JP2017132668A - Hydrogen station system - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide an online hydrogen station system in which a hydrogen gas generation system including hydrogen production equipment using renewable energy and a hydrogen gas supply system including equipment for supplying hydrogen gas to motor vehicles are directly connected to each other.SOLUTION: A hydrogen station system directly connects a hydrogen gas generation system A which comprises a water gas generator A-2 for heating carbides, generated by partial combustion of organic waste, together with superheated steam to generate water gas and a hydrogen purification device A-3 for removing impurities from the water gas to separate hydrogen to a hydrogen gas supply system B which comprises a compressor B-1 for compressing the hydrogen, a pressure accumulator B-2 for storing the hydrogen, and a dispenser B-3 for supplying the hydrogen while controlling a flow rate and pressure thereof, and includes a pressure controller C for controlling the pressure of the pressure accumulator which changes with the consumption of the hydrogen and indicating the supply amount of the organic waste according to the change, and a flow controller D for controlling the supply amount of the organic waste according to the indication.SELECTED DRAWING: Figure 1

Description

  The present invention stably supplies hydrogen to a hydrogen gas generation system and a fuel cell vehicle using organic waste (hereinafter referred to as “organic waste”) containing wood waste, which is one of renewable energy sources. The present invention relates to an on-site hydrogen station system directly connected to a hydrogen supply system.

  One of the essential issues for human beings to build a sustainable society without destroying the earth's material circulation system is to regenerate without depleting resources such as fossil fuels and uranium and without destroying the resource environment. The creation of possible clean energy. In other words, instead of fossil energy using petroleum, coal, natural gas, etc., and nuclear energy using uranium, etc., harmful substance emissions (carbon dioxide, Renewable energy that can be produced using solar / solar heat, wind power, hydropower, geothermal power, wave power / tidal power, and biomass that can be used permanently as an energy source. (Non-Patent Document 1).

  Among these, photovoltaic power generation, that is, a solar cell has the following characteristics and is actively being developed. First, since the energy source can be directly converted into electrical energy by a chemical reaction, the minimum unit is extremely small, and it can be mounted on any device or apparatus. Secondly, the module can be applied to houses, public facilities, industrial / commercial facilities, facilities for power generation business, etc., by providing modules with output and durability for batteries, and an array in which many modules are arranged. In particular, silicon-based solar cells have been put to practical use in a wide range of fields, from consumer applications such as calculators, watches, street lights, etc. to power applications used in houses, public facilities, various industries, artificial satellites, and the like. Currently, solar power generation is systemized with silicon solar cells and has been installed in houses, public facilities, industrial / commercial facilities, power generation facilities, etc., and is one of the major pillars of greenhouse gas reduction measures. It has become the most advanced technology. Such silicon-based solar cells also have problems, but are being overcome by organic solar cells and the like that aim to reduce costs, increase the area, and reduce the thickness.

  Furthermore, a fuel cell is expected as a next-generation battery. This is because the fuel cell generates electricity by the reverse reaction of water electrolysis using hydrogen, which is an element that constitutes inexhaustible water on the earth, and oxygen that is inexhaustible in the atmosphere. This is because the power generation system does not emit greenhouse gases.

  Already, a commercial experiment of a household fuel cell cogeneration system represented by ENE-FARM (registered trademark) has been in progress for consumer use. On the other hand, in the transportation field, as the shift from fossil energy to clean energy that does not emit carbon dioxide progresses from gasoline vehicles / diesel vehicles to hybrid vehicles and from hybrid vehicles to electric vehicles, the performance of storage batteries for electric vehicles is limited. Therefore, fuel cell vehicles have been developed as next-generation electric vehicles. In the future, the installation of fuel cells will expand to railway vehicles, jet planes, ships, industrial vehicles, etc., and hydrogen power generation systems using fuel cells will be used for industrial / commercial facilities and power generation facilities. It is expected.

  In particular, fuel vehicles are expected to be put to practical use to the same extent as gasoline and diesel vehicles, as one of the major stages of widespread use of hydrogen power generation systems using fuel cells that use hydrogen and oxygen as raw materials. Yes. This is because fuel cell vehicles having performance comparable to gasoline and diesel vehicles have been developed. However, this has a major problem of building a hydrogen station system that directly connects a hydrogen gas generation system using renewable energy and a hydrogen gas supply system that supplies hydrogen gas to an automobile.

  There are two types of hydrogen station systems, depending on where hydrogen production is performed. One is an off-site type and the other is an on-site type, and each has the following characteristics (Non-Patent Document 2).

  In the off-site type, hydrogen produced at a location different from the hydrogen station where hydrogen is supplied is transported to the hydrogen station in the form of compressed hydrogen or liquid hydrogen by curdle or lorry and stored in a hydrogen tank. The fuel cell vehicle is filled with hydrogen through a compressor that compresses hydrogen therefrom, a pressure accumulator that stores hydrogen at a predetermined pressure, and a dispenser that supplies hydrogen. As described later, there are various methods for producing hydrogen. However, any production method can be used, and hydrogen can be produced with low loss using a large-scale hydrogen production facility, or a hydrogen production facility can be established at a hydrogen station. There is an advantage that it is not necessary to raise. However, conventional mass transportation technology and mass storage technology such as gasoline cannot be used, and since hydrogen gas mass transportation technology and mass storage technology have not been established, hydrogen gas is transported in the form of compressed hydrogen and liquid hydrogen. In addition, there is a great disadvantage in that the costs for the curdles, lorries, tanks, etc. are very high for storage. As a type of off-site type, there is a mobile hydrogen station where all equipment for supplying hydrogen, such as compressors, pressure accumulators, dispensers, etc., is installed on the vehicle, but it covers the area where stationary hydrogen stations are used. is there.

  The on-site type is a system in which a raw material storage tank and a hydrogen production apparatus are provided in a hydrogen station, and the fuel cell vehicle is filled with hydrogen while producing hydrogen. This is a hydrogen production method suitable for the size and location of the hydrogen station, and is limited to medium to small-scale hydrogen production facilities and has the disadvantage that it takes time to start up the hydrogen production facility. However, the transportation cost of hydrogen gas is unnecessary, the conventional technology can be adopted for storing raw materials for producing hydrogen, and the operation rate of the hydrogen production facility according to the hydrogen supply amount to the fuel cell vehicle can be obtained. Therefore, it is not necessary to store a large amount of hydrogen gas. Therefore, there is a great advantage that a hydrogen station system without any loss can be constructed.

  On the other hand, the hydrogen production method in the hydrogen generation system currently includes steam reforming method, partial oxidation reforming method, water electrolysis method, etc., and in the future, coal gasification method, dimethyl ether reforming method, high-temperature steam The electrolysis method, the thermochemical method of water, and the like are expected, but there are the following problems (Non-patent Document 3).

  The steam reforming method uses natural gas mainly composed of methane, liquefied petroleum gas, naphtha, or hydrocarbons such as methanol, ethanol, etc. as raw materials and reacts with steam at high temperature in the presence of a catalyst. Is a method for separating only hydrogen from a gas containing hydrogen and carbon monoxide produced by the above. Although it is the most common method as a large-scale and inexpensive manufacturing method, fossil fuel is used for both raw materials and heat sources, and it cannot be said that it is clean energy. Similarly, the partial oxidation reforming method uses only hydrocarbons such as kerosene, heavy oil and natural gas as raw materials, separates only hydrogen from hydrogen and carbon monoxide produced by mixing air and combusting with a small amount of oxygen. This is not a clean energy. The water electrolysis method is different from the method using fossil fuel described above because it produces hydrogen by electrolysis using abundant water as a raw material, but electrolysis requires enormous electric power, However, since fossil fuels such as thermal power generation must be used, it is not recognized as clean energy. Rather, this method is rarely adopted because it is more efficient to produce hydrogen by reforming fossil fuels.

  And since the hydrogen generation system using the hydrogen production method using the fuel generated from such an oil complex is more efficient as the scale is larger, the location condition of the oil complex, that is, the coastal area away from the house The hydrogen generation system is suitable for an off-site type hydrogen station system because it is installed in a place that is wide and flat and has a strong ground, and requires a lot of labor for transporting hydrogen gas. However, at present, it is also used as a hydrogen generation system of an on-site type hydrogen station system, and is a very inefficient hydrogen generation system.

  The coal gasification method is a method for separating hydrogen from hydrogen, carbon monoxide, and the like produced by gasifying coal at a high temperature. This is focused on abundant coal reserves and stable prices, and is not intended to create clean energy. In particular, coal is a fossil fuel that generates a large amount of greenhouse gases, and requires a large amount of equipment for its recovery.

  Further, the dimethyl ether reforming method, the high-temperature steam electrolysis method, and the thermochemical method of water are expected as methods using the power and heat of nuclear power generation (Non-Patent Document 4). The dimethyl ether reforming method separates hydrogen from dimethyl ether chemically synthesized from natural gas, hydrogen produced from water, and carbon dioxide, and uses a low-temperature heat source of about 250 ° C. in a light water reactor. The high-temperature steam electrolysis method is a method for electrolyzing high-temperature steam generated in a high-temperature gas furnace, and can produce hydrogen more efficiently than ordinary electrolysis. The thermochemical method of water consists of a pyrolysis process of sulfuric acid, a pyrolysis process of hydrogen iodide, and a Bunsen reaction that produces sulfuric acid and hydrogen iodide from these pyrolysis products and water. A high temperature gas furnace is used as a heat source in the method of producing hydrogen only with energy. However, nuclear power generation uses depleted resources called uranium and cannot be said to be renewable energy.

  In addition, a hydrogen generation system using a hydrogen production method that uses the power and heat of nuclear power generation must be connected to a nuclear reactor, so it must be adjacent to a nuclear power plant and produce hydrogen to produce hydrogen. The system must be an off-site hydrogen station system, which is a separate location from the hydrogen station that produces hydrogen.

  In addition, methods have also been developed to solve the problem of hydrogen gas transport and storage in off-site hydrogen station systems. This is an organic chemical hydride method in which hydrogen gas is transported and stored by methylcyclohexane produced by the hydrogenation reaction of toluene (Non-Patent Document 5). According to this method, the produced hydrogen is converted into liquid methylcyclohexane at room temperature and normal pressure by the hydrogenation reaction of toluene, and can be transported and stored. By the dehydrogenation reaction of methylcyclohexane at the place where hydrogen is used. Hydrogen is taken out and the produced toluene is recovered and reused as a hydrogen carrier. However, no mention is made regarding the hydrogen production method, and it does not solve the above-described hydrogen generation system using renewable energy.

