JP6886242B2 - Hydrogen supply system - Google Patents

Description

The present invention relates to a hydrogen supply system that thermally decomposes and gasifies biomass (organic waste such as waste wood), purifies and compresses hydrogen using the obtained water gas, and supplies hydrogen.

In recent years, pyrolysis gasification of wood-based materials containing a large amount of biomass, especially lignin, has great potential as a supply source of new energy resources, and attempts are being made to effectively utilize it. In order to pyrolyze and gasify wood-based materials, carbonized material is recovered from woody biomass, which is a raw material, at a carbonization furnace temperature of 1000 to 1200 ° C. To generate water gas.

As an alternative energy resource to fossil fuels, the method of recovering energy from biomass and waste by thermochemical methods has attracted attention, and in addition to steam turbine power generation using boiler equipment, a gas engine with high power generation efficiency using generated gas as fuel gas. It generates electricity and has a power generation efficiency of over 35%. In addition, since the synthetic gas obtained by gasification can be used as a raw material for liquid fuels such as methanol, synthetic light oil, and mixed alcohol, gasification technology is attracting attention as one of petroleum alternative combustion technologies.

In biomass power generation, gas engines, gas turbine engines, steam turbine engines and the like are used. Among them, the gas engine has the same engine structure as the gasoline engine, is more compact (about 50 to 4000 kW) than other engines, has high power generation efficiency, and is suitable for biomass power generation. However, the calorific value of the pyrolysis gas (water gas) is determined by the content ratio of the combustible gas (CO, H _{2) in the gas.} That is, if _{there is a fluctuation in the composition ratio of hydrogen (H 2} ), carbon monoxide (CO) and carbon dioxide (CO ₂ ) in the water gas, the calorific value changes, which affects the rotation speed of the engine that rotates the generator. Not only is it not possible to obtain stable power, but it also causes problems due to overheating and the like, which is a problem. It is also conceivable to directly supply the water vapor generated in the conventional boiler to the pyrolysis gasifier, but there is a possibility that the temperature distribution in the gasification region will be blurred or extra gas such as methane gas will be generated due to excess or deficiency of heat. There is a problem that occurs.

Therefore, the applicant heats the steam generated in the boiler and supplies the high-temperature superheated steam to the gasification region of the pyrolysis gasification device without lowering the temperature of the gasification region and the high temperature of the carbonization furnace. We first proposed a biomass power generation system that can stabilize the temperature distribution in the region by the synergistic effect with the radiant heat of the exhaust gas, further make the composition ratio of the water gas more uniform, and prevent the generation of methane gas etc. in the water gas component. It is applied as Patent Document 1.

Japanese Unexamined Patent Publication No. 2015-165019

Hydrogen stations have also been proposed as an alternative to gas stations that use conventional fossil fuels to supply fuel to automobiles and the like. In order to supply hydrogen to a hydrogen station or the like, it is necessary to remove impurities as well as hydrogen purity as hydrogen gas used for a fuel cell vehicle.

The present inventor has improved the carbonization furnace and pyrolysis furnace used in the previously proposed biomass power generation system to generate water gas, and further refined the obtained water gas by hydrogen using the mechanism of water gas generation. We focused on applying compression. Then, a new hydrogen supply system suitable for use in fuel cell vehicles and the like was developed.

As a previously proposed carbonization furnace used to generate water gas for hydrogen supply, a solid with a large amount of carbonization above the region formed between a substantially circular body and a cylindrical body housed in the body. A carbonized part that carbonizes the portion is formed, and a non-combustible part that extinguishes the carbonized material is formed below. If the amount of air is not appropriate, the combustion efficiency of combustible gas will deteriorate.

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

Due to the decrease in combustion efficiency and the outflow of combustion gas, the composition ratio of the water gas supplied to the downstream equipment may fluctuate, resulting in malfunction of each equipment and imbalance of the system, and the efficiency of the entire system also decreases. It ends up.

An object of the present invention is to solve such a problem and to provide a safe and efficient hydrogen supply system.

In order to solve the above problems, the present invention uses a carbonization furnace for carbonizing biomass and a combustion gas obtained in the carbonization furnace as a heat source, and generates a pyrolysis gas by the carbides and steam obtained in the carbonization furnace. A pyrolysis furnace for combustion, a hydrogen purification device for purifying the aqueous gas obtained by cleaning the pyrolysis gas, and a hydrogen compression device are provided to generate and supply hydrogen gas from the biomass, and air is supplied to the carbonization furnace. A means for controlling the temperature according to the supply amount of the above is provided, and the temperature-controlled combustion gas is supplied to the pyrolysis furnace, and the carbonization furnace supplies the primary combustion air for partially burning the biomass toward the deposited biomass. It has a primary air supply unit for combusting the combustible gas contained in the combustion gas generated in the primary combustion region where the biomass is partially combusted, and a secondary air supply unit for supplying secondary combustion air for combusting the combustible gas. It provides a hydrogen supply system characterized by.

According to the present invention, hydrogen gas can be efficiently and stably extracted from biomass such as wood chips as an alternative energy resource instead of fossil fuel by a thermochemical method, and hydrogen gas can be supplied as an energy resource.

Further, the present invention is characterized in that the hydrogen purification apparatus includes an aqueous gas compression means and a pressurized adsorption means for adsorbing unnecessary substances from the hydrogen gas obtained by the aqueous gas compression means.

