance from the axis X increases. Therefore, a gap is formed between the lower end of the gap 20a and the inclined surface of the turntable 24a.

The 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 rotation speed of the turntable 24a increases, the amount of carbide discharged from the lower end of the gap 20a to the carbide discharge port 24c increases. Similarly, as the rotation speed of the turntable 24a decreases, the amount of carbide discharged from the lower end of the gap 20a to the carbide discharge port 24c decreases.

The drive unit 24b is a device that transmits a driving force to the turntable 24a and rotates the turntable 24a around the axis X. As shown in FIG. 2, 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 torque while decelerating the rotational speed of 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, as the drive shaft 24h rotates around the axis X, the turntable 24a rotates around the axis X.

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

The clinker crusher 24d is a member for crushing a clinker, which is a mass larger than the gap formed between the lower end of the gap 20a and the inclined surface of the turntable 24a. Here, the clinker is a mass of combustion ash produced by burning organic waste in the primary combustion region R2.

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

Next, the primary air supply unit 25 will be described.
The primary air supply unit 25 is a device that supplies air for primary combustion that partially burns the organic waste toward the organic waste deposited in the gap 20a. As shown in FIG. 2, the primary air supply unit 25 has a primary combustion fan 25a (blower 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 has an inverter motor (not shown) and a fan driven by the inverter motor (not shown). The primary combustion fan 25a can adjust the amount of air to be blown by controlling the rotation speed of the inverter motor.

The cover portion 25b is a member that forms a closed space 25d in which the air blown from the primary combustion fan 25a is introduced and the air is supplied to the air supply port 25c.
As shown in FIG. 4A (the end view taken along the line AA of the carbonization furnace 20 shown in FIG. 2), the cover portion 25b is a closed space extending around the axis X between the cover portion 25b and the outer peripheral surface 21e of the main body portion 21. Form 25d.

The air supply port 25c is a flow path for supplying the air blown from the primary combustion fan 25a to the closed space 25d from the closed space 25d to the primary combustion region R2 inside the main body 21.
As shown in FIG. 2, 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 in which the organic waste is partially burned by the primary combustion air.

Further, as shown in FIG. 4A, 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. 4A). Further, as shown in FIG. 4A, 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. 4A, 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.) are used. Alternatively, they may be arranged at arbitrary intervals instead of being evenly spaced.

The primary air supply unit 25 shown in FIG. 2 has a heating unit (not shown) that heats 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, the ambient temperature of the primary combustion region R2 can be maintained at a high temperature as compared with the case where the air blown from the primary combustion fan 25a is not heated.

Next, the secondary air supply unit 26 will be described.
The secondary air supply unit 26 is a device that supplies the secondary combustion air for burning the flammable gas contained in the combustion gas generated by the combustion of organic waste in the primary combustion region R2 to the inside of the main body 21. is there. As shown in FIG. 2, the secondary air supply unit 26 is provided in the secondary combustion region R4, and supplies the secondary combustion air toward the secondary combustion region R4. The secondary air supply unit 26 has 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 has an inverter motor (not shown) and a fan driven by the inverter motor (not shown). The secondary combustion fan 26a can adjust the amount of air to be blown by controlling the rotation speed of the inverter motor.

The cover portion 26b is a member that forms a closed space 26d in which the air blown from the secondary combustion fan 26a is introduced and the air is supplied to the air supply port 26c.
As shown in FIG. 4B (the end view of the carbonization furnace 20 shown in FIG. 2 as seen by the arrow BB), the cover portion 26b is a closed space extending around the axis X between the cover portion 26b and the outer peripheral surface 21e of the main body portion 21. Form 26d.

The air supply port 26c is a flow path for supplying the air blown from the secondary combustion fan 26a to the closed space 26d from the closed space 26d to the secondary combustion region R4 inside the main body 21.
As shown in FIG. 2, air supply ports 26c are provided at a plurality of vertical directions along the axis X in the secondary combustion region R4 in which the flammable gas contained in the combustion gas is burned by the secondary combustion air. ing.

Further, as shown in FIG. 4 (b), the air supply ports 26c are provided in the main body 21 at equal intervals (30 ° intervals in FIG. 4 (b)) along the circumferential direction around the axis X. Further, as shown in FIG. 4B, the air supply port 26c 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. 4B, 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.) are used. Alternatively, they may be arranged at arbitrary intervals instead of being evenly spaced.

The combustion gas discharge unit 27 is a discharge port for discharging the combustion gas generated in the primary combustion region R2 and burning the combustible gas component in the secondary combustion region R4 to the combustion gas flow path 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 28a is a sensor that detects the temperature of the combustion gas discharged from the combustion gas discharge unit 27. The temperature sensor 28a transmits a temperature detection signal indicating the detected temperature to the carbonization furnace control unit 29.
As shown in FIG. 2, the temperature sensor 28a is arranged in a region of the secondary combustion region R4 close to the combustion gas flow path 200a. Therefore, the combustion gas temperature Tg detected by the temperature sensor 28a is a temperature substantially equal to 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 28b 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 the carbide temperature Tc, which is the temperature of the carbides deposited on the lower end side of the gap 20a. The temperature sensor 28b 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 accumulated amount of organic waste existing in the Y direction of the axis shown in FIG. 1 in the primary combustion region R2 by obtaining an output signal corresponding to the accumulated amount.
The level sensor 28d may be a reflection type sensor that detects the amount of deposit by receiving the reflection of emitted light, ultrasonic waves, or the like. Further, the level sensor 28d may be a transmission type sensor in which a receiving unit for receiving emitted X-rays or the like is provided in the cylindrical portion 22.

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

The ignition burner 20c is a device used to ignite the organic waste when starting the combustion of the organic waste in the carbonization furnace 20. As shown in FIG. 2, the ignition burner 20c is provided on the lower end side of the gap 20a. Further, as shown in FIG. 2, the ignition burners 20c 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 an ignition fuel such as kerosene. The ignition burner 20c generates a flame when the combustion of organic waste in the carbonization furnace 20 is started by a control command from the carbonization furnace control unit 29. Further, the ignition burner 20c stops the generation of flame at a predetermined timing by a control command from the carbonization furnace control unit 29.

The carbonization furnace control unit 29 is a device that controls each unit by receiving detection signals indicating the state of each unit from each unit included in the carbonization furnace 20 and transmitting a control signal to each unit based on the detection signal. Further, 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 the 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 an accumulation amount detection signal indicating the accumulation 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 amount of air blown by the primary combustion fan 25a to the primary air supply unit 25. Further, the carbonization furnace control unit 29 transmits a control signal for controlling the amount of air blown by the secondary combustion fan 26a to the secondary air supply unit 26. Further, the carbonization furnace control unit 29 transmits a control signal to the ignition burner 20c to generate a flame when starting combustion of organic waste, and also transmits a control signal at a predetermined timing to stop the generation of the flame. .. Further, 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 of controlling the amount of air blown by the primary combustion fan 25a 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 primary combustion fan 25a based on the ambient temperature of the primary combustion region R2 detected by the temperature sensor 28b. The amount of air blown by the primary combustion fan 25a is the same as the amount of air for primary combustion 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 air for primary combustion 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 ambient temperature of the primary combustion region R2 detected by the temperature sensor 28b so that a combustion state suitable for carbonizing the organic waste deposited 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 falls within the range of 900 ° C. or higher and 1200 ° C. or lower.