  On the other hand, as a hydrogen generation system using renewable energy, there is a method using biomass as an energy source. Since it is converted into energy using the heat obtained by directly burning organic waste derived from biological resources or carbonized, liquefied, and gasified fuel, it is a circulation type that leads to reuse and reduction of waste. It is expected to contribute greatly to the construction of social structures. For example, organic waste is decomposed into gas (hydrogen, carbon monoxide, carbon dioxide, light hydrocarbon gas, etc.), carbides, and hydrocarbons at low temperatures under low oxygen, and thermal decomposition reaction between the carbides and high-temperature steam. A system that uses water gas (hydrogen gas, carbon monoxide gas, carbon dioxide gas as a main component) generated as a fuel for power generation has been reported, and is consistent with carbonization, gasification, and power generation of organic waste. It is of interest as a biomass fuel production process and power generation system (Patent Document 1). Furthermore, from hydrogen, carbon monoxide, light hydrocarbon gas generated by pyrolysis of organic waste such as wood chips and waste plastic with high-temperature steam, and hydrogen, carbon monoxide generated by steam reforming of heavy hydrocarbons A hydrogen production method for separating and purifying hydrogen has been reported (Non-patent Document 6). However, in this case, there is a problem in that hydrogen cannot be efficiently produced because the ratio of hydrogen in the gas generated by pyrolysis and steam reforming is low. For this reason, carbonization furnaces (Patent Document 2) and pyrolysis furnaces (Patent Document 3) for producing water gas having a high hydrogen content from organic waste have been studied, but the hydrogen content is not satisfactory. .

  As is apparent from the above, the conventional hydrogen station system comprising a hydrogen gas generation system including a hydrogen production facility and a hydrogen gas supply system including a facility for supplying hydrogen gas to an automobile is either an offline type or an online type. In addition, there is a problem that the hydrogen gas generation system does not use a hydrogen production method using renewable energy. Furthermore, in the case of the offline type, there is a problem that the hydrogen gas must be transported from the hydrogen gas generation system to the hydrogen gas supply system and stored in large quantities. In the case of the online type, the location of the hydrogen gas supply system is required. There is a problem that an inefficient hydrogen production method must be adopted depending on conditions.

  Therefore, in order to disseminate fuel cell vehicles as widely as gasoline and diesel vehicles by using energy that does not destroy the earth's material circulation system and do not use depleting resources such as fossil fuels and uranium, It is necessary to construct an on-site hydrogen station system that directly connects a hydrogen gas generation system that uses possible energy and a hydrogen gas supply system that supplies hydrogen gas to an automobile.

Japanese Patent Laying-Open No. 2015-165019 Japanese Patent No. 4222666 Japanese Patent No. 5342664

Independent administrative corporation, New Energy and Industrial Technology Development Organization, "NEDO Renewable Energy Technology White Paper Second Edition", February 2014, Morikita Publishing Co., Ltd. Hydrogen Supply and Utilization Technology Research Association website, “Hydrogen Station” (panel at the 2015 FC EXPO exhibition), http: // hysut. or. jp / information / pdf / DS002. pdf Independent administrative corporation, industrial property information and training hall, “2005 Patent Distribution Support Chart (General 20) Hydrogen Production Technology”, March 2006 Akira Ozaki et al., “Nuclear Hydrogen Production System”, Toshiba Review, Vol. 60, no. 2 (2005) Yoshida Okada, “Safety of large-scale long-distance transportation technology of hydrogen energy by organic chemical hydride method”, Hydrogen Energy System, Vol. 35, no. 4, pp. 19-24 (2010) Koichi Yamamoto, “Hydrogen production equipment using raw gas from unused resources using high-temperature steam”, Energia Research Institute Review, No. 14, pp. 16-19

  A conventional hydrogen station system comprising a hydrogen gas generation system including a hydrogen production facility and a hydrogen gas supply system including a facility for supplying hydrogen gas to an automobile provides renewable energy in both offline and on-line types. There was a problem that it was not a hydrogen gas generation system equipped with a hydrogen production facility to be used. Furthermore, in the case of the offline type, there is a problem that the hydrogen gas must be transported from the hydrogen gas generation system to the hydrogen gas supply system and stored in large quantities. In the case of the online type, the location of the hydrogen gas supply system is required. There is a problem that an inefficient hydrogen production method must be adopted depending on conditions.

  Accordingly, the present invention provides an online hydrogen station system in which a hydrogen gas generation system including a hydrogen production facility using renewable energy and a hydrogen gas supply system including a facility for supplying hydrogen gas to an automobile are directly connected. Objective.

  In order to solve the above-mentioned problems, an on-line hydrogen station system of the present invention includes an organic waste supply device, and a gasifying agent (hereinafter referred to as a gasifying agent) generated by partial combustion of organic waste supplied from the organic waste supply device. A water gas generator that generates water gas by heating together with “superheated steam” or “superheated steam”, and hydrogen that produces hydrogen by removing impurities from the water gas generated by the water gas generator A hydrogen gas generation system comprising a purifying device, a compressor that makes hydrogen produced by the hydrogen gas generation system a predetermined pressure, a pressure accumulator that stores hydrogen that has been brought to a predetermined pressure by the compressor, and a pressure accumulator A hydrogen gas supply system having a dispenser for supplying hydrogen while controlling the flow rate and pressure of the hydrogen stored in the tank, and is connected between the organic waste supply device and the pressure accumulator. A pressure control device that controls the pressure of the pressure accumulator that changes with the amount of hydrogen consumed, and also instructs the supply amount of organic waste according to the change, and the flow rate that controls the supply amount of organic waste according to the instruction And a control device.

  In the hydrogen station system of the present invention, the hydrogen gas generation system includes a carbonization furnace that partially burns organic waste to generate carbides and combustion gas, and the carbide generated by the carbonization furnace is heated by combustion gas together with superheated steam. A pyrolysis furnace that generates water gas, a steam generator that heats water with the combustion gas to generate steam, and the steam generated by the steam generator is superheated with the combustion gas and the superheated steam is decomposed into the pyrolysis furnace A steam superheater that supplies water, a dryer that dries organic waste with combustion gas, and supplies the dried organic waste to the carbonization furnace, and removes harmful substances from the combustion gas discharged from the dryer and is harmless The exhaust gas cooling and cleaning device and the combustion gas generated by the carbonization furnace are supplied to the pyrolysis furnace, and the combustion gas discharged from the pyrolysis furnace is supplied to the steam superheater. A combustion gas flow path for supplying the discharged combustion gas to the steam generator, supplying the combustion gas discharged from the steam generator to the dryer, and supplying the combustion gas discharged from the dryer to the exhaust gas cooling and cleaning device; A char recovery device that recovers unreacted carbide discharged from the pyrolysis furnace and supplies it to the pyrolysis furnace again, a temperature reducer that cools the water gas generated in the pyrolysis furnace, and a temperature reducer A cyclone for removing the residue from the generated water gas, a residue collecting device for collecting the residue removed by the cyclone, a water gas cooling device for cooling the water gas from which the residue has been removed by the cyclone, and a water gas cooling device And a water gas holder for storing the generated water gas.

  In particular, the carbonization furnace of the water gas generator constituting the hydrogen gas generation system of the hydrogen station system of the present invention is formed in a cylindrical shape extending along the axis, and a main body formed in a cylindrical shape extending along the axis. In addition, the organic waste is injected into the gap formed by the cylindrical portion having an outer peripheral surface that forms a gap for carbonizing the organic waste between the inner peripheral surface of the main body portion and the main body portion and the cylindrical portion. An air supply unit that supplies combustion air for organic waste accumulated in a gap formed by the input unit, the main body unit, and the cylinder unit, and a combustion gas exhaust that exhausts combustion gas generated by the combustion of the organic waste A carbide discharge unit that discharges carbides carbonized by combustion of organic waste from the gap formed by the main body unit and the cylinder unit, and a carbonization furnace control unit that controls the combustion conditions of the organic waste It is characterized by that.

  More specifically, the carbonization furnace is configured such that organic waste is formed between a main body portion formed in a cylindrical shape extending along an axis and a cylindrical portion extending along the axis and an inner peripheral surface of the main body portion. From the cylinder part which has the outer peripheral surface which forms the gap | interval for carbonization, the input part which throws an organic waste into the gap | interval formed with a main-body part and a cylinder part, and the gap | interval formed with a main-body part and a cylinder part A carbide discharge section for discharging carbide obtained by carbonizing organic waste; a first air supply section for supplying primary combustion air for partially burning organic waste deposited in a gap formed by the main body section and the cylinder section; A second air supply unit for supplying secondary combustion air for burning a combustible gas contained in a combustion gas generated by the combustion of organic waste into the main body, and a combustion gas discharge unit for discharging the combustion gas And detects the temperature of the combustion gas discharged from the combustion gas discharge section The temperature of the carbide deposited on the lower end side of the gap formed by the main body portion and the cylinder portion is detected. Carbide temperature detection unit, a deposition amount detection unit for detecting the amount of organic waste deposited in a gap formed by the main body unit and the cylinder unit, and a primary combustion region detected by the primary combustion region temperature detection unit The first air supply unit, the second air, respectively, according to the temperature, the combustion gas temperature detected by the combustion gas temperature detection unit, the carbide temperature detected by the carbide temperature detection unit, and the deposition amount detected by the deposition amount detection unit It is characterized by comprising a supply unit and a carbonization furnace control unit that controls the discharge amount of the carbide discharged by the carbide discharge unit.