According to the present invention, the purity of hydrogen gas is high and stable extraction is possible.

Further, in the present invention, the carbonization furnace is provided with means for controlling the temperature according to the amount of air supplied, and the temperature-controlled combustion gas is supplied to the pyrolysis furnace. A reaction tube protruding from the upper end of the main body is provided inside the main body, a heating flow path is provided between the inner wall of the main body and the outer peripheral surface of the reaction tube, and the inside of the reaction tube is a carbonized product and a gasifying agent. It is characterized in that the obtained aqueous gas is used as a reaction unit of the above and supplied to the hydrogen purification apparatus.

According to the present invention, it is possible to control an appropriate amount of air for burning flammable gas, maintain high combustion efficiency and stably, contribute to stabilization to a device on the downstream side, and burn from a pyrolysis furnace. Water gas can be efficiently taken out without the gas flowing out.

Further, the present invention is characterized in that a dryer is provided in front of the carbonization furnace to pre-dry the biomass to be charged into the carbonization furnace.

According to the present invention, various wastes, waste materials, wood chips and the like can be used as biomass to generate and supply hydrogen gas as renewable energy.

Further, the present invention is characterized in that a plurality of inclined plates are provided inside the reaction tube of the pyrolysis furnace, and carbides are gradually retained from the upper end side to the lower end side.

According to the present invention, water gas can be efficiently extracted from carbides.

Further, in the present invention, in the pyrolysis furnace, a recovery means for recovering the unreacted product after the reaction between the carbide and the gasifying agent in the pyrolysis furnace and the pyrolysis furnace for recovering the unreacted product from the recovery means. The unreacted material is provided with a transporting means for transporting the unreacted material to the upper part of the reaction tube, and the unreacted material can be put into the pyrolysis furnace again.

According to the present invention, the residence time of carbides in the reaction tube can be lengthened, water gas can be efficiently extracted, and the supply amount of hydrogen gas can be increased.

According to the present invention, a carbonization furnace having improved combustion efficiency of biomass and a pyrolysis furnace capable of stable thermal decomposition can be used to generate an aqueous gas having a small fluctuation in composition ratio, and the aqueous gas can be further produced. By hydrogen purification and compression, hydrogen gas having high hydrogen purity and few irregularities can be generated, and a safe and efficient hydrogen supply system can be provided. Further, according to the present invention, it is possible to provide a larger amount of hydrogen gas by using a return system of a pyrolysis furnace capable of increasing the reaction efficiency of carbides and increasing the amount of water gas to be purified.

It is a block diagram of the hydrogen supply system which concerns on one Embodiment of this invention. The block diagram of the hydrogen supply system which concerns on one Embodiment of this invention is shown, and it is the block diagram of the water gas generator. The block diagram of the hydrogen supply system which concerns on one Embodiment of this invention is shown, and it is the block diagram of a water tank purification apparatus and a hydrogen compression apparatus. It is a vertical sectional view of the carbonization furnace which concerns on one Embodiment of this invention shown in FIG. 2A and FIG. 2B. 2A and 2B are vertical cross-sectional views of a pyrolysis furnace according to an embodiment of the present invention shown in FIGS. 2A and 2B. It is a block diagram which shows the pyrolysis furnace, the thermostat, the cyclone, the steam generator, and the steam superheater which concerns on one Embodiment of this invention shown in FIG. 2A and FIG. 2B. It is a block diagram of the return system of the pyrolysis furnace which concerns on other embodiment of this invention. It is a block diagram which shows the dryer which concerns on one Embodiment of this invention shown in FIG. 2A and FIG. 2B.

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

The hydrogen supply system according to an embodiment of the present invention uses biomass (organic waste), which is a waste containing carbon, as a raw material and carbonizes it to generate carbide, and then superheats steam (hereinafter, also referred to as “steam”). Aqueous gas (mixed gas containing hydrogen gas, carbon monoxide gas, and carbon dioxide gas as main components) is generated by thermally decomposing carbides using.) As a gas agent, and this aqueous gas is further purified by hydrogen. It is a system in which hydrogen gas is obtained by purifying with an apparatus and applying hydrogen compression with a hydrogen compression apparatus.

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

FIG. 1 shows a block diagram of a hydrogen supply system according to an embodiment of the present invention, and FIGS. 2A and 2B show a configuration diagram of a hydrogen supply system according to an embodiment of the present invention. In FIG. 2, FIG. 2A shows a block diagram of a water gas generator, and FIG. 2B shows a block diagram of a water tank purification device and a hydrogen compression device. In addition, with respect to the block diagram of FIG. 1, in the block diagram of FIGS. 2A and 2B, there are a part where the description is omitted and a part which is detailed. Further, in FIGS. 1 and 2 (FIGS. 2A and 2B), the functions of the water gas generator, the hydrogen purification apparatus, and the hydrogen compression apparatus are shown separately for convenience. Is not strictly classified and is not construed as being limited to these embodiments. The hydrogen supply system of the present invention is provided in cooperation with each of the illustrated devices.

As shown in FIGS. 1, 2A and 2B, the hydrogen supply system according to the embodiment of the present invention includes a water gas generator A, a hydrogen purification device 71, and a hydrogen compression device 72, and further comprises hydrogen. A station supply holder 73 may be provided.