In the carbonization furnace 20 of the present embodiment, the carbonization furnace control unit 29 controls the amount of air blown by the primary combustion fan 25a so that the atmospheric temperature Ta of the primary combustion region R2 falls within the range of 900 ° C. or higher and 1200 ° C. or lower. As a result, the carbonized state of the organic matter is controlled so that the organic waste deposited on the upper layer side of the carbonized material refining / cooling region R1 is maintained in a temperature range (predetermined temperature range) of 900 ° C. or higher and 1200 ° C. or lower. In the following, 900 ° C., which is the lower limit of the atmospheric temperature Ta of the primary combustion region R2 controlled by the carbonization furnace control unit 29, is set as the first atmospheric temperature Ta1, and 1200 ° C., which is the upper limit of the atmospheric temperature Ta of the primary combustion region R2. Is the second atmospheric temperature Ta2.
Each process in the flowchart shown in FIG. 5 is a process performed by the arithmetic unit (not shown) included in the carbonization furnace control unit 29 executing a control program stored in the storage unit (not shown).

Prior to the process shown in the flowchart of FIG. 5, when the carbonization furnace control unit 29 starts the combustion of the organic waste in the carbonization furnace 20, the ignition burner 20c generates a flame and the organic waste is deposited in the gap 20a. Start burning. The carbonization furnace control unit 29 then starts blowing external air (atmosphere) by the primary combustion fan 25a. The carbonization furnace control unit 29 controls the primary combustion fan 25a so that the amount of air blown is constant until the atmospheric temperature Ta of the primary combustion region R2 detected by the temperature sensor 28b becomes equal to or higher than the first atmospheric temperature Ta1. After the atmospheric temperature Ta detected by the temperature sensor 28b becomes equal to or higher than the first atmospheric temperature Ta1, each process shown in the flowchart of FIG. 5 is started.

The amount of air for primary combustion blown by the primary combustion fan 25a until the atmospheric temperature Ta becomes equal to or higher than the first atmospheric temperature Ta1 completely burns the organic waste charged into the primary combustion region R2. It is the amount obtained by subtracting a certain amount from the amount required for. This is to prevent the carbon yield (the ratio of the weight of the input organic waste to the weight of the carbon component contained in the obtained carbide) to decrease due to excessive combustion of the organic waste. is there.

In step S500, the carbonization furnace control unit 29 detects the atmospheric temperature Ta in the primary combustion region R2 by receiving the temperature detection signal transmitted from the temperature sensor 28b.
In step S501, the carbonization furnace control unit 29 determines whether or not the atmospheric temperature Ta detected by the temperature sensor 28b is lower than the first atmospheric temperature Ta1. If the carbonization furnace control unit 29 determines that the atmospheric temperature Ta is lower than the first atmospheric temperature Ta1, the process proceeds to step 502, and if not, the process proceeds to step S503.

In step S502, the carbonization furnace control unit 29 transmits a control signal for increasing the amount of air blown by the primary combustion fan 25a to the primary combustion fan 25a. The primary combustion fan 25a increases the amount of air blown in response to receiving a control signal from the carbonization furnace control unit 29. The carbonization furnace control unit 29 increases the amount of oxygen for burning organic waste by increasing the amount of air blown by the primary combustion fan 25a, thereby raising the atmospheric temperature Ta.

In step S503, the carbonization furnace control unit 29 determines whether or not the atmospheric temperature Ta detected by the temperature sensor 28b is higher than the second atmospheric temperature Ta2. If the carbonization furnace control unit 29 determines that the detected atmospheric temperature Ta is higher than the second atmospheric temperature Ta2, the process proceeds to step S504, and if not, the process proceeds to step S501.

In step S504, the carbonization furnace control unit 29 transmits a control signal for reducing the amount of air blown by the primary combustion fan 25a to the primary combustion fan 25a. The primary combustion fan 25a reduces the amount of air blown in response to receiving a control signal from the carbonization furnace control unit 29. The carbonization furnace control unit 29 reduces the amount of air blown by the primary combustion fan 25a to reduce the amount of oxygen in the candy that burns organic waste and lowers the atmospheric temperature Ta.
When the carbonization furnace control unit 29 finishes the process of the flowchart shown in FIG. 5, the carbonization furnace control unit 29 starts executing the process shown in FIG. 5 again.

In this way, the carbonization furnace control unit 29 primary so that the atmospheric temperature Ta of the primary combustion region R2 falls within the range of the first atmospheric temperature Ta1 (900 ° C.) or higher and the second atmospheric temperature Ta2 (1200 ° C.) or lower. The amount of air blown by the combustion fan 25a is controlled. As a result, the carbonization furnace control unit 29 carbonizes the organic matter so that the organic waste deposited on the upper layer side of the carbide refining / cooling region R1 is maintained in the temperature range (predetermined temperature range) of 900 ° C. or higher and 1200 ° C. or lower. Control the state.

The carbonization furnace control unit 29 of the present embodiment repeatedly executes the process shown in FIG. 5 with a control cycle of 3 seconds so that the difference in atmospheric temperature Ta detected in the continuous control cycle does not exceed 25 ° C. Can be controlled. In the water gas generation system 100 of the present embodiment, the atmospheric temperature Ta is automatically controlled by the carbonization furnace control unit 29, so that the organic waste deposited in the gap 20a is in a temperature range of 900 ° C. or higher and 1200 ° C. or lower (predetermined). It can be maintained in the temperature range).

Next, a method of controlling the amount of air blown by 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 coincides with the amount of air for secondary combustion supplied from the air supply port 26c to the secondary combustion region R4 of the carbonization furnace 20. Therefore, the carbonization furnace control unit 29 can adjust the amount of air for secondary combustion blown to the secondary combustion region R4 by controlling the amount of air blown by the secondary combustion fan 26a. ..

The carbonization furnace control unit 29 is based on the combustion gas temperature Tg detected by the temperature sensor 28a so that a 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. 6 is a process performed by the arithmetic unit (not shown) included in the carbonization furnace control unit 29 executing a control program stored in the storage unit (not shown).

Prior to the process shown in the flowchart of FIG. 6, when the carbonization furnace control unit 29 starts the combustion of the organic waste in the carbonization furnace 20, the ignition burner 20c generates a flame and the organic waste is deposited in the gap 20a. Start burning. The carbonization furnace control unit 29 then 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 amount of air blown 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 reaches the first combustion gas temperature Tg1 or higher, each process shown in the flowchart of FIG. 6 is started.

The amount of air for secondary combustion 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 a flammable gas that is assumed to exist in the secondary combustion region R4. It is the amount required to completely burn the gas plus a certain surplus amount.

In step S600, the carbonization furnace control unit 29 detects the combustion gas temperature Tg, which is the temperature of the combustion gas discharged from the combustion gas discharge unit 27, by receiving the temperature detection signal transmitted from the temperature sensor 28a.

In step S601, 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. If the carbonization furnace control unit 29 determines that the combustion gas temperature Tg is lower than the first combustion gas temperature Tg1, the process proceeds to step S602, and if not, the process proceeds to step S603.

In step S602, the carbonization furnace control unit 29 transmits a control signal for reducing the amount of air blown by the secondary combustion fan 26a to the secondary combustion fan 26a. The secondary combustion fan 26a reduces the amount of air blown in response to receiving a 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 amount of air blown by the secondary combustion fan 26a is reduced 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 certain amount more than the amount of completely combusting the flammable gas contained in the combustion gas existing in the secondary combustion region R4. It is preferable to use a large amount. That is, it is preferable that the excess air ratio in the secondary combustion region R4 is a constant value larger than 1.0.