The pyrolysis furnace of the water gas generator constituting the hydrogen gas generation system of the hydrogen station system of the present invention is formed in a cylindrical shape extending along the axis, and a main body formed in a cylindrical shape extending along the axis. And a reaction tube having an outer peripheral surface that forms a heating gas passage for circulating a heating gas between the inner peripheral surface of the main body and an upper end projecting from the upper surface of the main body, and a reaction A supply unit that supplies carbide and water vapor to the inside of the reaction tube to generate water gas inside the tube, and a heating gas that is provided above the main unit and supplies the heating gas to the heating gas passage A supply unit, a water gas outlet unit that is attached to the lower end of the reaction tube and leads the water gas generated by the pyrolysis reaction of carbide inside the reaction tube to the outside, and a heating gas provided below the main body unit For heating from the flow path A heating gas discharge section for discharging the gas, and the carbide contained in the reaction tube and supplied from the upper end of the reaction tube in a stepwise manner from the upper end side to the lower end side of the reaction tube to heat the carbide and steam. A thermal decomposition promoting mechanism that promotes a decomposition reaction, and an inner peripheral surface that is provided below the upper surface of the main body so as to contact the upper surface and that contacts the outer peripheral surface of the reaction tube. Heating from the upper surface of the main body The first seal portion for blocking the outflow of the working gas and the lower end portion of the reaction tube protrude from the bottom surface of the main body portion, and are provided in contact with the bottom surface above the bottom surface of the main body portion and in contact with the outer peripheral surface of the reaction tube Has an inner peripheral surface
The outer surface of the reaction tube and the outer surface of the water gas outlet are attached to the second seal portion that blocks outflow of the heating gas from the bottom surface of the main body and the lower end of the reaction tube and the water gas outlet. It has the inner peripheral surface which contacts each, It is characterized by including the 3rd seal | sticker part which interrupts | blocks the outflow of the water gas from the attachment position.

  The hydrogen gas generation system according to the present invention uses hydrogen as an organic fuel to produce hydrogen by refining water gas obtained by pyrolyzing carbide generated by partial combustion with superheated steam using petroleum as a fuel. Unlike a hydrogen gas generation system using a hydrogen production method using fuel generated from a complex, there is no need to be adjacent to an oil complex installed in a coastal area away from a house, and there are no restrictions on site conditions. That is, an on-site gas station directly connected to a hydrogen gas supply system that supplies hydrogen to a fuel cell vehicle can be constructed.

  In addition, the pressure control device and the flow rate control device provided between the pressure accumulator and the organic waste supply device control the supply amount of the organic waste according to the hydrogen supply amount, and the hydrogen gas generation system is unnecessary. Operation can be suppressed.

  Therefore, the transportation cost of hydrogen gas is unnecessary, and there is no need to provide a special device for storing raw materials for producing hydrogen, and the operating rate of the hydrogen production facility according to the amount of hydrogen supplied to the fuel cell vehicle can be achieved. Therefore, it is not necessary to store a large amount of hydrogen gas, and a hydrogen station system with no overall loss can be constructed.

  In particular, since organic waste derived from biological resources is converted into water gas by using heat and carbide obtained by direct combustion and hydrogen is extracted, fossil fuel and Hydrogen can be produced using energy that does not use depleting resources such as uranium, and it can greatly contribute to the construction of a recycling-oriented social structure that leads to reuse and reduction of waste.

  And the water gas generator of the present invention has a high carbonization efficiency and a carbonization furnace with high carbonization efficiency, which discharges carbides with high combustion efficiency and appropriately reduced temperature of the burned carbides compared to conventional carbonization furnaces and pyrolysis furnaces. , Because it uses a pyrolysis furnace in which the outflow of the heating gas is suppressed and the pyrolysis reaction proceeds rapidly, it is possible to more efficiently produce a higher purity water gas and to purify hydrogen. Hydrogen is easily and efficiently produced.

It is a whole lineblock diagram showing one embodiment of a hydrogen station system. It is a block diagram which shows one Embodiment of the hydrogen gas production | generation system which comprises the hydrogen station system of FIG. It is a longitudinal cross-sectional view of the carbonization furnace shown in FIG. It is a principal part enlarged view of the carbonization furnace shown in FIG. It is a figure which shows the clinker crusher shown in FIG. 4, (a) is a top view, (b) is CC arrow end surface of (a). It is an end view of the carbonization furnace shown in FIG. 3, (a) is an AA arrow end view, (b) is an BB arrow end view. It is a longitudinal cross-sectional view which shows the 1st modification of the primary air supply part of a carbonization furnace. It is a longitudinal cross-sectional view which shows the 2nd modification of the primary air supply part of a carbonization furnace. It is a 1 chart which shows the control method of the ventilation volume of the secondary combustion fan by a carbonization furnace control part. It is a flowchart which shows the control method of the rotational speed of the turntable by a carbonization furnace control part. It is a longitudinal cross-sectional view of the pyrolysis furnace shown in FIG. It is sectional drawing of the reaction tube of the thermal decomposition furnace shown in FIG. 11, (a) is DD arrow sectional drawing, (b) is EE arrow sectional drawing. It is a principal part enlarged view of the pyrolysis furnace shown in FIG. It is a block diagram which shows the thermal decomposition furnace, temperature reducer, cyclone, steam generator, and steam superheater which are shown in FIG. It is a block diagram which shows the dryer shown in FIG.

  Hereinafter, the present invention will be described in detail based on an embodiment illustrated in the drawings. However, the present invention is not limited to these embodiments, and only the matters described in the claims. It is specified and can be changed as appropriate without departing from the scope of the invention.

  As shown in FIG. 1, the online hydrogen station system according to an embodiment of the present invention includes a hydrogen gas generation system A, a hydrogen gas supply system B, a pressure control device C, and a flow rate control device D. Yes. The hydrogen gas generation system A includes an organic waste supply apparatus A-1, a water gas generation apparatus A-2, and a hydrogen purification apparatus A-3, and the hydrogen gas supply system B supplies hydrogen gas to a predetermined pressure. Compressor B-1, an accumulator B-2 that stores hydrogen gas at a predetermined pressure, a dispenser B-3 that supplies hydrogen gas to the fuel cell vehicle E while controlling the flow rate and pressure, and surplus hydrogen In order to deliver the gas to each home, etc., a filling device B-4 that fills the cylinder with hydrogen gas is provided. The pressure control device C and the flow rate control device D allow the organic gas of the hydrogen gas generation system to be adjusted according to the amount of hydrogen gas consumed. The supply amount of the organic waste supplied from the waste supply device A-1 to the water gas generation device A-2 is controlled.

  The hydrogen gas generation system A constituting the on-line hydrogen station system generates carbon by carbonizing organic waste, which is carbon-containing waste, and then heats the carbide using superheated steam as a gasifying agent. This is a system for producing hydrogen by generating a water gas (mixed gas containing hydrogen gas, carbon monoxide gas, carbon dioxide gas as a main component) through a decomposition reaction and purifying the water gas.

  Organic waste is, for example, food waste, construction waste, shredder dust, livestock waste, wood waste such as thinned wood and pruned branches, sludge, and general waste discharged from households. Various organic wastes as exemplified above can be used as a raw material for generating water gas, but it is particularly preferable to use wood waste (also referred to as “woody biomass”).

  Furthermore, it is preferable that the hydrogen gas generation system A of the on-line type hydrogen station which is one embodiment of the present invention has a configuration as shown in FIG. The organic waste supply apparatus A-1 stores a dryer 10 that dries organic waste, a hopper 11 that stores organic waste to be input to the dryer 10, and an organic waste that is dried by the dryer 10. The hopper 12, the combustion gas passages 200d and 200e that effectively use the combustion gas generated in the carbonization furnace, and the exhaust gas cooling and cleaning device 13 that processes the exhaust gas discharged by drying the organic waste. The water gas generator A-2 includes a carbonization furnace 20 that generates carbide from the dried organic waste, a pyrolysis furnace 30 that thermally decomposes the carbide generated in the carbonization furnace 20 and superheated steam, and water. Steam generator 80 that generates saturated steam, steam superheater 81 that superheats the steam generated by steam generator 80, water supply device 82 that supplies water to steam generator 80, and combustion generated in carbonization furnace 20 Combustion gas flow paths 200a, 200b, 200c, and 200d that effectively use gas in each process, a temperature reducer 40 that cools the water gas generated in the pyrolysis furnace 30, and unburned gas discharged from the carbonization furnace 20 A char recovery device 41 for recovering the carbides, a cyclone 50 for removing residues from the water gas supplied from the temperature reducer 40, a residue collection device 51 for recovering residues removed by the cyclone 50, and a cyclone The water gas cooling device 60 that cools the water gas from which the residue is removed at 0, the water gas holder 70 that stores the water gas cooled by the water gas cooling device 60, and the entire water gas generator A-2 are controlled. And a control device 90. The hydrogen purifier A-3 removes impurities such as carbon monoxide gas and carbon dioxide gas contained in the water gas by adsorption or separation, and has high purity hydrogen gas (for example, hydrogen gas having a purity of 99.995% or more). Any general purification device that can be purified to any level can be used.

  Subsequently, each part with which organic waste supply apparatus A-1, water gas production | generation apparatus A-2, and hydrogen purification apparatus A-3 are provided is demonstrated in detail sequentially.

  First, the organic waste supply apparatus A-1 will be described. The dryer 10 is an apparatus that dries organic waste with combustion gas and supplies the dried organic waste to the carbonization furnace 20. The dryer 10 is supplied with organic waste from a hopper 11 that stores the organic waste through a raw material supply path 11a. Moreover, the combustion gas discharged | emitted from the steam generator 80 is supplied to the dryer 10 through the combustion gas flow path 200d as a heat source which dries organic waste.

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

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

The exhaust gas cooling and cleaning device 13 is a device that removes harmful substances such as sulfur oxide (SO _X ) and hydrochloric acid (HCl) contained in the combustion gas and renders the combustion gas harmless. The exhaust gas cooling and cleaning device 13 cools the combustion gas (exhaust gas) from which harmful substances have been removed while detoxifying it, and then discharges it into the atmosphere. The exhaust gas cooling and cleaning device 13 is, for example, a scrubber and is adjusted so that the temperature of the combustion gas discharged into the atmosphere is 50 ° C. or less.

  Next, the water gas generator A-2 will be described. The carbonization furnace 20 is an apparatus that generates carbide and combustion gas by partially burning dry organic waste. The carbonized furnace 20 is supplied with the dried organic waste from the hopper 12 that stores the organic waste through the raw material supply path 12a. The carbonization furnace 20 supplies the carbide generated by the combustion of the organic waste to the pyrolysis furnace 30 via the carbide supply path 101. Moreover, the carbonization furnace 20 supplies the combustion gas produced | generated by the combustion of the organic waste to the thermal decomposition furnace 30 via the combustion gas flow path 200a.