The water gas generator A crushes biomass (organic waste) such as wood chips, which is a raw material, into chips by a raw material crusher or the like, or carries it in by a truck or the like and stores the organic waste to be put into the dryer. A raw material hopper 11, a dryer 10 that dries organic waste such as crushed wood chips using waste heat (high temperature exhaust gas), and a carbonization furnace 20 that produces carbonized products from the dried organic waste such as wood chips. , A pyrolysis furnace 30 that thermally decomposes the carbonized material generated in the carbonization furnace 20 and a gasifying agent, a thermostat 40 that cools the water gas generated in the thermal decomposition furnace 30, and discharge from the carbonization furnace 20. A char recovery device 41 that recovers the unburned carbonized material, a cyclone 50 that removes the residue from the water gas supplied from the thermostat 40, and a residue recovery device 51 that recovers the residue removed by the cyclone 50. A CO reforming tower 55 in which the aqueous gas from which the residue has been removed by the cyclone 50 is subjected to a CO shift reaction with a catalyst, an aqueous gas cleaning tower 60 for cleaning the modified aqueous gas, and a clean aqueous gas that has been cleaned are maintained. It is provided with a water gas holder 70 and the like. Further, it includes 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, and the like. Further, a control device 90 for controlling each device of the water gas generator A is provided. The control device 90 is a control device that controls the entire system including a hydrogen purification device, a hydrogen compression device, and the like, which will be described later.

Hereinafter, each part included in the water gas generator A will be described.

Organic waste such as wood chips thrown into the dryer 10 from the raw material popper 11 via the raw material supply path 11a by the automatic dispensing mechanism is dried by the combustion gas in the dryer 10 and supplied to the carbonization furnace. 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 raw material hopper 11 to the dryer 10 is, for example, a wooden chip having a length of 5 mm or more and 60 mm or less. Further, the organic waste reduces the water content of the organic waste to a weight ratio of about 15% by heating and drying the wood chips containing water at a weight ratio of about 55%, for example. is there.

The dryer 10 supplies the organic waste dried by the heat of the combustion gas to the quantitative feeder 12 via the raw material supply path 10a to supply the dried wood chips and the like. The fixed-quantity feeder 12 supplies the dried raw material (wood chips, etc.) to the carbonization furnace 20 via a conveyor while measuring the supply amount per unit time. In this quantitative control, for example, the amount transported per unit time is measured and the weight for a certain period of time is calculated, and the increase or decrease is adjusted by the inverter control of the conveyor.

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, 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. In the configuration diagram of FIG. 2A, as an example of the exhaust gas cooling / cleaning device 13, one including a heat exchanger 13a, an exhaust gas equipment (bug dust collector) 13b, a waste tower 13c, and the like is shown.

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 the dried organic waste from the fixed quantity feeder 12 that supplies the organic waste through the raw material supply path 12a. The carbide furnace 20 supplies the carbides produced by the combustion of organic waste to the pyrolysis furnace 30 via the carbide supply path 101. The carbide supply path 101 is provided with a clinker removing device (101b described later), a magnetic separator (101d described later), and the like.

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

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 heated in the carbide 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, 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 the carbide and the 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 amount of the endothermic reaction represented by the formula (1) is larger than the calorific value of 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 so as to be at room temperature (for example, 25 ° C.) or higher and 350 ° C. or lower. 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 unreacted components and residues of the water gas and carbides generated by the pyrolysis reaction to the heater 40 via the water gas supply path 102. Further, the pyrolysis furnace 30 supplies the combustion gas used as a heat source for the thermal decomposition 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 sprayed on the water gas adjusted in the pyrolysis furnace 30 so as to be 750 ° C. or higher and 900 ° C. or lower so as to be 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 the unreacted portion of the carbide from being discarded without being used for producing the water gas. Therefore, by providing the char recovery device 41, the yield of the water gas from the carbide is improved. Using this char recovery device 41, it is possible to provide a return system of a pyrolysis furnace 30 that is suitable for a power generation system or a hydrogen supply system and has improved water-gas reaction of water gas with high efficiency. The details of this return system will be described later.

The cyclone 50 is a device for removing residues contained in the water gas supplied via the water gas supply path 103. The cyclone 50 centrifuges the residue contained in the water gas by internally swirling the water gas supplied through the water gas supply path 103, guides the residue downward, and supplies the residue to the residue recovery device 51. Further, the cyclone 50 guides the water gas from which the residue has been removed upward and supplies it to the CO reforming tower 55. The CO reforming tower 55 reacts _{CO to CO 2 with a catalyst.} The water gas supplied to this CO reforming tower is subjected to a CO shift reaction with a catalyst, and the water gas composition is, for example, hydrogen H ₂ : 70 to 75%, carbon monoxide CO: 2 to 5 v%, carbon dioxide CO _2. : 23 to 28 v%. The reformed water gas is washed in the water gas washing tower 60. The water gas is sprayed with water which is a liquid in the water gas cleaning tower 60, and is supplied as a clean water gas to the hydrogen purification apparatus 72 via the water gas holder 70.