However, the amount of flammable gas existing in the secondary combustion region R4 generally fluctuates 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 by the secondary air supply unit 26 to the secondary combustion region R4 remains constant, it is not possible to maintain an amount of air suitable for completely combusting the flammable gas.

When the amount of secondary combustion air is excessively large with respect to the amount of complete combustion of the combustible gas, a large amount of excess air not used for combustion of 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 of the secondary combustion region R4, the atmospheric temperature of 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 deteriorates, and the combustion gas containing a large amount of the combustible gas is discharged from the combustion gas discharge unit 27. The flammable gas contains high molecular weight hydrocarbons, which are components that solidify into tar. Therefore, if the flammable gas still contains a large amount of components that solidify into tar, the carbonization furnace 20 and the equipment installed on the downstream side thereof may be damaged. Therefore, it is desirable to prevent the combustion gas from containing a large amount of components that solidify into tar, and to suppress damage to the carbonization furnace 20 and the equipment installed on the downstream side thereof.
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 excess air supplied to the secondary combustion region R4. The amount of air blown by the fan 26a is reduced.

In step S603, 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. If the carbonization furnace control unit 29 determines that the detected combustion gas temperature Tg is higher than the second combustion gas temperature Tg2, the process proceeds to step S604, and if not, the process proceeds to step S601.

In step S604, the carbonization furnace control unit 29 transmits a control signal for increasing the amount of air blown by the secondary combustion fan 26a to the secondary combustion fan 26a. The secondary combustion fan 26a increases the amount of air blown in response to receiving the control signal from the carbonization furnace control unit 29.
When the carbonization furnace control unit 29 finishes the process of the flowchart shown in FIG. 6, the carbonization furnace control unit 29 starts executing the process shown in FIG. 6 again.
Here, when it is determined that the combustion gas temperature Tg is higher than the second combustion gas temperature Tg2, the amount of air blown by the secondary combustion fan 26a is increased for the following reason.

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

Therefore, the carbonization furnace control unit 29 increases the amount of air blown by 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 excess air is supplied to the secondary combustion region R4 by increasing the amount of air blown by the secondary combustion fan 26a, the atmospheric temperature of 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 is first. The combustion gas temperature is Tg1 or more and the second combustion gas temperature is Tg2 or less.
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 high molecular weight hydrocarbons can be removed from the combustion gas by maintaining the temperature of the secondary combustion region R4 at 900 ° C. or higher. .. High molecular weight hydrocarbon is a component of combustible gas contained in combustion gas that solidifies into tar. Therefore, by removing most of the high molecular weight hydrocarbon from the combustion gas, it is possible to suppress damage to the carbonization furnace 20 and the equipment installed on the downstream side thereof.

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 reduces the amount of air blown when the combustion gas temperature Tg is lower than the first combustion gas temperature Tg1, and increases the amount of air blown 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 the combustion.

Next, a method of controlling the rotation 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. 7 is a process performed by the arithmetic unit (not shown) included in the carbonization furnace control unit 29 executing a control program stored in the storage unit (not shown).

In the flowchart shown in FIG. 7, the carbide furnace control unit 29 controls the amount of 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 so that the organic waste input from the organic waste input unit 23 is deposited in the gap 20a over a predetermined time. This is because the components other than the carbon component contained in the organic waste are sufficiently removed by thermal decomposition by heating or the like. If the time for the organic waste to be deposited in the gap 20a is short, the components other than the carbon component cannot be sufficiently removed, and the obtained carbide content is lowered.

Further, if the organic waste is deposited in the gap 20a for a long time, a part of the carbon component is completely burned, and the carbon yield of the carbide obtained from the organic waste as a raw material is lowered. The predetermined time for depositing the organic waste in the gap 20a varies depending on the type and condition of the organic waste, the environmental temperature of the carbonization furnace 20, and the like, but is, for example, an arbitrary time of 30 minutes or more and 50 minutes or less. Is preferable. More preferably, it is an arbitrary time of 35 minutes or more and 45 minutes or less.
Further, the amount of carbide discharged by the carbide discharge unit 24 is controlled by the carbide discharge unit 24 as the charge of organic waste from the organic waste input unit 23 into the gap 20a is stopped. This is to prevent the temperature of the discharged carbide from rising.

As the amount of organic waste deposited in the gap 20a gradually decreases, the carbide refining / cooling region R1 that extinguishes the carbide gradually narrows. In this case, if the rotation speed of the turntable 24a is kept constant, the carbides are discharged from the lower end of the gap 20a in a state where they are not sufficiently cooled. This is because the carbides that are carbonized in the primary combustion region R2 and become hot are not sufficiently cooled in the carbide refining / cooling region R1.
Therefore, the carbide 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 carbide furnace control unit 29 adjusts the temperature of the carbide discharged by the carbide discharge unit 24 by using both the temperature sensor 28c and the level sensor 28d. The former is a sensor that directly detects the temperature of carbides, and the latter is a sensor that indirectly detects a state in which the temperature of carbides becomes high from the amount of accumulated carbides.
Hereinafter, each step of the flowchart of FIG. 7 will be described.

In step S700, the carbide furnace control unit 29 detects the carbide temperature Tc, which is the temperature of the carbide deposited on the lower end side of the gap 20a, by receiving the temperature detection signal transmitted from the temperature sensor 28c.
In step S701, the carbonization furnace control unit 29 detects the accumulated amount Ao, which is the accumulated amount of the organic waste accumulated in the gap 20a, by receiving the accumulated amount detection signal transmitted from the level sensor 28d.

In step S702, the carbide furnace control unit 29 determines whether or not the carbide temperature Tc detected by the temperature sensor 28c is equal to or higher than the first carbide temperature Tc1. If the carbonization furnace control unit 29 determines that the detected carbide temperature Tc is equal to or higher than the first carbide temperature Tc1, the process proceeds to step S703, and if not, the process proceeds to step S704.
Here, as the first carbide temperature Tc1, for example, any temperature in the range of 250 ° C. or higher and 300 ° C. or lower can be set.

In step S703, the carbonization furnace control unit 29 controls the drive unit 24b so that the rotation speed of the turntable 24a is rotated by 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 at which the carbide furnace 20 discharges an amount of carbide required for maintaining the normal operating state from the carbide discharge unit 24. In step S703, the rotation speed of the turntable 24a is first 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 becomes the first carbide temperature Tc1 or higher. The second rotation speed Rs2 is lower than the rotation speed Rs1. By lowering the rotation speed of the turntable 24a, the time for the carbide to stay in the carbide refining / cooling region R1 becomes longer, and the temperature of the carbide discharged by the carbide discharge unit 24 decreases accordingly.

In step S704, the carbonization furnace control unit 29 determines whether or not the accumulated amount Ao detected by the level sensor 28d is equal to or less than the first accumulated amount Ao1. If the carbonization furnace control unit 29 determines that the detected accumulated amount Ao is equal to or less than the first accumulated amount Ao1, the process proceeds to step S705, and if not, the process proceeds to step S706.