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

The pyrolysis furnace 30 causes a pyrolysis reaction of the carbide and superheated steam to generate a water gas mainly composed of hydrogen gas, carbon monoxide gas, and carbon dioxide gas. The thermal decomposition reaction between carbide and superheated steam is a reaction mainly represented by the following formulas (1) and (2). The water gas reaction shown in Formula (1) is an endothermic reaction, and the water gas shift reaction shown in Formula (2) is an exothermic reaction. The endothermic amount of the endothermic reaction shown in formula (1) is larger than the exothermic amount of the exothermic reaction shown in formula (2). Therefore, the thermal decomposition reaction between the carbide and the superheated steam is an endothermic reaction as a whole.
C + H ₂ O → CO + H ₂ (1)
CO + H ₂ O → CO ₂ + H ₂ (2)

  The temperature of the carbide supplied to the pyrolysis furnace 30 is adjusted so as to be normal temperature (for example, 25 ° C.) or higher and 350 ° C. or lower. Moreover, the temperature of the superheated steam supplied to the pyrolysis furnace 30 is adjusted to be 730 ° C. or more and 830 ° C. or less. The temperature of the combustion gas supplied to the pyrolysis furnace 30 is adjusted to be 900 ° C. or higher and 1300 ° C. or lower. Moreover, the temperature of the water gas which the pyrolysis furnace 30 produces | generates is adjusted so that it may become 750 degreeC or more and 950 degrees C or less.

  The pyrolysis furnace 30 supplies unreacted components and residues of the water gas and carbide generated by the pyrolysis reaction to the temperature reducer 40 via the water gas supply path 102. Further, the pyrolysis furnace 30 supplies the combustion gas used as a heat source for the pyrolysis reaction to the steam superheater 81 through the combustion gas channel 200b. The temperature of the combustion gas supplied to the steam superheater 81 is adjusted to be 750 ° C. or higher and 850 ° C. or lower.

  The temperature reducer 40 is a device that lowers the temperature of the water gas supplied from the water gas supply path 102 by spraying liquid water. Water is supplied to the temperature reducer 40 from a water supply device 82 by a water supply pump (not shown). The temperature reducer 40 supplies the temperature-reduced water gas to the cyclone 50 through the water gas supply path 103. Further, the temperature reducer 40 supplies unreacted carbide residues and residues supplied from the water gas supply path 102 to the char recovery device 41. The temperature reducer 40 adjusts the amount of water sprayed so that the water gas adjusted in the pyrolysis furnace 30 is 750 ° C. or higher and 950 ° C. or lower and the water gas is 250 ° C. or higher and 450 ° C. or lower.

  The char recovery device 41 is a device that recovers an unreacted portion of the carbide and supplies it to the pyrolysis furnace 30 again. By providing the char recovery device 41, it is possible to avoid that the unreacted portion of the carbide is not used for the generation of the water gas and is discarded. Therefore, by providing the char recovery device 41, the yield of water gas from the carbide is improved.

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

  The water gas cooling device 60 is a device that lowers the temperature of the water gas supplied from the water gas supply path 104 by washing and cooling with circulating water that is a liquid. The water gas cooling device 60 collects the cooling water washed and cooled in the water gas and circulates the cooling water so that the water is washed and cooled again in the water gas by a circulation pump (not shown).

  The water gas cooling device 60 supplies the cooled water gas to the water gas holder 70. The water gas cooling device 60 is provided with a temperature sensor (not shown) for detecting the temperature of the water gas supplied to the water gas holder 70 and is circulated by a circulation pump (not shown) so that the detected temperature matches the target temperature. Control the amount of cooling water. The water gas cooling device 60 adjusts the circulation amount of water so that the water gas adjusted by the temperature reducer 40 is 250 ° C. or more and 450 ° C. or less, and the water gas is 30 ° C. or more and 50 ° C. or less.

  The water gas holder 70 is a device that stores the water gas supplied from the water gas cooling device 60 and supplies the stored water gas to the hydrogen purifier A-3.

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

  The saturated steam generated by the steam generator 80 is supplied to the steam superheater 81. Further, the combustion gas used as a heat source for vaporizing water in the steam generator 80 is also supplied to the dryer 10 of the organic waste supply apparatus A-1 via the combustion gas channel 200d (the dryer 10). The temperature of the combustion gas supplied to is adjusted to be 540 ° C. or higher and 640 ° C. or lower).

  The steam superheater 81 is a device that generates heated steam from saturated steam by heating the saturated steam with combustion gas. The steam superheater 81 is supplied with saturated steam generated by the steam generator 80. Further, the combustion gas discharged from the pyrolysis furnace 30 is supplied to the steam superheater 81 through the combustion gas flow path 200b. The temperature of the combustion gas supplied to the steam superheater 81 is adjusted to be 750 ° C. or higher and 850 ° C. or lower. The superheated steam generated by the steam superheater 81 is supplied to the pyrolysis furnace 30 as a gasifying agent. 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.

  As described above, the combustion gas passages 200a, 200b, 200c, 200d, and 200e formed between the organic waste supply apparatus A-1 and the water gas generation apparatus A-2 shown in FIG. Compared with the conventional technology that uses a dedicated heat source as a heat source for drying superheated steam and organic waste used as a gasifying agent, the thermal efficiency of the entire device is dramatically improved. improves.

  That is, the flow of the combustion gas generated by the carbonization furnace 20 is organized as follows. First, the combustion gas generated by the carbonization furnace 20 is supplied to the pyrolysis furnace 30 through the combustion gas flow path 200a. Secondly, the combustion gas discharged from the pyrolysis furnace 30 is supplied to the steam superheater 81 through the combustion gas channel 200b. Third, the combustion gas discharged from the steam superheater 81 is supplied to the steam generator 80 through the combustion gas flow path 200c. Fourth, the combustion gas discharged from the steam generator 80 is supplied to the dryer 10 through the combustion gas channel 200d. Fifthly, the combustion gas discharged from the dry operation machine 10 is supplied to the exhaust gas cooling and cleaning device 13 through the combustion gas channel 200e. Sixth, the combustion gas detoxified by the exhaust gas cooling and cleaning device 13 is discharged into the atmosphere by the exhaust gas cooling and cleaning device 13.

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

  The control device 90 is a device that controls the water gas generation device A-2. The control device 90 can communicate with a control unit (not shown) included in each unit constituting the water gas generation device A-2. The control device 90 can control each unit by transmitting a control command to a control unit included in each unit included in the water gas generation device A-2, and the temperature from each unit included in the water gas generation device A-2. A signal indicating the state of each part such as pressure can be received. The control device 90 can cause each unit constituting the water gas generation device A-2 to perform a desired operation by reading and executing a control program stored in a storage unit (not shown).

  Finally, the hydrogen purifier A-3 will be described. This is an apparatus for purifying hydrogen gas having a high purity (for example, hydrogen gas having a purity of 99.995% or more) by removing components such as carbon monoxide gas and carbon dioxide gas contained in the water gas. For example, the hydrogen purifier 73 pressurizes water gas to a predetermined pressure with a compressor (not shown) and fills with an adsorbent (suitable for removing components such as carbon monoxide gas and carbon dioxide gas). It is supplied to an adsorption tower (not shown), and components such as carbon monoxide gas and carbon dioxide gas are adsorbed and removed by an adsorbent, and purified to high purity hydrogen gas. After completion of the adsorption, the adsorption tower is depressurized to desorb components such as carbon monoxide gas and carbon dioxide gas from the adsorbent. By alternately using a plurality of adsorption towers, hydrogen can be continuously purified and delivered. Further, as the hydrogen purification apparatus A-3, a hydrogen purification module using a palladium alloy film that does not transmit any substance other than hydrogen can be used.

  On the other hand, unlike the hydrogen gas generation system A, the hydrogen gas supply system B that is directly connected to the hydrogen gas generation system A to form a hydrogen station system is a general compressor B-1 that has been conventionally used. The pressure accumulator B-2, the dispenser B-3, and the filling device B-4 can sufficiently achieve the object.

  However, not only the hydrogen generation gas generation system A and the hydrogen gas supply system B are directly connected, but also between the pressure accumulator B-2 and the organic waste supply apparatus A-1, according to the consumption of hydrogen gas. While controlling the pressure of the accumulator B-2 which changes, the pressure control apparatus C which instruct | indicates the supply amount of organic waste according to the change, and the flow control which controls the supply amount of organic waste according to the instruction | indication It is necessary to provide the device D. By these control devices, the supply amount of organic waste from the organic waste supply device A-1 to the water gas generation device A-2 in conjunction with the consumption amount of hydrogen gas is determined. An appropriate operation rate without waste is realized.

  Hereinafter, each component apparatus suitable for the hydrogen gas generation system A for efficiently operating the hydrogen station system of the present invention will be described in detail. By using the components shown below, the combustion efficiency and carbonization efficiency are higher than those of conventional carbonization furnaces and pyrolysis furnaces, and the thermal decomposition reaction proceeds quickly, so that water gas with higher purity is more efficient. Hydrogen can be easily purified, hydrogen can be easily purified, hydrogen can be efficiently produced, and a hydrogen gas generation system suitable for a hydrogen station system can be provided.

  FIGS. 3 to 6 show in detail an embodiment of a carbonization furnace suitable for the water gas generation apparatus A-2 of the hydrogen gas generation system A constituting the hydrogen station system of the present invention.

  FIG. 3 is a longitudinal sectional view of the carbonization furnace 20 shown in FIG. In FIG. 3, the axis X indicates the vertical direction (gravity direction) perpendicular to the installation surface (not shown) on which the carbonization furnace 20 is installed.

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

The main body 21 is a member that is formed in a substantially cylindrical shape that extends along the axis X and that is an exterior of the carbonization furnace 20. The main body 21 forms a primary combustion region R2 in which organic waste is partially combusted and a secondary combustion region R4 in which combustible gas contained in the combustion gas generated from the organic waste is combusted. Yes. The main body 21 is attached to a metal (for example, iron) housing 21a that forms the exterior of the carbonization furnace 20, a heat insulating material 21b that is attached to the inner peripheral surface of the housing 21a, and an inner peripheral surface of the heat insulating material 21b. Refractory material 21c.

  The cylindrical portion 22 is a member formed in a substantially cylindrical shape extending along the axis X. The cylindrical portion 22 has an outer peripheral surface 22 a that forms a gap 20 a for combusting organic waste to generate carbides with the inner peripheral surface 21 d of the main body portion 21. Since the cylindrical part 22 becomes high temperature by combustion of organic waste, it is preferable to form the cylindrical part 22 from a heat resistant material (for example, a metal material such as stainless steel). As shown in FIG. 2, the inside of the cylindrical portion 22 is a hollow closed space, and this closed space is not in communication with other spaces. Therefore, the cylindrical portion 22 can heat a certain amount of heat, and is not easily affected by external temperature changes.