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 can communicate with a control unit (not shown) included in each part constituting the water gas generator A, and a control unit (not shown) included in each part of the hydrogen purification device 71 and the hydrogen compression device 72 described later. ) Can also be communicated. Further, the control device 90 can also receive signals indicating the states of each part such as temperature and pressure from each part constituting the hydrogen supply system. Further, the control device 90 can make each unit constituting the water gas generator A execute a desired operation by reading and executing the control program stored in the storage unit (not shown).

In the water gas generator A 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 drying machine 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 exhaust gas that has been detoxified by the exhaust gas cooling and cleaning device 13 is discharged into the atmosphere by the exhaust gas cooling and cleaning device 13.

As shown in FIGS. 2A and 2B, the exhaust gas cooling / cleaning device 13 includes, for example, a heat exchanger 13a, a bug dust collector 13b, an exhaust tower 13c, and the like.

Here, the combustion gas generated by the carbonization furnace 20 is supplied to the pyrolysis furnace 30 without exchanging heat with another heat medium by using the pyrolysis gas maintained in a high temperature state. This is to promote the pyrolysis reaction in No. 30 and improve the yield of the water gas from the carbonized material. 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 inside of the pyrolysis furnace 30 can be kept at a high temperature. The reaction is promoted and the yield of aqueous gas from the carbonized material is improved.

Next, the hydrogen purification device 71 and the hydrogen compression device 72 illustrated in FIG. 1 will be described with reference to the configuration diagram of FIG. 2B.

The water gas held in the water gas holder 70 shown in FIG. 2A is supplied to the hydrogen purification device 71 shown in FIG. 2B.

The hydrogen purification apparatus 71 includes an inlet snapper 711, a water gas compressor 712, a front stage heat exchanger 713 and a rear stage heat exchanger 714, an outlet snapper 715, a pressure adsorption tower 716, and a hydrogen holder 717.

The water gas is received from the water gas holder 70 into the inlet snapper 711, cooled by the pre-stage heat exchange tree 13 via the water gas compressor 712, and then pressure-compressed by the water gas compressor 712 again. Further, the compressed water gas is supplied to the pressure adsorption tower 716 via the post-stage heat exchanger 714 and the outlet snapper 715. Indicated by arrows in the figure, S indicates the input fan or cooling water supply, R indicates the discharge fan or cooling water discharge, and cold water or cold air is input to each heat exchanger (or cooler) or the like. Indicates to output. In the present embodiment, the water gas is compressed by the water gas compressor 712 in two steps, but the number of compressions is not limited to this, and the target compression ratio can be achieved. All you need is.

CO, CO _{2 and the} like are adsorbed in the _{pressurized adsorption tower 716, and hydrogen H 2} recovers hydrogen H 2 having a purity of 99.999 v%, and supplies the hydrogen H ₂ to the hydrogen compressor 72 via the hydrogen holder 717.

The pressurized adsorption tower 716 shows an example composed of three towers, and repeats adsorption and regeneration by opening and closing an electromagnetic valve (not shown) with a standby timer to obtain a predetermined hydrogen purity. The number of towers is not limited to these three, and any number of towers can be used as long as hydrogen gas can be obtained with a predetermined purity.

The hydrogen compressor 72 that compresses the hydrogen gas supplied from the hydrogen holder 717 includes a front-stage hydrogen compressor 721, a rear-stage hydrogen compressor 723, and heat exchangers 722 and 724 that cool the hydrogen gas.

The hydrogen gas supplied to the hydrogen compressor 72 is primarily compressed by the pre-stage hydrogen compressor 721, cooled by the pre-stage heat exchanger 722, input to the post-stage hydrogen compressor 723, and is input to the post-stage hydrogen compressor 723 by the post-stage hydrogen compressor 723. It is secondarily compressed and held in the hydrogen station supply holder 73 via the post-stage heat exchanger 724. In this embodiment of the hydrogen compressor, an example of hydrogen compression in two stages is shown, but the present invention is not limited to this, and the hydrogen compression device can be appropriately changed to one stage, three stages, or the like.

The hydrogen gas obtained by hydrogen refining the aqueous gas and hydrogen-compressing it is, for example, hydrogen stations 74 arranged in various places via a hydrogen station supply holder 73 in order to supply the hydrogen gas to a fuel cell vehicle powered by a fuel cell. It will be supplied to the car at.

According to an example of carrying out the present invention
1) About 55 wt% of water is dried to 15 wt% in the dryer 10 and supplied to the carbonization furnace 20.
2) In the carbonization furnace 10, 15 wt% to 25 wt% of clean carbide is recovered with respect to the amount of raw material. As will be described later, the inside of the carbonization furnace 20 is automatically controlled from the upper part to a combustion zone of 1000 ° C. to 1200 ° C., a combustion carbonization zone of 1000 ° C. to 1100 ° C., a refining zone of 1000 ° C. to 1100 ° C., and a digestion zone of 300 ° C. to 500 ° C. , Collect the carbonized material at room temperature on the turntable. The above temperature is automatically controlled to prevent the generation of wood acetic acid, tar, etc.
3) A certain amount of carbonized material recovered in the carbonization furnace is replaced with nitrogen gas N2, and then the air contained in the carbonized portion is supplied to the pyrolysis furnace 30.
4) by thermal decomposition furnace 30, reaction tube 32 is heated to 700 ° C. to 800 ° C. at heat radiation, the reaction rate 80～90Wt% relative to the feed carbides, water gas composition, hydrogen _H 2: 60 ~ 65v%, carbon monoxide CO: 10 to 20v%, carbon dioxide CO ₂ : 20 to 25v% are obtained.
5) The water gas supplied to the CO reforming tower 55 is subjected to a CO shift reaction with a catalyst, so that the water gas composition is hydrogen H 2: 70 to 75 v%, carbon monoxide CO: _{2 to 5 v%, carbon dioxide.} Carbon CO ₂ : 23-28v% is obtained.
6) The water gas is received at 0.01 to 0.06 MpaG by the inlet snapper 711 of the hydrogen purification apparatus 71, and the water gas is compressed to 0.8 to 0.9 MpaG by the water gas compressor 712.
7) Carbon monoxide CO, carbon dioxide CO _{2, and the} like were adsorbed in the pressure adsorption _{tower 716, and hydrogen H 2} having a purity of 99.999 v% was recovered.
_{8) In the hydrogen compressor 72, hydrogen H 2} of 0.8 to 0.9 MpaG supplied from the hydrogen purification device 71 was compressed to 70 MpaG by the compressors 721 and 723.