In step S705, the carbonization furnace control unit 29 controls the drive unit 24b so that the rotation speed of the turntable 24a is rotated at the second rotation speed Rs2. The second rotation speed Rs2 is lower than the first rotation speed Rs1 described later. In step S705, the rotation speed of the turntable 24a is first set so that the temperature of the carbide discharged by the carbide discharge unit 24 decreases when the deposit amount Ao detected by the level sensor 28d becomes the first deposit amount Ao1 or less. The second rotation speed Rs2 is lower than the rotation speed Rs1.

In step S706, the carbonization furnace control unit 29 controls the drive unit 24b so that the rotation speed of the turntable 24a is rotated at the first rotation speed Rs1. As described above, the first rotation speed Rs1 is a speed at which the carbide furnace 20 discharges an amount of carbide required for maintaining the normal operating state from the carbide discharge unit 24. In step S906, the carbide furnace control unit 29 has an amount required to maintain the operating state because the carbide temperature Tc is lower than the first carbide temperature Tc1 and the accumulated amount Ao is larger than the first accumulated amount Ao1. The drive unit 24b is controlled so that the carbide is discharged from the carbide discharge unit 24.

When the carbonization furnace control unit 29 finishes the process of the flowchart shown in FIG. 7, the carbonization furnace control unit 29 starts executing the process shown in FIG. 7 again. In this way, in the carbonization furnace control unit 29, the rotation speed at which the drive unit 24b rotates the turntable 24a based on the carbide temperature Tc detected by the temperature sensor 28c and the accumulated amount of organic waste Ao detected by the level sensor 28d. To control.

In the flowchart shown in FIG. 7 above, the rotation speed of the turntable 24a is switched in 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 aspects may be used.
For example, the rotation speed of the turntable 24a may be switched in a plurality of steps of two or more steps according to the carbide temperature Tc. Further, for example, the rotation speed of the turntable 24a may be controlled so as to be inversely proportional to the carbide temperature Tc detected by the temperature sensor 28c without gradually switching the rotation speed of the turntable 24a.

Further, in the flowchart shown in FIG. 7, the rotation speed of the turntable 24a is switched in two stages depending on whether or not the deposit amount Ao detected by the level sensor 28d is equal to or higher than the first deposit amount Ao1. However, other aspects may be used.
For example, the rotation speed of the turntable 24a may be switched in a plurality of stages of two or more stages according to the amount of deposit Ao. Further, for example, the rotation speed of the turntable 24a may be controlled so as to be proportional to the deposit amount Ao detected by the level sensor 28d without switching the rotation speed of the turntable 24a stepwise.

Further, in the flowchart shown in FIG. 7, the rotation speed of the turntable 24a is controlled by using both the carbide temperature Tc detected by the temperature sensor 28c and the deposition amount Ao detected by the level sensor 28d. Other aspects may be used.
For example, the rotation speed of the turntable 24a may be controlled by using either the carbide temperature Tc detected by the temperature sensor 28c or the deposition amount Ao detected by the level sensor 28d.

As described above, in the carbonization furnace control unit 29 of the present embodiment, the carbide temperature Tc detected by the temperature sensor 28c is lower than the first carbide temperature Tc1 (for example, an arbitrary temperature in the range of 250 ° C. or higher and 300 ° C.). The rotation speed of the turntable 24a is controlled.
As a result, organic waste deposited in the temperature range of 900 ° C. or higher and 1200 ° C. or lower on the upper layer side of the carbide scouring / cooling region R1 by controlling the air flow rate of the primary combustion fan 25a is deposited for a predetermined time (for example, 30 minutes or longer). And it is deposited in the gap 20a for 50 minutes or less), and then discharged from the carbide discharge part 24.
Further, the organic waste having a temperature lower than the first carbide temperature Tc1 at the position of the temperature sensor 28c is gradually cooled in the gap 20a below the temperature sensor 28c and is gradually cooled at room temperature (for example, 25 ° C.). Is discharged from.

The carbonization furnace control unit 29 of the present embodiment repeatedly executes the process shown in FIG. 7 with a control cycle of 3 seconds so that the difference in carbide temperature Tc detected in the continuous control cycle does not exceed 25 ° C. Can be controlled. In the water gas generation system 100 of the present embodiment, by automatically controlling the carbide temperature Tc by the carbonization furnace control unit 29, the gap 20a is formed over a time (predetermined time) of 30 minutes or more and 50 minutes or less for organic waste. Can be deposited in.

Next, the pyrolysis furnace 30 of the present embodiment will be described in detail.
FIG. 8 is a vertical cross-sectional view of the pyrolysis furnace 30 shown in FIG. In FIG. 8, the axis Z indicates a vertical direction (gravity direction) orthogonal to an installation surface (not shown) on which the pyrolysis furnace 30 is installed.

As shown in FIG. 8, the pyrolysis furnace 30 of the present embodiment includes a main body 31, a reaction tube 32, a reaction tube head 33 (supply section), a water gas outlet nozzle 34 (water gas outlet section), and the like. Combustion gas supply unit 35 (heating gas supply unit), combustion gas discharge unit 36 (heating gas discharge unit), gland packing 37 (first seal part), gland packing 38 (second seal part), It is provided with 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 inside.
The main body 31 is attached to a metal (for example, iron) housing 31a forming the exterior of the pyrolysis furnace 30, a heat insulating material 31b to be attached to the inner peripheral surface of the housing 31a, and an inner peripheral surface of the heat insulating material 31b. It has a heat-resistant material 31c to be used.

The upper surface of the substantially cylindrical main body 31 is formed of an annular top plate 31d in a plan view, and the bottom surface of the main body 31 is formed of an annular bottom plate 31e in a plan view.
Further, an upper end flange portion 31g (first flange portion) is provided at the upper end of the side surface 31f of the main body portion 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 portion 31. ing.

The upper plate 31d and the upper end flange portion 31g have 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 locations around the axis Z. ) Is concluded.
Similarly, the bottom plate 31e and the lower end flange 31i have a fastening bolt 31j (fastening member) with a gasket (fifth seal portion) (not shown) sandwiched between the bottom plate 31e and the lower end flange 31i at a plurality of locations around the axis Z. 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 32d that forms a combustion gas flow path 30a for flowing a combustion gas (heating gas) with 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). ) And.

As shown in FIG. 8, the upper end flange 32b of the reaction tube 32 and the end portion of the center pipe 32a on the upper end flange 32b side project upward from the upper plate 31d (upper surface) of the main body portion 31.
Further, the lower end portion 32c of the reaction tube 32 projects downward from the bottom plate 31e (bottom surface) of the main body portion 31.

The center pipe 32a is a member formed in a cylindrical shape extending along the axis Z. Inside the center pipe 32a, a thermal decomposition promoting 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) is housed.
The pyrolysis promoting mechanism promotes the pyrolysis reaction of the carbide and the superheated vapor (gasifying 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 inside the reaction tube 32. It is a mechanism to make it.

As shown in FIG. 8, the plurality of first inclined plates 32f and the plurality of second inclined plates 32g are held by four holding rods (not shown) at a plurality of locations along the axis Z. Further, the first inclined plate 32f and the second inclined plate 32g are alternately arranged along the axis Z.
The upper ends of the four holding rods are attached to the lower surface of the lower end flange 33a 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 promotion mechanism can be removed (attached / detached) upward from the center pipe 32a.