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

  The organic waste supplied to the gap 20a is partially combusted by the primary combustion air supplied from the primary air supply unit 25 in the primary combustion region R2, and burns containing solids containing a large amount of carbides and combustible gas. Gas is generated. The solid content containing a large amount of carbide is guided to the lower carbide refining / cooling region R1 along the immediate side 20a, and the combustion gas containing combustible gas is guided to the secondary combustion region R4. The carbide refining / cooling region R <b> 1 is a region where the upper side is closed with organic waste and the primary combustion air from the primary air supply unit 25 is not supplied. Therefore, the carbide is refined while being cooled in the carbide refinement / cooling region R1.

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

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

  The carbide discharge unit 24 is a mechanism for discharging carbide generated by partial combustion of organic waste in the gap 20 a to the carbide supply path 101. The carbide discharged from the carbide discharge unit 24 to the carbide supply path 101 is supplied to the pyrolysis furnace 30. As shown in FIG.2 and FIG.4, the carbide | carbonized_material discharge part 24 has the turntable 24a (rotary body), the drive part 24b, and the carbide | carbonized_material discharge port 24c.

  As shown in FIG. 4, the turntable 24 a is a member provided at a position facing the lower end of the gap 20 a in the axis X direction, and is an annular rotator extending in the circumferential direction around the axis X. The turntable 24a rotates around the axis X by the driving force transmitted from the driving unit 24b. As shown in FIG. 4, the surface of the turntable 24 a facing the lower end of the gap 20 a is an inclined surface that is inclined downward as the distance from the axis line X increases. Therefore, a gap is formed between the lower end of the gap 20a and the inclined surface of the turntable 24a.

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

  The driving unit 24b is a device that transmits driving force to the turntable 24a and rotates the turntable 24a around the axis X. As shown in FIG. 3, 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 24 e is an inverter motor whose rotation speed is controlled by a control signal transmitted from the carbonization furnace control unit 29. The rotational power of the drive motor 24e is transmitted to the speed reducer 24f by the drive belt 24g. The speed reducer 24f is a device that increases the torque while reducing the rotational speed of the rotational power transmitted from the drive motor 24e by the drive belt 24g. The speed reducer 24f transmits the rotational power with increased torque to the drive shaft 24h extending around the axis X. The turntable 24a is connected to the drive shaft 24h. Therefore, the turntable 24a rotates about the axis X as the drive shaft 24h rotates about the axis X.

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

  The clinker crusher 24d is a member for crushing a clinker that is a lump larger than a gap formed between the lower end of the gap 20a and the inclined surface of the turntable 24a. Here, the clinker is obtained by melting the combustion ash generated by the combustion of the organic waste in the primary combustion region R2 into a lump. As shown in FIG. 5A, the clinker crusher 24d is a substantially annular member arranged around the axis X, and claws 24i projecting radially inward are provided at a plurality of positions in the circumferential direction. ing. As shown in FIG. 5B (end view taken along the line CC in FIG. 5A), the claw 24i is bent upward along the inclined surface of the turntable 24a.

  As shown in FIG. 4, the clinker crusher 24d is attached to the main body portion 21 by fastening bolts. The clinker crusher 24d remains fixed to the main body 21 even when the turntable 24a rotates about the axis X. Therefore, when the clinker moves as the turntable 24a rotates, the clinker collides with the claws 24i of the clinker crusher and is crushed.

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

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

  The cover portion 25b is a member that forms a closed space 25d that introduces air blown from the primary combustion fan 25a and supplies air to the air supply port 25c. As shown in FIG. 6A (end view taken along the line AA of the carbonization furnace 20 shown in FIG. 2), the cover portion 25b is a closed space extending around the axis X between the outer peripheral surface 21e of the main body portion 21. 25d is formed.

  The air supply port 25c is a flow path for supplying air blown from the primary combustion fan 25a to the closed space 25d to the primary combustion region R2 inside the main body 21 from the closed space 25d. As shown in FIG. 3, the air supply ports 25 c are provided at a plurality of locations in the vertical direction along the axis X in the primary combustion region R <b> 2 where the organic waste is partially combusted by the primary combustion air.

  Further, as shown in FIG. 6A, the air supply ports 25c are provided in the main body 21 at equal intervals along the circumferential direction around the axis X (30 ° intervals in FIG. 6A). Further, as shown in FIG. 6A, the air supply port 25 c is a linear flow path extending from the outer peripheral surface 21 e of the main body 21 toward the axis X. In the example shown in FIG. 6A, the air supply ports 25c are arranged at intervals of 30 ° along the circumferential direction around the axis X. However, as other intervals (for example, 20 °, 45 °, etc.) Alternatively, they may be arranged at arbitrary intervals instead of at equal intervals.

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

  As the heating unit provided in the primary air supply unit 25, the radiation fins 25e shown in FIGS. 7 and 8 may be employed. The modification of the primary air supply part 25 shown in FIG.7 and FIG.8 uses the air transmitted from the gap | interval 20a of the carbonization furnace 20 via the main-body part 21, and the air ventilated from the primary combustion fan 25a is used. The heat dissipating fins 25e are provided. As shown in FIG.7 and FIG.8, the radiation fin 25e is an annular member that contacts the outer peripheral surface 21e of the main body 21 and extends around the axis X along the outer peripheral surface 21e. The radiation fins 25e are provided at a plurality of locations along the axis X. The radiation fin 25e is attached to the outer peripheral surface 21e of the main body 21 by welding or the like.

  FIG. 7 is a longitudinal sectional view showing a first modification of the primary air supply unit 25. The cover portion 25b of the primary air supply portion 25 shown in FIG. 3 is provided only at substantially the same position in the axis X direction as the air supply rod 25c. On the other hand, the cover portion 25b of the primary air supply unit 25 shown in FIG. 7 is provided so as to include a position below the air supply port 25c in addition to substantially the same position in the axis X direction as the air supply port 25c. It is done.

  7 is a heat transfer member that transfers the ambient temperature of the gap 20a through the outer peripheral surface 21e of the main body 21. Although the outer peripheral surface 21e of the main body 21 is protected by the refractory material 21c and the heat insulating material 21b so that the housing 21a is not overheated, the outer peripheral surface 21e is heated to about 50 ° C to 70 ° C. Therefore, the air (atmosphere) blown from the primary combustion fan 25a can be heated by the radiation fin 25e.

  As shown in FIG. 7, the primary combustion fan 25a blows air introduced from the outside toward the outer peripheral surface 21e of the main body 21 located on the outer peripheral side below the gap 20a. This is because the outer peripheral surface 21e of the main body 21 located on the outer peripheral side below the gap 20a is cooled by air introduced from the outside.

  As shown in FIG. 7, a carbide refining / cooling region R1 is provided below the gap 20a. The carbide refining / cooling region R1 is a region in which the carbide generated in the primary combustion region R2 is refined while being cooled, and therefore it is desirable to maintain the temperature at a certain low level. Therefore, in the present embodiment, the position where the primary combustion fan 25a blows air is set so that the carbide refining / cooling region R1 is cooled.

  FIG. 8 is a cross-sectional view showing a second modification of the primary air supply unit 25. The second modification of the primary air supply unit 25 shown in FIG. 8 is different in that the thickness of the heat insulating material 21b and the position of the outer peripheral surface 21e of the main body 21 are different at the positions where the radiation fins 25e are arranged. This is the same as the first modification shown in FIG.

  As shown in FIG. 8, the distance from the inner peripheral surface 21d of the main body 21 to the outer peripheral surface 21e at the position where the air supply port 25c is arranged is a distance D1. On the other hand, the distance from the inner peripheral surface 21d of the main body 21 to the outer peripheral surface 21e at the position where the radiation fin 25e is disposed is the distance D2. As shown in FIG. 8, the distance D2 is shorter than the distance D1.

  According to the second modified example of the primary air supply unit 25 shown in FIG. 8, compared to the first modified example of the primary air supply unit 25 shown in FIG. The atmospheric temperature is easily transmitted to the outer peripheral surface 21e. Therefore, according to the second modification, the radiating fins 25e are heated to a higher temperature than in the first modification. Therefore, according to the primary air supply unit 25 of the second modification, the air blown by the primary combustion fan 25a can be supplied to the air supply port 25c while being heated to a higher temperature.

  7 and 8 is an annular member extending around the axis X, but other modes may be used. For example, the heat dissipating fin 25e may have a structure that forms a spiral flow path that contacts the outer peripheral surface 21e of the main body 21 and swivels around the axis X along the outer peripheral surface 21e from below to above. .

  Next, the secondary air supply unit 26 will be described. The secondary air supply unit 26 is a device that supplies secondary combustion air for burning the combustible gas contained in the combustion gas generated by the combustion of the organic waste in the primary combustion region R2 to the inside of the main body 21. is there. As shown in FIG. 3, the secondary air supply unit 26 is provided in the secondary combustion region R4 and supplies secondary combustion air toward the secondary combustion region R4. The secondary air supply unit 26 includes a secondary combustion fan 26a, a cover unit 26b, and an air supply port 26c.

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

  The cover portion 26b is a member that forms a closed space 26d that introduces air blown from the secondary combustion fan 26a and supplies air to the air supply port 26c. As shown in FIG. 6B (end view taken along arrow B-B of the carbonization furnace 20 shown in FIG. 3), the cover portion 26 b is a closed space extending around the axis X between the outer peripheral surface 2 le of the main body portion 21. 26d is formed.

  The air supply port 26c is a flow path for supplying air blown from the secondary combustion fan 26a to the closed space 26d to the secondary combustion firing region R4 inside the main body 21 from the closed space 26d. As shown in FIG. 2, the air supply ports 26 c are provided at a plurality of locations in the vertical direction along the axis X in the secondary combustion region R <b> 4 where the combustible gas contained in the combustion gas is combusted by the secondary combustion air. ing.