According to this embodiment, a hydrogen battery vehicle of 250 units / day to 320 units / day can be supplied with a raw material amount of 2 Ton / h (moisture 15 w%) of wood chips and the like (biomass). It is based on 5 kg (56 Nm3) per vehicle.

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

FIG. 3 is a vertical sectional view of a carbonization furnace according to an embodiment of the present invention shown in FIGS. 1 and 2A and 2B.

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

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 the 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. 3, 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 a turntable 24a, which will be described later, so that the turntable 24a rotates about 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 unit 23 is an opening provided in the main body 21 and for charging organic waste (not shown) supplied from the hopper 12 via the raw material supply path 12a into the main body 21. 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 organic waste supplied from the organic waste input unit 23 is guided along the inclined surface 23a to the upper surface 22b of the cylindrical portion 22 and the gap 20a.

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

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.

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

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 guided 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 guided 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 24c to rotate the turntable 24b around the axis X. The drive unit 24b includes a drive motor 24e, a speed reducer 24f, a drive belt 24g, and a drive shaft 24h.

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

The speed reducer 24f is a device that increases 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. The clinker crusher 24d is a substantially annular member arranged around the axis X, and is provided with claws protruding inward in the radial direction at a plurality of positions in the circumferential direction.

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 about the axis X. Therefore, when the clinker moves with the rotation of the turntable 24a, the clinker collides with the claw 24i of the clinker crusher and is crushed.

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

The primary air supply unit 25 is a device that supplies air for primary combustion that partially burns the organic waste toward the organic waste deposited in the gap 20a. The primary air supply unit 25 includes 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.

The cover portion 25b forms a closed space 25d extending around the axis X between the cover portion 25b and the outer peripheral surface of the main body portion 21. Further, 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 the figure, 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, the air supply port 25c is provided in the main body 21 as a linear flow path at equal intervals (for example, at intervals of 30 °, 20 °, 45 °, etc.) along the circumferential direction around the axis X or at arbitrary intervals. ing. Further, the primary air supply unit 25 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 atmospheric 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 unit 21. is there. As shown in FIG. 3, 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.

Similar to the cover portion 25b, the cover portion 26b forms a closed space 26d extending around the axis X between the cover portion 26b and the outer peripheral surface 21e of the main body portion 21.

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. The air supply ports 26c are provided at a plurality of locations in the vertical direction 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. The air supply port 26c is a straight line extending from the outer peripheral surface of the main body 21 toward the axis X at equal intervals (for example, intervals of 30 °, 20 °, 45 °, etc.) along the circumferential direction around the axis X or at arbitrary intervals. It is provided in the main body 21 as a shaped flow path.

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. 3, 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 atmospheric temperature in 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. 3 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 the 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 (zero), the accumulated amount of organic waste existing in the gap 20a. Is determined to have decreased to a predetermined first deposit amount 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. 3, the ignition burner 20c is provided on the lower end side of the gap 20a. Further, as shown in FIG. 3, the ignition burners 20c are arranged at two positions 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 the 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, when the carbonization furnace control unit 29 transmits a control signal to the ignition burner 20c to start combustion of organic waste, the carbonization furnace control unit 29 generates a flame and transmits a control signal at a predetermined timing to stop the generation of the flame. Let me. 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.

The carbonization furnace control unit 29 controls the amount of air blown by the primary combustion fan 25a based on the atmospheric temperature of the primary combustion region R2 detected by the temperature sensor 28b. The amount of air blown by the primary combustion fan 25a matches 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 atmospheric temperature of the primary combustion region R2 falls within the range of 1000 ° C. or higher and 1200 ° C. or lower.

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.

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.

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 starts the combustion of the organic waste deposited in the gap 20a. 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. 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.

After the combustion gas temperature Tg detected by the temperature sensor 28a becomes the first combustion gas temperature Tg1 or more, the temperature is controlled in the following steps 1) to 3).

1) 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.