As shown in FIG. 8, the first inclined surface formed by the first inclined plate 32f is inclined so as to guide the carbides that have fallen from the second opening 32j downward, and the second inclined plate 32g is formed. The inclined surface is inclined so as to guide the carbides that have fallen from the first opening 32i downward.
As described above, the thermal decomposition promotion mechanism guides the carbide stepwise from the upper end side to the lower end side of the center pipe 32a by using the first inclined plate 32f and the second inclined plate 32g alternately arranged along the axis Z. be able to.

The angle of inclination 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 the carbide is ensured to move along the inclined surface. It is preferable that the angle is equal to or greater than the angle of repose of. On the other hand, if the inclination angle is made too large, the residence time of the carbide in the reaction tube 32 becomes short, 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 set to be equal to or more than the angle of repose of the carbide in the range of 20 ° or more and 60 ° or less.

The reaction tube head 33 is attached to the reaction tube 32 and supplies carbides and superheated steam (gasifying 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 path 101, and a flow path in which superheated steam is supplied from the steam superheater 81 (not shown). ) With a side flange 33c.

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 tubular member attached to the lower end 32c of the reaction tube 32. The water gas outlet nozzle 34 removes residues such as water gas, unreacted carbides, and ash generated by the thermal decomposition reaction of carbides inside the reaction tube 32 via the water gas supply path 102. Lead to.
The unreacted carbides led from the water gas outlet nozzle 34 to the heater 40 are washed with superheated steam (steam) to remove components other than the carbon component. Therefore, the carbide guided to the cooler 40 is a carbide having a high carbon content in which components other than the carbon component are satisfactorily removed.

The combustion gas supply unit 35 is an opening provided above the main body 31 and supplying the combustion gas guided from the combustion gas flow path 200a to the combustion gas flow path 30a.
The combustion gas discharge unit 36 is provided below the main body 31 and is an opening for discharging the combustion gas from the combustion gas flow path 30a to the combustion gas flow path 200b.
The combustion gas supplied from the combustion gas supply unit 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 unit 36. Will be done.

The gland packing 37 is a member that blocks the outflow of the combustion gas in the combustion gas flow path 30a from the upper plate 31d of the main body 31 to the outside. The gland packing 37 is a plan view annular member provided so as to be in contact with the lower surface of the upper plate 31d of the main body 31 and having an inner peripheral surface 37d in contact with the outer peripheral surface 32d of the reaction tube 32.

The gland packing 37 is configured with the ceramic board 37a, the ceramic board 37b, and the ceramic fiber 37c in close contact with each other. By using the ceramic fiber 37c, which is a fibrous material that can be deformed relatively easily, the sealing property at the portion in contact with the heat insulating material 31b and the heat insulating material 31c is improved.

The gland packing 38 is a member that blocks the outflow of combustion gas in the combustion gas flow path 30a from the bottom plate 31e of the main body 31 to the outside. The gland packing 38 is a plan view annular member provided so as to be in contact with the upper surface of the bottom plate 31e of the main body 31 and having an inner peripheral surface 38d in contact with the outer peripheral surface 32d of the reaction tube 32.

The gland packing 38 is configured with the ceramic board 38a, the ceramic board 38b, and the ceramic fiber 38c 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 property at the portion in contact with the heat insulating material 31b and the heat insulating material 31c is improved.
The gland packing 39 is a member that blocks the outflow of water gas from the mounting position at the mounting position of the lower end 32c of the reaction tube 32 and the water gas outlet nozzle 34.

Next, with reference to FIG. 9, the pyrolysis furnace 30, the heater 40, the cyclone 50, the steam generator 80, the steam superheater 81, and the peripheral devices of the present embodiment will be described in detail.
As shown in FIG. 9, 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 for transporting carbides discharged from the carbonization furnace 20. The screw conveyor 101a accommodates a screw inside a cylinder extending in a straight line. The screw conveyor 101a conveys carbides 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 clinker having a certain particle size or more from the carbide discharged from the screw conveyor 101a by 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 uses a magnet to remove iron debris such as nails contained in carbides. The carbide from which the iron debris has been removed is supplied to the screw conveyor 101e.

The screw conveyor 101e and the screw conveyor 101f are devices for transporting carbides, respectively. The screw conveyor 101f supplies carbides to the nitrogen substituent 30b of the pyrolysis furnace 30. Since the structures of the screw conveyor 101e and the screw conveyor 101f are the same as those of the screw conveyor 101a, the description thereof will be omitted.

The screw conveyor 101e and the screw conveyor 101f transport the carbides above the pyrolysis furnace 30 by supplying the carbides from above the pyrolysis furnace 30 and using the weight of the carbides in the reaction tube 32 of the pyrolysis furnace 30. This is to allow carbides to pass through. By passing the reaction tube 32 of the thermal decomposition furnace 30 by the 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 thermal decomposition reaction. Further, since the carbide is passed through the reaction tube 32 by the weight of the carbide, no special power is required to move the carbide.

In addition, transporting carbides in two stages of the screw conveyor 101e and the screw conveyor 101f requires an expensive motor with a large driving force by reducing the power required for each screw conveyor to rotate the screw. This is to prevent.

The nitrogen substituent 30b is an apparatus constituting the pyrolysis furnace 30, and is an apparatus for replacing oxygen contained in the air supplied from the screw conveyor 101f together with carbides with an inert nitrogen gas.
The nitrogen substitution device 30b is arranged in each of the upper part connected to the screw conveyor 101f and the lower part connected to the reaction tube head 33, and the open / closed state is controlled by the control device 90 (for example, a ball valve). ).

The control device 90 supplies carbides to the inside of the nitrogen substituent 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 substitution device 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 substitution device 30b. ..

Nitrogen gas is constantly supplied to the nitrogen substituent 30b from a device that generates nitrogen gas, such as an air separation device. Therefore, when a certain period of time elapses with the control valves above and below the nitrogen substitution device 30b closed, the air supplied to the inside of the nitrogen substitution device 30b together with the charcoal is discharged to the outside and the inside is replaced with nitrogen gas. It becomes a state.

After the inside of the nitrogen substitution device 30b is replaced with nitrogen gas, the control device 90 switches the control valve below the nitrogen substitution device 30b to the open state to carry carbides from the nitrogen substitution device 30b to the reaction tube head 33. Supply.
The control device 90 closes the control valve below the nitrogen substitution device 30b after supplying carbides from the nitrogen substitution device 30b to the reaction tube head 33. Further, the control device 90 subsequently opens the control valve above the nitrogen substitution device 30b and supplies new carbides to the inside of the nitrogen substitution device 30b.

The control device 90 uses nitrogen gas as the gas supplied together with the carbides to the reaction tube head 33 by controlling the opening and closing of the control valves above and below the nitrogen substituent 30b as described above. This nitrogen gas is an inert gas that does not react with the water gas produced in the reaction tube 32. Therefore, it is possible to prevent the air containing oxygen together with the carbides from being supplied to the reaction tube 32 and the oxygen and the water gas reacting with each other to reduce the yield of the water gas.

The char recovery device 41 has a nitrogen substituent 41a and a char recovery unit 41b.
The nitrogen substitution device 41a is a device for replacing the water gas supplied from the heater 40 together with the unreacted component of the carbide with the inert nitrogen gas.
The char recovery unit 41b is a device that recovers the unreacted portion of carbide and supplies it to the nitrogen substituent 30b from a supply path (not shown).
The nitrogen substitution device 41a is arranged in each of the upper part connected to the thermostat 40 and the lower part connected to the char recovery unit 41b, and the open / closed state is controlled by the control device 90 (for example, a ball). Has a valve).