  As shown in FIG. 6B, the air supply ports 26c are provided in the main body portion 21 at equal intervals along the circumferential direction around the axis X (30 ° intervals in FIG. 6B). Further, as shown in FIG. 6B, the air supply port 26 c is a linear flow path extending from the outer peripheral surface 21 e of the main body 21 toward the axis X. In the example shown in FIG. 6B, the air supply ports 26c are arranged at intervals of 30 ° along the circumferential direction around the axis X. However, as other intervals (for example, 20 °, 45 °, etc.) Alternatively, they may be arranged at arbitrary intervals instead of at equal intervals.

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

  The temperature sensor 28 a is a sensor that detects the temperature of the combustion gas discharged from the combustion gas discharge unit 27. The temperature sensor 28 a transmits a temperature detection signal indicating the detected temperature to the carbonization furnace control unit 29. As shown in FIG. 3, the temperature sensor 28a is arranged in a region close to the combustion gas flow path 200a in the secondary combustion firing region R4. Therefore, the combustion gas temperature Tg detected by the temperature sensor 28a is substantially the same as the temperature of the combustion gas discharged to the combustion gas flow path 200a.

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

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

  The level sensor 28d is a sensor that detects the amount of organic waste deposited in the gap 20a. The level sensor 28d detects the amount of organic waste accumulated in the direction of the axis Y shown in FIG. 3 by obtaining an output signal corresponding to the amount of accumulation in the primary combustion region R2. The level sensor 28d may be a reflective sensor that detects the amount of deposition by receiving reflection of emitted light, ultrasonic waves, or the like. Further, the level sensor 28d may be a transmission type sensor in which a receiving part for receiving emitted X-rays or the like is provided in the cylindrical part 22.

  As will be described later, the level sensor 28d detects that the amount of organic waste deposited in the gap 20a has decreased, such as when the introduction of new organic waste from the organic waste supply unit 23 is stopped. It is a sensor for. For this reason, the level sensor 28d detects the amount of deposition along the axis Y directed downward from the mounting position in the vertical direction. When the carbonization furnace control unit 29 outputs a detection signal indicating that the deposition amount Ao, which is the deposition amount of organic waste detected by the level sensor 28d, is 0, the deposition amount of the organic waste present in the gap 20a is predetermined. It is determined that the first deposition amount Ao1 has decreased.

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

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

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

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

  Next, a method 1 for controlling the blowing amount of the primary combustion fan 25a by the carbonization furnace control unit 29 will be described. The carbonization furnace control unit 29 controls the amount of air blown by the primary combustion firing fan 25a based on the atmospheric temperature of the primary combustion region R2 detected by the temperature sensor 28b. The amount of air blown by the primary combustion fan 25a coincides with the amount of primary combustion air supplied from the air supply port 25c to the primary combustion region R2 of the carbonization furnace 20. Therefore, the carbonization furnace control unit 29 can adjust the amount of primary combustion air blown to the primary combustion region R2 by controlling the amount of air blown by the primary combustion fan 25a. .

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

  Next, a method for controlling the blown amount of the secondary combustion fan 26a by the carbonization furnace control unit 29 will be described with reference to the flowchart of FIG. The carbonization furnace control unit 29 controls the amount of air blown by the secondary combustion fan 26a based on the combustion gas temperature Tg detected by the temperature sensor 28a. The amount of air blown by the secondary combustion fan 26a matches the amount of air for secondary combustion supplied to the secondary combustion region R4 of the carbonization furnace 20 from the air supply port 26c. Therefore, the carbonization furnace control unit 29 can adjust the amount of secondary combustion air 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 the combustion state suitable for burning the combustible gas contained in the combustion gas in the secondary combustion firing region R4 is maintained. The amount of air blown by the secondary combustion fan 26a is controlled. Specifically, the carbonization furnace control unit 29 controls the amount of air blown by the secondary combustion fan 26a according to the flowchart shown in FIG. Each process in the flowchart shown in FIG. 9 is a process performed when a calculation unit (not shown) included in the carbonization furnace control unit 29 executes a control program stored in a storage unit (not shown).

  Prior to the process shown in the flowchart of FIG. 9, when the carbonization furnace control unit 29 starts combustion of the organic waste in the carbonization furnace 20, the organic waste is generated by the ignition burner 20 c and accumulated in the gap 20 a. Start burning. Thereafter, the carbonization furnace control unit 29 starts blowing external air (atmosphere) by the secondary combustion fan 26a. The carbonization furnace control unit 29 controls the secondary combustion fan 26a so that the air flow rate is constant until the combustion gas temperature Tg detected by the temperature sensor 28a becomes equal to or higher than the first combustion firing gas temperature Tg1. Each process shown in the flowchart of FIG. 9 is started after the combustion gas temperature Tg detected by the temperature sensor 28a becomes equal to or higher than the first combustion gas temperature Tg1.

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

In step S800, the carbonization furnace control unit 29 receives the temperature detection signal transmitted from the temperature sensor 28a.
The combustion burning gas temperature Tg which is the temperature of the combustion gas discharged | emitted from the combustion gas discharge part 27 is detected.

  In step S801, the carbonization furnace control unit 29 determines whether or not the combustion gas temperature Tg detected by the temperature sensor 28a is lower than the first combustion gas temperature Tg1. If it is determined that the combustion gas temperature Tg is lower than the first combustion firing gas temperature Tg1, the carbonization furnace control unit 29 proceeds to step S802, otherwise proceeds to step S803.

  In step S802, the carbonization furnace control unit 29 transmits a control signal for reducing the blown amount of the secondary combustion fan 26a to the secondary combustion fan 26a. The secondary combustion fan 26a reduces the blown air volume in response to receiving the control signal from the carbonization furnace control unit 29. Here, when it is determined that the combustion gas temperature Tg is lower than the first combustion gas temperature Tg1, the blowing amount of the secondary combustion fan 26a is decreased for the following reason.

  The amount of secondary combustion air that the secondary air supply unit 26 supplies to the secondary combustion region R4 is a fixed amount rather than the amount that causes complete combustion of the combustible gas contained in the combustion gas present in the secondary combustion region R4. A large amount is preferable. That is, the excess air ratio in the secondary combustion region R4 is preferably set to a constant value larger than 1.0.

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

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

  If it does so, the combustion efficiency of the combustible gas in secondary combustion area | region R4 will deteriorate, and the combustion gas which contains much combustible gas will be discharged | emitted from the combustion gas discharge part 27. FIG. The combustible gas contains polymer hydrocarbons which are components that solidify to become tar. Therefore, if a large amount of components that solidify into combustible gas and become tar remains contained, the carbonization furnace 20 and equipment installed downstream thereof may be damaged. For this reason, it is desirable that a large amount of components that solidify into the combustion gas and become tar are not included, and damage to the carbonization furnace 20 and equipment installed downstream thereof is desirably suppressed. Therefore, when the carbonization furnace control unit 29 determines that the combustion gas temperature Tg is lower than the first combustion gas temperature Tg1, the secondary combustion is performed in order to reduce the amount of surplus air supplied to the secondary combustion region R4. The air volume of the fan 26a is reduced.

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

  In step S804, the carbonization furnace control unit 29 transmits a control signal for increasing the blowing amount of the secondary combustion fan 26a to the secondary combustion fan 26a. The secondary combustion fan 26a increases the blown air volume in response to receiving the control signal from the carbonization furnace control unit 29. When the process of the flowchart shown in FIG. 9 is completed, the carbonization furnace control unit 29 starts executing the process shown in FIG. 9 again. Here, when it is determined that the combustion gas temperature Tg is higher than the second combustion gas temperature Tg2, the blowing amount of the secondary combustion fan 26a is increased for the following reason.

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

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

  As described above, the carbonization furnace control unit 29 controls the amount of air blown by the secondary combustion fan 26a based on the combustion gas temperature Tg detected by the temperature sensor 28a, so that the combustion gas temperature Tg is the first. It is made to become more than combustion gas temperature Tg1 and below the 2nd combustion gas temperature Tg2. Here, as the first combustion gas temperature Tg1 and the second combustion gas temperature Tg2, for example, the first combustion gas temperature Tg1 can be set to 900 ° C., and the second combustion gas temperature Tg2 can be set to 1300 ° C.

  The reason why the first combustion gas temperature Tg1 is set to 900 ° C. is that most of the polymer hydrocarbons can be removed from the combustion gas by maintaining the temperature of the secondary combustion region R4 at 900 ° C. or higher. . The polymer hydrocarbon is a component that solidifies into a tar in the combustible gas contained in the combustion gas. Therefore, by removing most of the polymer hydrocarbons from the combustion gas, it is possible to suppress damage to the carbonization furnace 20 and equipment installed downstream 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 decreases the blowing amount when the combustion gas temperature Tg is lower than the first combustion gas temperature Tg1, and increases the blowing amount when the combustion gas temperature Tg is higher than the second combustion gas temperature Tg2. The secondary combustion fan 26a is controlled so as to cause this to occur.

  Next, a method for controlling the rotational speed of the turntable 24a by the carbonization furnace control unit 29 will be described with reference to the flowchart of FIG. Each process in the flowchart shown in FIG. 10 is a process performed when a calculation unit (not shown) included in the carbonization furnace control unit 29 executes a control program stored in a storage unit (not shown).

  In the flowchart shown in FIG. 10, the carbonization furnace control unit 29 controls the discharge amount of the carbide discharged by the carbide discharge unit 24. In the present embodiment, the amount of carbide discharged by the carbide discharge unit 24 is controlled because the input of the organic waste from the organic waste input unit 23 to the gap 20a is stopped. This is to prevent the temperature of the carbide discharged from 24 from rising.

  When the amount of organic waste deposited in the gap 20a is gradually reduced, the carbide refining / cooling region R1 for extinguishing the carbide gradually becomes narrower. In this case, if the rotation speed of the turntable 24a is maintained constant, the carbide is discharged from the lower end of the gap 20a in a state where the carbide is not sufficiently cooled. This is because the carbide that has been carbonized in the primary combustion region R2 to a high temperature is not sufficiently cooled in the carbide refining / cooling region R1. Then, the carbonization furnace control part 29 adjusts the temperature of the carbide | carbonized_material discharged | emitted by the carbide | carbonized_material discharge | emission part 24 by controlling the discharge | emission amount of the carbide | carbonized_material discharged | emitted by the carbide | carbonized_material discharge part 24. FIG.