2) The carbonization furnace control unit 29 determines whether or not the combustion gas temperature Tg detected by the temperature sensor 28a is lower than the first combustion gas temperature Tg1. When the carbonization furnace control unit 29 determines that the combustion gas temperature Tg is lower than the first combustion gas temperature Tg1, the carbonization furnace control unit 29 sends a control signal for reducing the amount of air blown by the secondary combustion fan 26a. It is transmitted 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 constant amount more than the amount of combustible gas contained in the combustion gas existing in the secondary combustion region R4 to be completely burned. 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 combustible 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 a component that solidifies 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.

3) When the carbonization furnace control unit 29 determines that the combustion gas temperature Tg is higher than the first combustion gas temperature Tg1, a control signal for increasing the amount of air blown by the secondary combustion fan 26a is sent to the secondary combustion fan 26a. Communicate to. The secondary combustion fan 26a increases 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 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 the carbonization furnace 20 and the carbonization furnace 20 are assumed so that the maximum heat resistance can be maintained even at the combustion gas temperature, assuming the highest expected combustion gas temperature. It is necessary to design the combustion gas flow path 200a. In this case, it is necessary to manufacture the carbonization furnace 20 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 the second. The temperature of one combustion gas is Tg1 or more and the temperature of the second combustion gas 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.

Each process is performed by the arithmetic unit (not shown) included in the carbonization furnace control unit 29 executing the control program stored in the storage unit (not shown).

The carbonization 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 by the carbide discharge unit when 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 carbide discharged from 24 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, it is controlled in the processes of 1) to 5).

1) 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.

2) The carbonization furnace control unit 29 detects the accumulated amount Ao, which is the accumulated amount of organic waste accumulated in the gap 20a, by receiving the accumulated amount detection signal transmitted from the level sensor 28d.

3) The carbonization 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. 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.

4) When 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 carbonization furnace control unit 29 controls the drive unit 24b so as to rotate the rotation speed of the turntable 24a at the second rotation speed Rs2. To do. 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. Here, 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, which is lower than the rotation speed Rs1, is set. 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.

5) When it is determined that the detected carbide temperature Tc is lower than the first carbide temperature Tc1, the carbide furnace control unit 29 determines whether or not the deposition amount Ao detected by the level sensor 28d is equal to or less than the first deposition amount Ao1. judge. When the carbonization furnace control unit 29 determines that the detected deposit amount Ao is equal to or less than the first deposit amount Ao1, 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 rotation speed of the turntable 24a is rotated for the first time 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, which is lower than the speed Rs1, is set.

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. When 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 carbide furnace control unit 29 carbonizes the amount of carbide required to maintain the operating state. The drive unit 24b is controlled so as to discharge from the discharge unit 24.

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 above control, 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, but this is another embodiment. You may.

For example, the rotation speed of the turntable 24c 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, 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, but other embodiments 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 amount of deposit Ao. Further, for example, the rotation speed of the turntable 24a may be controlled without gradually switching the rotation speed of the turntable 24a so that the distance is proportional to the deposit amount Ao detected by the level sensor 28d. ..

Further, in the above description, 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. There may be.

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.

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

FIG. 4 is a vertical sectional view of the pyrolysis furnace according to the embodiment of the present invention shown in FIGS. 1, 2A and 2B. In FIG. 4, the axis Z is the installation surface on which the pyrolysis furnace 30 is installed. The vertical direction (gravitational direction) orthogonal to (not shown) is shown.

As shown in FIG. 4, the pyrolysis furnace 30 of the present embodiment includes a main body 31, a reaction tube 32, a reaction tube head 33 (supply section), and a water gas outlet nozzle 34 (water gas outlet section). , 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) , A gland packing 39 (third seal portion) is provided.

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 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 attached.

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 a bottom plate 31e in an annular shape in a plan view.

Further, an upper end flange 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. There is.

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. 4, 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. 4, the plurality of first inclined plates 32f and the plurality of second inclined plates 32g are held at a plurality of locations along the axis Z (for example, by holding four holdings). Further, the first inclined plate 32f and the second inclined plate 32g are alternately arranged along the axis Z.

The upper ends of the plurality of holding rods (for example, 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. 4, 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). It has a side flange 33c attached to (omitted).

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

The water gas outlet nozzle 34 is a substantially tubular member attached to the lower end portion 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 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 woven material that can be deformed relatively easily, the sealing property at the portion in contact with the heat insulating material 31b and the heat resistant material 31c is improved.

The gland packing 38 is a member that blocks the outflow of the combustion gas in the combustion gas flow path 30a from the bottom surface 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 resistant 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 between the lower end portion 32c of the reaction tube 32 and the water gas outlet nozzle 34. The gland packing 39 is a member having an annular shape in a plan view having an inner peripheral surface in contact with each of the outer peripheral surface 32d of the reaction tube 32 and the outer peripheral surface of the water gas outlet nozzle.

The gland packing 39 has an annular packing member, an annular packing member, and a packing holding member. By fastening the packing holding member to the bottom plate 31e with a fastening bolt, each packing member contracts in the axis Z direction and expands in the radial direction orthogonal to the axis Z. As the gland packing 39 expands in the radial direction, the inner peripheral surface of the gland packing 39 comes into contact with the outer peripheral surface 32d of the reaction tube 32 and the outer peripheral surface of the water gas outlet nozzle 34 to form a seal region.

Next, with reference to FIG. 5, 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.

As shown in FIG. 5, 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 for removing an iron layer such as a nail contained in the carbide with a magnet. The carbide from which 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 pyrolysis 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 pyrolysis 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 it from happening.