The control device 90 supplies the unreacted portion of carbide to the inside of the nitrogen substituent 41a by opening the upper control valve and closing the lower control valve. When the unreacted amount of carbide supplied to the inside of the nitrogen substituent 41a reaches a certain amount, the control device 90 closes the control valve above the nitrogen substituent 41a.

Nitrogen gas is constantly supplied to the nitrogen substituent 41a from a device that generates nitrogen gas, such as an air separation device. Therefore, when a certain period of time elapses with the control valves above and below the nitrogen substitution device 41a closed, the water gas supplied to the inside of the nitrogen substitution device 41a is discharged to the outside together with the unreacted component of the carbide, and the inside is nitrogen. It will be in a state of being replaced with gas. The water gas discharged from the nitrogen substituent 41a is supplied to the flare stack 71.

After the inside of the nitrogen substitution device 41a is replaced with nitrogen gas, the control device 90 switches the control valve below the nitrogen substitution device 41a to the open state and from the nitrogen substitution device 41a to the char recovery unit 41b. Supply the unreacted portion of.
The control device 90 supplies the unreacted portion of carbide from the nitrogen substitution device 41a to the char recovery unit 41b, and then closes the control valve below the nitrogen substitution device 41a. Further, the control device 90 subsequently opens the control valve above the nitrogen substituent 41a and supplies an unreacted portion of new carbides to the inside of the nitrogen substituent 41a.

By controlling the opening and closing of the control valves above and below the nitrogen substituent 41a as described above, the control device 90 supplies the water gas supplied to the char recovery unit 41b together with the unreacted portion of the carbide to the char recovery unit 41b. It prevents it from being supplied.

The residue recovery device 51 includes a nitrogen substituent 51a and a residue recovery unit 51b.
The nitrogen substituent 51a is a device for replacing the water gas supplied from the cyclone 50 with the unreacted carbides and residues with the inert nitrogen gas.
The residue recovery unit 51b is a device for recovering unreacted carbides and residues discharged from the nitrogen substituent 51a.

The nitrogen substituent 51a is arranged in the upper part connected to the cyclone 50 and the lower part connected to the residue recovery unit 51b, respectively, and an electric control valve (for example, a ball valve) whose opening / closing state is controlled by the control device 90. Has. Nitrogen gas is constantly supplied to the nitrogen substituent 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 substitution device 51a in the same manner as controlling the control valve of the nitrogen substitution device 41a, and prevents the water gas from being supplied to the residue recovery unit 51b. .. The method in which the control device 90 controls the control valve of the nitrogen substitution device 51a is the same as the method in which the control device 90 controls the control valve of the nitrogen substitution device 41a, and thus the description thereof will be omitted.

The steam generator 80 has a steam generator 80a and a steam circulation tank 80b.
The steam generator 80a is provided on a heat transfer tube (not shown) for internally circulating water that exchanges heat with combustion gas, and a jacket (not shown) provided on a cylinder formed so as to cover the heat transfer tube and allowing water to flow inside. Omitted) and. Water is supplied to the heat transfer tube and the jacket from the steam circulation tank 80b, respectively.

The steam circulation tank 80b supplies water from the water supply device 82 and also supplies the water to the heat transfer tube and the jacket of the steam generator 80a. The hot water heated by the jacket and the steam generated by heating the heat transfer tube with the combustion gas are recovered in the steam circulation tank 80b, respectively.
The steam circulation tank 80b supplies steam (saturated steam) supplied from the heat transfer tube of the steam generator 80a to the steam superheater 81.

Next, the dryer 10 of the present embodiment will be described in detail with reference to FIG.
The dryer 10 is a type of dryer called a rotary kiln, and has 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 flow path 200d into the inside of the dryer 10 and guides the introduced combustion gas into the inside of 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 rotational power is applied by a drive motor.
Further, organic waste is supplied to the inside of 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 agitated 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 10a is supplied to the carbonization furnace 20 via the hopper 12.
Further, the discharge unit 10d supplies the combustion gas guided from the combustion gas introduction unit 10b through the inside of the rotating body 10c to the combustion gas flow path 200e. The combustion gas supplied to the combustion gas flow path 200e is supplied to the exhaust gas cooling / cleaning device 13.

Next, the properties of the carbide obtained in the carbonization furnace 20 of the present embodiment and the carbides obtained in the char recovery device 41 and the residue recovery device 51 will be described.
When the wood waste material containing 15% by weight of water was used as the organic waste supplied from the hopper 12, 15 to 25% by weight of carbonized material was obtained in the carbonization furnace 20 with respect to the organic waste. The water gas generation system 100 is continuously operated, and the carbides discharged from the carbide furnace 20 are collected about every 6 hours to obtain a total of 16 samples of carbides, which is an organic element analyzer (MT-5 manufactured by Yanako Analytical Industry Co., Ltd.). ) Was used for the analysis. As a result, the average value of the carbon content of the carbide was 91.5%, and the standard deviation was 1.5%. The measured specific surface area of the carbide with a specific surface area measuring device (Quantachrome Co. ^Nova-4200e), to give the results of 300m ² / g~400m 2 / g. In addition, when the ash content (components other than carbides) contained in the organic waste was analyzed with a fluorescent X-ray analyzer (PW2400 manufactured by Philips), it was found that about 52% by weight of Ca was contained in the total ash content. I got the result.

Further, when the wood waste material containing 15% by weight of water is used as the organic waste supplied from the hopper 12, the char recovery device 41 and the residue recovery device 51 are totaled to be about 2 with respect to the organic waste. Up to 3% by weight of unreacted carbide was obtained. The water gas generation system 100 is continuously operated, and the carbides discharged from the char recovery device 41 and the residue recovery device 51 are collected about every 6 hours to obtain a total of 16 samples of carbides, which are organic element analyzers (Yanako Analytical Industry Co., Ltd.). The analysis was performed with MT-5) manufactured by the company. As a result, the average value of the carbon content of the carbide was 92.1%, and the standard deviation was 1.4%. The measured specific surface area of the carbide with a specific surface area measuring device (Quantachrome Co. ^Nova-4200e), to give the results of 300m ² / g~400m 2 / g. In addition, when the ash content (components other than carbides) contained in the organic waste was analyzed with a fluorescent X-ray analyzer (PW2400 manufactured by Philips), it was found that about 52% by weight of Ca was contained in the total ash content. I got the result.

As described above, according to the water gas generation system 100 of the present embodiment, 15 to 25% by weight of carbide can be obtained with respect to the organic waste, and the carbon content of the carbide is about 92%. Therefore, according to the water gas generation system 100 of the present embodiment, in the carbide furnace 20, the char recovery device 41, and the residue recovery device 51, carbides can be obtained with a high carbon yield and the carbon content is extremely high. Can be obtained.

Further, according to the water gas generation system 100 of the present ^embodiment, it is possible to obtain a large carbide having a specific surface area of 300m ² / g~400m 2 / g. Carbides with a large specific surface area are useful as humidity control agents and adsorbents (activated carbon). FIG. 11 shows an image of the carbide obtained by the water gas generation system 100 of the present embodiment taken by a scanning electron microscope, and shows a structure having a large specific surface area. A scale is shown in the lower right of FIG. 11, and one scale is 100 μm.