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

  Hereinafter, each step of the flowchart of FIG. 10 will be described. In step S900, the carbonization furnace control unit 29 receives the temperature detection signal transmitted from the temperature sensor 28c, thereby detecting the carbide temperature Tc, which is the temperature of the carbide deposited on the lower end side of the gap 20a. In step S901, the carbonization furnace control unit 29 receives the accumulation amount detection signal transmitted from the level sensor 28d, and thereby detects the accumulation amount Ao that is the accumulation amount of the organic waste deposited on the immediate side 20a.

  In step S902, 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. When determining that the detected carbide temperature Tc is equal to or higher than the first carbide temperature Tc1, the carbonization furnace control unit 29 proceeds to step S903, and otherwise proceeds to step S904. Here, as 1st carbide | carbonized_material temperature Tc1, arbitrary temperature of the range of 250 degreeC or more and 300 degrees C or less can be set, for example.

  In step S903, the carbonization furnace control unit 29 controls the driving unit 24b to rotate the rotation speed of the turntable 24a at the second rotation speed Rs2. The second rotation speed Rs2 is lower than the first rotation speed Rs1 described later. Here, the first rotation speed Rs1 is a speed for discharging the amount of carbide necessary for the carbonization furnace 20 to maintain the normal operation state from the carbide discharge portion 24. In step S903, the rotational speed of the turntable 24a is set to the first speed so that the temperature of the carbide discharged by the carbide discharge unit 24 is lowered when the carbide temperature Tc detected by the temperature sensor 28c is equal to or higher than the first carbide temperature Tc1. The second rotation speed Rs2 is lower than the rotation speed Rs1. By reducing the rotation speed of the turntable 24a, the time for which the carbide stays in the carbide refining / cooling region R1 becomes longer, and accordingly, the temperature of the carbide discharged by the carbide discharge portion 24 decreases.

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

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

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

  When the process of the flowchart shown in FIG. 10 is completed, the carbonization furnace control unit 29 starts executing the process shown in FIG. 10 again. In this way, the carbonization furnace control unit 29 is configured so that the drive unit 24b rotates the turntable 24a based on the carbide temperature Tc detected by the temperature sensor 28c and the organic waste accumulation amount Ao detected by the level sensor 28d. To control.

  In the flowchart shown in FIG. 10 above, the rotational speed of the turntable 24a is switched in two steps depending on whether or not the carbide temperature Tc detected by the temperature sensor 28c is equal to or higher than the first carbide temperature Tc1. Other embodiments may be used. For example, the rotational speed of the turntable 24a may be switched in two or more stages according to the carbide temperature Tc. Further, for example, the rotational speed of the turntable 24a may be controlled so as to be a speed inversely proportional to the carbide temperature Tc detected by the temperature sensor 28c without switching the rotational speed of the turntable 24a stepwise.

  Further, in the flowchart shown in FIG. 10, the rotation speed of the turntable 24a is switched in two steps depending on whether or not the accumulation amount Ao detected by the level sensor 28d is equal to or greater than the first accumulation amount Ao1. However, other embodiments may be used. For example, the rotation speed of the turntable 24a may be switched in a plurality of stages of two or more stages according to the accumulation amount Ao. Further, for example, the rotational speed of the turntable 24a may be controlled so as to be a speed proportional to the accumulation amount Ao detected by the level sensor 28d without switching the rotational speed of the turntable 24a stepwise.

  In the flowchart shown in FIG. 10, the rotational speed of the turntable 24a is controlled using both the carbide temperature Tc detected by the temperature sensor 28c and the accumulation amount Ao detected by the level sensor 28d. Other embodiments may be used. For example, the rotational speed of the turntable 24a may be controlled using either the carbide temperature Tc detected by the temperature sensor 28c or the deposition amount Ao detected by the level sensor 28d.

  Next, an embodiment of the main body of the pyrolysis furnace 30 suitable for the water gas generator A-2 of the hydrogen gas generation system constituting the hydrogen station system of the present invention will be described in detail with reference to FIGS. . FIG. 11 is a longitudinal sectional view of the main body of the pyrolysis furnace 30 shown in FIG. In FIG. 11, the axis Z indicates the vertical direction (gravity direction) orthogonal to the installation surface (not shown) on which the pyrolysis furnace 30 is installed.

  As shown in FIG. 11, the pyrolysis furnace 30 of the present embodiment includes a main body 31, a reaction tube 32, a reaction tube head 33 (supply portion), a water gas outlet nozzle 34 (water gas outlet portion), Combustion gas supply part 35 (heating gas supply part), combustion gas discharge part 36 (heating gas discharge part), gland packing 37 (first seal part), gland packing 38 (second seal part), And a gland packing 39 (third seal portion).

  The main body 31 is a member formed in a substantially cylindrical shape extending along the axis Z. The main body 31 forms a space for accommodating the reaction tube 32 therein. The main body 31 is attached to a metal (for example, iron) housing 31a that forms the exterior of the pyrolysis furnace 30, a heat insulating material 31b that is attached to the inner peripheral surface of the housing 31a, and an inner peripheral surface of the heat insulating material 31b. And a heat-resistant material 31c.

  The upper surface of the substantially cylindrical main body 31 is composed of an upper plate 31d that is annular in plan view, and the bottom surface of the main body 31 is composed of a bottom plate 31e that is annular in plan view. An upper end flange 31g (first flange portion) is provided at the upper end of the side surface 31f of the main body 31, and a lower end flange 31i (second flange portion) is provided at the lower end of the side surface 31f of the main body 31. Yes.

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

  The reaction tube 32 is a mechanism formed in a substantially cylindrical shape extending along the axis Z. The reaction tube 32 has an outer peripheral surface 32 d that forms a combustion gas flow path 30 a for allowing a combustion gas (heating gas) to flow between the inner peripheral surface of the main body 31. The reaction tube 32 includes a center pipe 32a (tubular member), an upper end flange 32b (third flange portion), a plurality of first inclined plates 32f, a plurality of second inclined plates 32g, and a plurality of holding rods 32h (holding portions). ).

  As shown in FIG. 10, the upper end flange 32 b of the reaction tube 32 and the end of the center pipe 32 a on the upper end flange 32 b side protrude upward from the upper plate 31 d (upper surface) of the main body 31. Further, the lower end portion 32 c of the reaction tube 32 protrudes downward from the bottom plate 31 d (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 is housed a thermal decomposition promotion mechanism including a plurality of first inclined plates 32f, a plurality of second inclined plates 32g, and a plurality of holding rods 32h (holding portions). The thermal decomposition promotion mechanism is a mechanism that promotes the thermal decomposition reaction between the carbide and superheated steam by guiding the carbide stepwise from the upper end side to the lower end side of the center pipe 32a and retaining the carbide in the reaction tube 32. .

  As shown in FIGS. 11 and 12, the plurality of first inclined plates 32f and the plurality of second inclined plates 32g are held by the four holding bars 32h at a plurality of locations along the axis Z. The first inclined plates 32f and the second inclined plates 32g are alternately arranged along the axis Z. The upper ends of the four holding rods 32 h are attached to the lower surface of the lower end flange 33 a of the reaction tube head 33. By releasing the fastening between the upper end flange 32b of the reaction tube 32 and the lower end flange 33a of the reaction tube head 33, the thermal decomposition promoting mechanism can be removed (detached) upward from the center pipe 32a.

  The first inclined plate 32f shown in FIG. 12 (a) has the carbide in one end (the left end in FIG. 12 (a)) of the inner peripheral surface 32e of the reaction tube 32 and the other end (in FIG. 12 (a)). It is arranged so as to form a first inclined surface that is inclined so as to be led to the first opening 32i provided at the right end). Further, the second inclined plate 32f shown in FIG. 12 (b) has one end portion (FIG. 12 (b)) from the other end portion (the right end portion in FIG. 12 (b)) of the carbide 32 to the carbide. It is arranged so as to form a second inclined surface that is inclined so as to be led to the second opening 32j provided at the left end portion in the middle.

  As shown in FIG. 11, the first inclined surface formed by the first inclined plate 32f is inclined so as to guide the carbide falling from the second opening 32j downward, and the second inclined plate 32g forms the second inclined surface. The inclined surface is inclined so as to guide the carbide falling from the first opening 32i downward. In this manner, the thermal decomposition promoting mechanism guides the carbide stepwise from the upper end side to the lower end side of the center pipe 32a using the first inclined plates 32f and the second inclined plates 32g that are alternately arranged along the axis Z. be able to.

  The inclination angle of the first inclined surface and the second inclined surface with respect to the plane orthogonal to the axis Z can be arbitrarily set according to the properties of the carbide, but in order to reliably move the carbide along the inclined surface, the carbide. It is preferable that the angle be equal to or greater than the angle of repose. On the other hand, if the inclination angle is too large, the residence time of the carbide in the reaction tube 32 is shortened, and the thermal decomposition reaction is not sufficiently promoted. Therefore, it is particularly preferable that the inclination angle of the first inclined surface and the second inclined surface with respect to the plane orthogonal to the axis Z is determined to be equal to or greater than the repose angle of the carbide in the range of 20 ° to 60 °.

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

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

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

  The combustion gas supply unit 35 is an opening that is provided above the main body 31 and supplies the combustion gas guided from the combustion gas channel 200a to the combustion gas channel 30a. The combustion gas discharge unit 36 is an opening that is provided below the main body 31 and discharges the combustion gas from the combustion gas channel 30a to the combustion gas channel 200b. The combustion gas supplied from the combustion gas supply part 35 to the combustion gas flow path 30a flows from the upper end side to the lower end side of the center pipe 32a while heating the outer peripheral surface 32d of the center pipe 32a, and is discharged from the combustion gas discharge part 36. Is done.

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

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

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

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

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

  As shown in FIG. 13, the gland packing 39 includes an annular packing member 39a, an annular packing member 39b, and a packing pressing member 39c. By fastening the packing pressing member 39c to the bottom plate 31e with fastening bolts, the packing member 39a and the packing member 39b contract in the axis Z direction and expand in the radial direction perpendicular to the axis Z. As the gland packing 39 expands in the radial direction, the inner peripheral surface 39d of the gland packing 39 comes into contact with the outer peripheral surface 32d of the reaction tube 32 and the outer peripheral surface 34a of the water gas outlet nozzle 34, thereby forming a seal region.