The nitrogen substitution device 30b is a device constituting the thermal decomposition furnace 30, and is a device 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, an electric control valve). , 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 open, the air provided inside the nitrogen substitution device 30b is discharged to the outside together with the carbides, and the inside is replaced with nitrogen gas. It will be in a state of being.

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 and from the nitrogen substitution device 30b to the reaction tube head 33. Supply carbides.

The control device 90 closes the control valve below the nitrogen substitution device 30b after supplying the carbide to the reaction tube from the nitrogen substitution device 30b. 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. Since this nitrogen gas is an inert gas that does not react with the water gas generated in the reaction tube 32, air containing oxygen together with carbides is supplied to the reaction tube 32, and the oxygen and the water gas react with each other to form the water gas. It is possible to prevent the yield from decreasing.

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 the carbide and supplies it to the nitrogen substituent 30b from a supply path (not shown). This detail will be described later as a return system.

The chamber element replacement 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, it has a ball 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.

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 carbonizes the carbide 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 a new unreacted portion of carbide to the inside of the nitrogen substituent 41a.

The control device 90 controls the opening and closing of the control valves above and below the nitrogen substituent 41a as described above, so that the water gas supplied to the char recovery unit 41b together with the unreacted portion of the carbide is supplied 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 substitution device 51a is a device for replacing the water gas supplied from the cyclone 50 together with the residue with the inert nitrogen gas.

The residue recovery unit 51b is a device that recovers the residue discharged from the nitrogen substituent 51a.

The nitrogen substitution device 51a is arranged in each of the upper part connected to the cyclone 50 and the lower part connected to the residue recovery unit 51b, and an electric control valve (for example, a ball) whose opening / closing state is controlled by the control device 90. Has a valve). 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 generating unit 80a is provided on a heat transfer tube (not shown) for internally circulating water that exchanges heat with combustion gas and a cylinder formed so as to cover the heat transfer tube, and a jacket for circulating water inside (not shown). ) 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.

In the equipment of the water gas generator described above, a further improved new system of the pyrolysis furnace will be described with reference to FIG.

FIG. 6 is a block diagram of a return system of a pyrolysis furnace according to another embodiment of the present invention. This return system relates to the char collecting device 41 described with reference to FIG. 1 above, and although a part thereof has been described, it is configured in cooperation with the char collecting device. Further, the pyrolysis furnace 30 shown in FIG. 6 is basically the same as the configuration of FIG. 4 shown as an embodiment of the pyrolysis furnace 30 of FIGS. 1, 2A and 2B. The same applies to the equipment described with reference to FIG. 5 as peripheral equipment of the pyrolysis furnace 30 of the present embodiment. Therefore, in FIG. 6, those having the same reference numerals as those used in the above-described drawings have the same functions.

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

In FIG. 6, a heater 40 and a char recovery device 41 are arranged in the lower stage of the pyrolysis furnace 30, and a carbide receiving hopper 30c and a nitrogen substitution device 30b are arranged in the upper stage of the pyrolysis furnace 30. The char recovery device 41 includes a nitrogen substitution device 41a, a char recovery section 41b, a carbide transport section 41c, a carbide recovery section 41d, and the like. An unreacted material transport path 30d is provided between the carbide transport portion 41c and the receiving hopper 30c. The transport section 41c, the transport path 30d, and the like can be configured by a conveyor, a lifter, or the like, and literally becomes a transport path.

By selectively switching the carbide discharged from the char recovery unit 41b to the carbide transport unit 41c, the unreacted portion can be put into the pyrolysis furnace 30 again via the transport path 30d. This recovery and transportation means constitutes the return system of the pyrolysis furnace.

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

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

Example)
a) Installed a return system that can return 50% to 200% of the unreacted portion b) Resident time in the reaction tube of the pyrolysis furnace: By setting the residence time to 1.5 to 3 times, the aqueous reaction rate is 75% to 80. Increased from% to 90% to 95%.
Therefore, when applied to a hydrogen supply system:
Assuming that the case where the return system is not adopted is 100 Nm3 / h, when the return system is installed, hydrogen of 119 to 127 Nm3 / h can be supplied.
When the raw material (wood chips) is 2 To / h (moisture content 15 wt%),
The amount of hydrogen increases from 660 Nm3 / h to 790 to 838 Nm3 / h (99.999 v% hydrogen).

Next, the dryer 10 of the present embodiment will be described with reference to FIG. 7.

FIG. 7 is a configuration diagram of a dryer according to an embodiment of the present invention shown in FIGS. 1, 2A and 2B.

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 derived 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.

Each of the embodiments described above is exemplified for the understanding of the present invention, and the present invention is not limited to these embodiments and is defined by the description of the scope of claims. Further, as long as it does not deviate from the technical idea of the present invention, the structure equivalent to the configuration described in the claims is also included in the scope of protection of the present invention.

The hydrogen supply system according to the present invention raises the combustion efficiency by controlling the temperature of the carbonization furnace, enables the pyrolysis furnace to be sealed, improves the gasification efficiency, and keeps the composition ratio of the generated water gas constant. Since it can be stably supplied to hydrogen purification and compression processes and high-purity hydrogen gas can be obtained from water gas, hydrogen can be used as an alternative to gas stations that supply fuel to automobiles using fossil fuels. Since the hydrogen supply to stations and the like can be stably supplied, it is extremely useful for energy saving, protection of the natural environment and economically by effective use of biomass.