It should be noted that the carbon content of the carbides obtained in the char recovery device 41 and the residue recovery device 51 (average value of 92.1%) is higher than the carbon content of the carbides obtained in the carbonization furnace 20 (91.5% on average). %) Is higher. This is because the carbides obtained in the char recovery device 41 and the residue recovery device 51 are washed with superheated steam (steam) in the pyrolysis furnace 30 to satisfactorily remove components other than the carbon component.
Further, the carbide produced by the water gas generation system 100 of the present embodiment can be effectively used for applications other than the above-mentioned humidity control agent and adsorbent. For example, it can be used as a soil conditioner, a charcoal filling agent, a snow melting agent, and an abrasive.

The actions and effects of the present embodiment described above will be described.
According to the water gas generation system 100 of the present embodiment, the organic waste input portion 23 organically disposes of the gap 20a formed between the inner peripheral surface of the main body 21 of the carbonization furnace 20 and the outer peripheral surface of the cylindrical portion 22. The material is charged, and in the normal operating state of the carbonization furnace 20, the organic waste charged from the organic waste charging unit 23 is deposited from below to above the gap 20a along the axis X. The organic waste on the upper layer side of the gap 20a is partially burned by the primary combustion air supplied from the primary air supply unit 25 and guided to the lower layer side of the gap 20a.

The organic waste on the lower layer side of the gap 20a is blocked by the organic waste on the upper layer side, and the lower layer side of the gap 20a is a carbide refining / cooling region R1 in which the solid content containing a large amount of carbon component is refined and cooled. In the carbide refining / cooling region R1, the solid content containing a large amount of carbon component is refined while being further carbonized in a state where the oxygen concentration is low, and the fire is gradually extinguished as it approaches the lower end of the gap 20a. As a result, the temperature of the carbide discharged from the lower end of the gap 20a can be lowered.

Further, according to the water gas generation system 100 of the present embodiment, the carbonization state of the organic waste is controlled so that the organic waste is maintained in a predetermined temperature range in the gap 20a. Therefore, there is a problem that the organic waste becomes high temperature and most of the carbon components are completely burned, and the organic waste becomes low temperature in the gap and other components other than the carbon component cannot be sufficiently removed. It can be suppressed. Here, the predetermined temperature range is, for example, preferably 900 ° C. or higher and 1200 ° C. or lower, and more preferably 1000 ° C. or higher and 1100 ° C. or lower.

Further, according to the water gas generation system 100 of the present embodiment, the organic waste is controlled to be deposited in the gap 20a over a predetermined time. Therefore, it is possible to suppress a problem that the time for the organic waste to be deposited in the gap 20a is shortened and the components other than the carbon component cannot be sufficiently removed from the organic waste. Here, the predetermined time is preferably in the range of, for example, 30 minutes or more and 50 minutes or less.
As described above, according to the water gas generation system 100 of the present embodiment, it is possible to produce a carbide in which the carbon component other than the carbon component is sufficiently removed while suppressing the decrease of the carbon component contained in the organic waste. it can.

The water gas generation system 100 of the present embodiment has a pyrolysis furnace 30 that generates an aqueous gas by thermally decomposing the carbides discharged from the carbide discharge unit 24 and superheated steam, and the carbides discharged from the thermal decomposition furnace 30. The char recovery device 41 and the residue recovery device 51 are provided.
By doing so, the carbide having a high carbon content and the superheated steam can be thermally decomposed in the thermal decomposition furnace 30 to generate an aqueous gas, and the unreacted carbide can be recovered. This unreacted carbide is washed with superheated steam to remove components other than the carbon component. Therefore, it is possible to obtain a carbide having a high carbon content in which components other than the carbon component are satisfactorily removed.

<Second Embodiment>
Next, the carbide production system 300 of the second embodiment of the present invention will be described with reference to the drawings.
The carbide production system 300 of the present embodiment is a modification of the water gas generation system 100 of the first embodiment. The carbide production system 300 of the present embodiment is the same as the water gas generation system 100 of the first embodiment unless otherwise specified below.

The water gas generation system 100 of the first embodiment generates water gas by thermally decomposing the carbides obtained in the carbonization furnace 20 with superheated steam in the thermal decomposition furnace 30, and produces water gas as a main product. As a by-product, carbides were produced.
On the other hand, the carbide production system 300 of the present embodiment does not have a pyrolysis furnace and produces carbide as a main product.

As shown in FIG. 12, the carbonized product manufacturing system 300 of the present embodiment includes a dryer 10, a hopper 11, a hopper 12, an exhaust gas cooling and cleaning device 13, a carbonizing furnace (carbonized product manufacturing device) 20, and a carbonizing furnace 20. The carbonized material recovery device 310 that recovers the carbonized material produced in the above, and the steam generator (heat exchange unit) 320 that generates steam by exchanging heat between the combustion gas discharged from the carbonization furnace 20 and water (heat medium). , A steam turbine 330 driven by steam generated by a steam generator 320, a power generation facility 340 that obtains power output from a generator connected to a turbine shaft (not shown) of the steam turbine 330, and each part of a carbonized product production system 300. A control device 350 for controlling the above.

The power generation facility 340 can supply electric power so that the obtained power generation output can be used in each part of the carbide manufacturing system 300. Further, the power generation facility 340 can also supply the power generation output that is surplus in the carbide manufacturing system 300 to the power system (not shown). The steam generated by the steam generator 320 and used as the rotational power of the turbine shaft of the steam turbine 330 is returned to the steam generator 320 as a heat medium after being restored by the condenser (not shown). To.

In the carbide manufacturing system 300 shown in FIG. 12, the combustion gas generated in the carbonization furnace 20 is circulated as follows by the combustion gas flow path including the combustion gas flow paths 300a, 300b, and 300c.
The combustion gas generated by the carbonization furnace 20 is supplied to the steam generator 320 by the combustion gas flow path 300a. The combustion gas discharged from the steam generator 320 is supplied to the dryer 10 by the combustion gas flow path 300b. The combustion gas discharged from the dryer 10 is supplied to the exhaust gas cooling / cleaning device 13 by the combustion gas flow path 300c. The combustion gas detoxified by the exhaust gas cooling / cleaning device 13 is discharged into the atmosphere by the exhaust gas cooling / cleaning device 13.

According to the carbide production system 300 of the present embodiment, since the entire amount of carbide produced in the carbide furnace 20 is recovered by the carbide recovery device 310, it is possible to obtain carbide having an extremely high carbon content as a main product.
Further, according to the carbonized product production system 300 of the present embodiment, steam is generated by exchanging heat of high temperature (for example, 1000 ° C. to 1200 ° C.) combustion gas generated in the carbonization furnace 20 with water to generate steam, and a steam turbine. The 330 can be operated and recovered as power for the power generation facility 340. Further, the relatively high temperature (for example, 500 ° C. to 600 ° C.) combustion gas that has passed through the steam generator 320 can be used for drying the organic waste in the dryer 10, and the heat of the combustion gas can be further effectively utilized.

[Other Embodiments]
The present invention is not limited to the above-described embodiment, and can be appropriately modified without departing from the gist thereof.

10 Dryer (drying part)
20 Carbonization furnace 20a Gap 21 Main body 22 Cylindrical part 23 Organic waste input part 24 Carbide discharge part 25 Primary air supply part (air supply part)
26 Secondary air supply section (second air supply section)
27 Combustion gas discharge unit 28a Temperature sensor 28b Temperature sensor (1st temperature detection unit)
28c temperature sensor (second temperature detector)
28d level sensor (deposition amount detection unit)
29 Carbonization furnace control unit (control unit)
30 Pyrolysis furnace (pyrolysis part)
40 Incubator 41 Char recovery device (carbide recovery section)
51 Residue recovery device (carbide recovery section)
90 Control device 100 Water gas generation system 300 Carbide production system 310 Carbide recovery device R1 Carbide refining / cooling area R2 Primary combustion area R3 Raw material input area R4 Secondary combustion area W, X, Y, Z Axis

Claims (9)

The main body, which is formed in a tubular shape that extends along the axis,
A tubular portion having a tubular shape extending along the axis and an outer peripheral surface forming a gap for carbonizing organic substances with the inner peripheral surface of the main body portion.
An organic substance charging section for charging the organic substance into the gap,
An air supply unit that supplies combustion air that partially burns the organic matter that accumulates in the gap,
A carbide discharge part that discharges carbonized matter obtained by carbonizing the organic matter from the gap,
A carbide manufacturing apparatus comprising a control unit that controls a carbonized state of the organic substance so that the organic substance is maintained in a predetermined temperature range in the gap and the organic substance is deposited in the gap over a predetermined time .
A first temperature detection unit that detects the ambient temperature in the region where partial combustion is performed,
A second temperature detection unit that detects the temperature of the organic matter deposited in the gap,
A third temperature detection unit that detects the temperature of the combustion gas of the combustion gas discharge unit that discharges the combustion gas of the organic substance,
A deposit amount detection unit that detects the deposit amount of the organic matter deposited in the gap,
A primary air supply unit that supplies external air to the air supply unit to burn organic matter,
A secondary air supply unit that supplies external air to burn the flammable gas contained in the combustion gas between the air supply unit and the combustion gas discharge unit.
A rotating body, which is provided in the carbide discharging portion at a position facing the lower end of the gap and the lower end of the gap, and which guides the carbide from the lower end of the gap to the discharging port by rotating around the axis. Has a drive unit, which rotates around the axis.
The control unit is a carbide manufacturing apparatus that performs the following control with a control cycle of 3 seconds.
When the detection temperature of the first temperature detection unit is lower than the predetermined first atmosphere temperature, the amount of air supplied from the primary air supply unit is increased.
When the detection temperature of the second temperature detection unit is equal to or higher than the predetermined carbide temperature, the rotation speed of the rotating body is rotated at a second rotation speed lower than the first rotation speed of normal operation.
When the detection temperature of the third temperature detection unit is lower than the predetermined first combustion gas temperature, the amount of air supplied from the secondary air supply unit is reduced. The carbide production apparatus according to claim 1, wherein the control unit further controls the following.
The amount of air supplied from the primary air supply unit when the detection temperature of the first temperature detection unit is equal to or higher than the first atmosphere temperature and further exceeds a predetermined second atmosphere temperature higher than the first atmosphere temperature. Decrease
When the detection temperature of the second temperature detection unit is lower than the predetermined carbide temperature, and when the detected accumulation amount of the accumulation amount detection unit is less than or equal to the predetermined accumulation amount, the rotation speed of the rotating body is set to the second rotation speed. Rotates at, and when the amount of accumulation exceeds the predetermined amount, the rotation speed of the rotating body is rotated at the first rotation speed.
When the detection temperature of the third temperature detection unit is equal to or higher than the predetermined first combustion gas temperature and further exceeds the predetermined second combustion gas temperature higher than the first combustion gas temperature, the secondary air supply unit Increased air supply The carbide production apparatus according to claim 1 or 2 , wherein the predetermined temperature range is 900 ° C. or higher and 1200 ° C. or lower. The carbide production apparatus according to any one of claims 1 to 3 , wherein the predetermined time is 30 minutes or more and 50 minutes or less. A pyrolysis section that produces an aqueous gas by thermally decomposing the carbide discharged from the carbide discharge section with water vapor.
The carbide manufacturing apparatus according to any one of claims 1 to 4 , further comprising a carbide recovery unit that recovers the carbide discharged from the thermal decomposition unit. An outer circumference that forms a gap for carbonizing organic substances between the main body portion that is formed in a tubular shape that extends along the axis and the inner peripheral surface of the main body that is formed in a tubular shape that extends along the axis. A carbide manufacturing method using a carbide manufacturing apparatus including a tubular portion having a surface.
An organic substance charging step of charging the organic substance into the gap, and
An air supply step of supplying combustion air to the gap and partially burning the organic matter deposited in the gap.
A carbide discharge step of discharging carbonized matter obtained by carbonizing the organic matter from the gap,
A carbide production method comprising a control step of controlling the carbonization state of the organic matter so that the organic matter is maintained in a predetermined temperature range in the gap and the organic matter is deposited in the gap over a predetermined time .
After the organic substance charging step, a first temperature detecting step of detecting the ambient temperature of the region where the partial combustion is performed, a second temperature detecting step of detecting the temperature of the organic substance deposited in the gap, and discharging of the combustion gas of the organic substance. A third temperature detection step for detecting the temperature of the combustion gas, and a deposit amount detection step for detecting the amount of the organic matter deposited in the gap.
The air supply step includes a primary combustion air supply step of supplying external air to burn organic matter.
After the air supply step, a secondary combustion air supply step of supplying external air to burn the flammable gas contained in the combustion gas is performed.
The carbide discharge step includes a carbide discharge step of guiding the carbide from the lower end of the gap to the discharge port by a rotating body provided at a position facing the lower end of the gap and rotating around the axis.
In the control step, a carbide production method in which the following control is performed with a control cycle of 3 seconds.
When the detection temperature of the first temperature detection step is lower than the predetermined first atmosphere temperature, the amount of air supplied from the primary air supply step is increased.
When the detection temperature in the second temperature detection step is equal to or higher than the predetermined carbide temperature, the rotating body is rotated at a second rotation speed lower than the first rotation speed in normal operation.
When the detection temperature of the third temperature detection step is lower than the predetermined first combustion gas temperature, the amount of air supplied from the secondary air supply step is reduced. The carbide production method according to claim 7, wherein the following control is further performed in the control step.
The amount of air supplied from the primary air supply step when the detection temperature in the first temperature detection step is equal to or higher than the first atmospheric temperature and further higher than the first atmospheric temperature to a predetermined second atmospheric temperature or lower. Decrease
When the detection temperature in the second temperature detection step is lower than the predetermined carbide temperature, and when the detection deposit amount in the deposit amount detection step is equal to or less than the predetermined deposit amount, the rotation speed of the rotating body is set to the second rotation speed. Rotates at, and when the amount of accumulation exceeds the predetermined amount, the rotation speed of the rotating body is rotated at the first rotation speed.
From the secondary air supply step when the detection temperature in the third temperature detection step is equal to or higher than the predetermined first combustion gas temperature and further exceeds the predetermined second combustion gas temperature higher than the first combustion gas temperature. Increased air supply The carbide production apparatus according to any one of claims 1 to 4 .
A heat exchange unit that exchanges heat between the combustion gas discharged from the carbide production apparatus and the heat medium,
A carbide manufacturing system including a power generation unit that generates power by obtaining power from a heat medium heated by the heat exchange unit. The carbide production system according to claim 8 , further comprising a drying unit for drying the organic substance charged from the organic substance charging unit by the combustion gas exchanged with heat in the heat exchange unit.