A ... Water gas generator 10 ... Dryer 13 ... Exhaust gas cooling and cleaning device 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 26 ... Secondary air supply unit 27 ... Combustion gas discharge unit 28a, 28b, 28c ... Temperature sensor (temperature detection unit)
28d ... Level sensor (deposit amount detection unit)
29 ... Carbonization furnace control unit (control unit)
30 ... Thermal decomposition furnace 30d ... Transport path 31 ... Main body 32 ... Reaction tube 32f ... First inclined plate 32g ... Second inclined plate 34 ... Water gas outlet nozzle 35 ... Combustion gas supply unit 36 ... Combustion gas discharge unit 40 ... Reduction Heater 41 ... Char recovery device 50 ... Cyclone 55 ... CO reforming tower 60 ... Water gas cooling device 70 ... Water gas holder 71 ... Hydrogen purification device 711 ... Inlet snapper 712 ... Water gas compressor 715 ... Water gas suction tower 716 ... Outlet Snapper 717 ... Hydrogen holder 72 ... Hydrogen compressor 712 ... Front compressor 723 ... Rear compressor 73 ... Hydrogen station supply holder 80 ... Steam generator 81 ... Steam superheater 82 ... Water supply device 90 ... Control device

Claims (10)

The carbonization furnace that carbonizes biomass, the pyrolysis furnace that uses the combustion gas obtained in the carbonization furnace as a heat source, and the pyrolysis gas is generated by the carbonized substances and steam obtained in the carbonization furnace, and the pyrolysis gas are washed. It is equipped with a hydrogen purification device that purifies the obtained water gas with carbon and a hydrogen compression device.
Hydrogen gas is generated and supplied from the biomass,
The carbonization furnace is provided with a means for controlling the temperature according to the amount of air supplied, and the temperature-controlled combustion gas is supplied to the pyrolysis furnace.
The carbonization furnace
A primary air supply unit that supplies air for primary combustion that partially burns the biomass toward the accumulated biomass, and
A secondary air supply unit that supplies air for secondary combustion that burns flammable gas contained in the combustion gas generated in the primary combustion region where the biomass is partially burned.
A hydrogen supply system characterized by having. The primary air supply unit has a first air blower unit that blows air introduced from the outside.
The secondary air supply unit has a second air blower unit that blows air introduced from the outside.
The hydrogen supply system according to claim 1, further comprising a carbonization furnace control unit that controls the amount of air blown by the first blower unit and controls the amount of air blown by the second blower unit. .. The hydrogen supply according to claim 2, wherein the carbonization furnace control unit controls the amount of air blown by the first blower so that the temperature of the primary combustion region falls within a predetermined temperature range. system. The carbonization furnace control unit
It is determined whether or not the detected temperature of the combustion gas is lower than the predetermined first combustion gas temperature, and if it is determined that the temperature is lower than the first combustion gas temperature, the amount of air blown by the second blower unit is reduced. The hydrogen supply system according to claim 2 or 3, wherein the second blowing unit controls the amount of air blown so as to be blown. The carbonization furnace control unit
When it is determined whether or not the detected temperature of the combustion gas is lower than the predetermined second combustion gas temperature set higher than the first combustion gas temperature, and when it is determined that the temperature is higher than the second combustion gas temperature. The hydrogen supply system according to claim 4, wherein the amount of air blown by the second blower is controlled so that the amount of blown air of the second blower is increased. The pyrolysis furnace
Cylindrical body and
A reaction tube that protrudes from the upper end of the main body inside the main body,
Have,
The inner wall of the main body and the outer peripheral surface of the reaction tube are used as a heating flow path, the inside of the reaction tube is used as a reaction part between a carbide and a gasifying agent, and the obtained water gas is supplied to the hydrogen purification apparatus.
The pyrolysis furnace is a plan-viewing annular member having an inner peripheral surface that is provided so as to be in contact with the lower surface of the upper plate of the main body and that is in contact with the outer peripheral surface of the reaction tube. The hydrogen supply system according to any one of claims 1 to 5, further comprising a gland packing that blocks the combustion gas in the heating flow path from flowing out from the upper plate to the outside. The method according to any one of claims 1 to 6, wherein the hydrogen purification apparatus includes an aqueous gas compression means and a pressurized adsorption means for adsorbing unnecessary substances from the hydrogen gas obtained by the aqueous gas compression means. Hydrogen supply system. The hydrogen supply system according to any one of claims 1 to 7, wherein a dryer is provided in front of the carbonization furnace to pre-dry the biomass to be charged into the carbonization furnace. The hydrogen supply system according to any one of claims 1 to 8, wherein a plurality of inclined plates are provided inside the reaction tube of the pyrolysis furnace, and carbides are gradually retained from the upper end side to the lower end side. In the pyrolysis furnace, a recovery means for recovering the unreacted product after the reaction between the carbide and the gasifying agent in the pyrolysis furnace and the unreacted product are transported from the recovery means to the upper part of the reaction tube of the pyrolysis furnace. Equipped with a means of transportation
The hydrogen supply system according to any one of claims 1 to 9, wherein the unreacted product can be put into the thermal decomposition furnace again.

Images