  Subsequently, referring to FIG. 14, a pyrolysis furnace 30, a desuperheater 40, a cyclone 50, a steam generator 80, suitable for the water gas generator A-2 of the hydrogen gas generation system constituting the hydrogen station system of the present invention, An embodiment of the steam superheater 81 and its peripheral devices will be described in detail. As shown in FIG. 14, 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 101 a is a device that conveys the carbide discharged from the carbonization furnace 20. The screw conveyor 101a accommodates a screw in a linearly extending cylindrical body. The screw conveyor 101a conveys the carbide along the extending direction of the cylinder by rotating the screw inside the cylinder by the driving force of the motor.

  The clinker removing device 101b is a device that removes clinker having a particle size of a certain size or more from the carbide discharged from the screw conveyor 101a by a net or the like. The carbide from which the clinker is removed is conveyed to the magnetic separator 101d by the belt conveyor 101c. The magnetic separator 101d is a device that removes iron scraps such as nails contained in carbide with a magnet. The carbide from which the iron scrap has been removed is supplied to the screw conveyor 101e.

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

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

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

  The nitrogen replacement device 30b is a device constituting the pyrolysis furnace 30, and is a device for replacing oxygen contained in the air supplied from the screw conveyor 101f together with the carbide with inert nitrogen gas. The nitrogen purger 30b is disposed on the upper side connected to the screw conveyor 101f and the lower side connected to the reaction tube head 33, and is an electric control valve (for example, a ball valve) whose open / close state is controlled by the control device 90. ).

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

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

  After the inside of the nitrogen purger 30b has been replaced with nitrogen gas, the control device 90 switches the control valve below the nitrogen purger 30b to the open state to transfer the carbide from the nitrogen purger 30b to the reaction tube head 33. Supply. After supplying carbide to the reaction tube head 33 from the nitrogen purger 30b, the controller 90 closes the control valve below the nitrogen purger 30b. Further, the control device 90 then opens the control valve above the nitrogen purger 30b and supplies new carbide into the nitrogen purger 30b.

  As described above, the control device 90 controls the opening and closing of the control valves above and below the nitrogen purger 30b, so that the gas supplied to the reaction tube head 33 together with the carbide is nitrogen gas. This nitrogen gas is an inert gas that does not react with the water gas generated in the reaction tube 32. For this reason, it is possible to suppress the reduction of the yield of the water gas due to the reaction between the oxygen and the water gas due to the supply of the air containing the acid cord together with the carbide to the reaction tube 32.

  The char recovery device 41 includes a nitrogen purger 41a and a char recovery unit 41b. The nitrogen replacer 41a is a device for replacing the water gas supplied from the temperature reducer 40 together with the unreacted portion of the carbide with inert nitrogen gas. The char recovery unit 41b is an apparatus that recovers an unreacted portion of the carbide and supplies the unreacted component to a nitrogen purger 30b from a supply path (not shown). The nitrogen purger 41a is disposed on the upper side connected to the temperature reducer 40 and the lower side connected to the char recovery unit 41b, and is an electric control valve (for example, a ball) whose opening / closing state is controlled by the control device 90. Valve).

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

  Nitrogen gas is always supplied to the nitrogen purger 41a from a device that generates nitrogen gas such as an air separation device. Therefore, when the upper and lower control valves of the nitrogen purger 41a are closed and a certain period of time has elapsed, the water gas supplied into the nitrogen purger 41a together with the unreacted portion of the carbide is discharged to the outside, and the interior becomes nitrogen. The gas is replaced. In addition, the water gas discharged | emitted from the nitrogen purge device 41a is supplied to a flare stack (illustration omitted), and a combustion process is carried out.

  After the inside of the nitrogen purger 41a is replaced with nitrogen gas, the control device 90 switches the control valve below the nitrogen purger 41a to the open state, and the carbide is transferred from the nitrogen purger 41a to the char recovery unit 41b. The unreacted portion is supplied. After supplying the unreacted portion of the carbide from the nitrogen purger 41a to the char recovery unit 41b, the control device 90 closes the control valve below the nitrogen purger 41a. In addition, the control device 90 then opens the control valve above the nitrogen purger 41a and supplies new unreacted carbon carbide into the nitrogen purger 41a.

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

  The residue collection device 51 includes a nitrogen purger 51a and a residue collection unit 51b. The nitrogen replacer 51a is a device for replacing the water gas supplied from the cyclone 50 together with the residue with inert nitrogen gas. The residue collection unit 51b is a device that collects the residue discharged from the nitrogen purger 51a.

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

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

  The steam generator 80 includes a steam generation unit 80a and a steam circulation tank 80b. The steam generator 80a includes a heat transfer tube (not shown) that circulates water that exchanges heat with the combustion gas, and a jacket (not shown) that is provided in a cylindrical body that is formed so as to cover the heat transfer tube. Abbreviation). Water is supplied to the heat transfer tube and the jacket from the steam circulation tank 80b.

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

  Finally, the dryer suitable for the organic waste supply apparatus A-1 of the hydrogen gas generation system constituting the hydrogen station system of the present invention and its peripheral devices will be described with reference to FIG. The dryer 10 is a dryer of a type called a rotary kiln, and includes a combustion gas introduction unit 10b, a rotating body 10c, and a discharge unit 10d. The combustion gas introduction part 10b introduces the combustion gas supplied from the combustion gas flow path 200d into the dryer 10 and introduces the introduced combustion gas into the rotary body 10c.

  The rotating body 10c is a cylindrical member formed in a direction extending along the axis W, and rotates about the axis W by being given rotational power by a drive motor. Moreover, organic waste is supplied into the inside of the rotary body 10c from the raw material supply path 11a. The organic waste supplied to the inside of the rotating body 10c is guided toward the discharge unit 10d while being dried by the combustion gas guided from the combustion gas introduction unit 10b. The organic waste is directly heated by the combustion gas while being stirred by the rotation of the rotating body 10c, and is conveyed by the flow of the combustion gas from one end to the other end of the rotating body 10c.

  The discharge unit 10d collects the organic waste dried while being conveyed by the rotating body 10c and supplies it to the raw material supply path 10a. The organic waste supplied to the raw material supply path 10 a is supplied to the carbonization furnace 20 via the hopper 12. Further, the discharge unit 10d supplies the combustion gas introduced from the combustion gas introduction unit 10b through the inside of the rotating body 10c to the combustion gas channel 200e. The combustion gas supplied to the combustion gas flow path 200e is supplied to the exhaust gas cooling and cleaning device 13.

  The operation and effect of the hydrogen station system according to the embodiment of the present invention described above will be described respectively.

  In the on-line type hydrogen station system of the present invention, a hydrogen gas generation system A and a hydrogen gas supply system B are directly connected via a pressure control device C and a flow rate control device D. Hydrogen that uses fuel generated from petroleum complex to produce hydrogen by purifying water gas obtained by pyrolyzing the carbide generated by partial combustion with superheated steam using organic waste as biomass as fuel Unlike the hydrogen gas generation system using the manufacturing method, there is no need to be adjacent to the oil complex installed in the coastal area away from the house, and there are no restrictions on the location conditions. That is, an on-site gas station directly connected to a hydrogen gas supply system that supplies hydrogen to a fuel cell vehicle can be constructed.

  In addition, the pressure control device C and the flow rate control device D provided between the pressure accumulator B-2 and the organic waste supply device A-1 control the supply amount of the organic waste according to the hydrogen supply amount. Unnecessary operation of the hydrogen gas generation system can be suppressed.

  Therefore, the transportation cost of hydrogen gas is unnecessary, and there is no need to provide a special device for storing raw materials for producing hydrogen, and the operating rate of the hydrogen production facility according to the amount of hydrogen supplied to the fuel cell vehicle can be achieved. Therefore, it is not necessary to store a large amount of hydrogen gas, and a hydrogen station system with no overall loss can be constructed.

  In addition, the heat and carbide obtained by directly burning organic waste derived from biological resources is converted into water gas and hydrogen is extracted, so that the earth's material circulation system is not destroyed. Hydrogen can be produced using energy that does not use depleting resources such as uranium, and it can greatly contribute to the construction of a recycling-oriented social structure that leads to reuse and reduction of waste.

  In particular, the water gas generator A-2 of the present invention has high combustion efficiency, the carbonization furnace 20 having high carbonization efficiency that discharges the carbide whose temperature of the burned carbide is appropriately reduced, and the outflow of the heating gas. Since it uses the thermal decomposition furnace 30 that is suppressed and the thermal decomposition reaction proceeds rapidly, it is possible to more efficiently generate a water gas having a higher purity, the hydrogen purification is easy, and the hydrogen is efficiently generated. Is manufactured, and a hydrogen gas generation system suitable for the hydrogen station system can be constructed.

  Hereinafter, this point will be described in detail.

  First, the carbonization furnace 20 is a conventional problem, that is, 1) a liquid (“tar”) that solidifies with cooling and has a high viscosity contained in a combustible gas generated by partial combustion of organic waste. 2) Problems with polymer hydrocarbons, 2) Insufficient cooling of carbides produced by partial combustion of organic waste, damage to carbide transport mechanisms, and ignition due to contact between exhausted carbides and air This solves the problems and 3) the problem of the carbonization efficiency of the carbide generated by partial combustion of the organic waste, and it is possible to stably supply the high-quality carbide to the pyrolysis furnace 30.

  Therefore, in the carbonization furnace 20, the carbonization furnace control unit 29 controls the rotation speed of the turntable 24a according to the temperature of the carbide detected by the temperature sensor 28b and the level sensor 28d, and the carbide discharge unit 24 discharges to the outside. By optimizing the amount of carbide discharged, the carbide is sufficiently cooled in the carbide refining / cooling region R1, and in an appropriately cooled state, the carbide is discharged from the lower end of the gap 20a, and the carbide touches the air. Eliminates the problem of fire again.

  Further, the carbonization furnace 20 heats the air blown by the primary combustion fan 25a by the heat radiating fins 25e, and supplies the heated air to the gap 20a from the air supply port 25c. Since the supplied air is heated by the radiation fins 25e, it is possible to suppress a decrease in the atmospheric temperature of the primary combustion region R2 as compared with the case where the air supplied to the gap 20a is not heated. It is possible to improve the carbonization efficiency of the organic waste material while supplying external air as the combustion air.

  Secondly, the pyrolysis furnace has a conventional problem, that is, the combustion gas generated in the carbonization furnace supplied to the gap between the outer cylinder and the inner cylinder and the outside of the water gas generated in the pyrolysis furnace. This is a solution to the problem of spilling into the water and the problem of the yield of water gas. It is possible to efficiently convert high-quality carbide supplied from the carbonization furnace 20 into water gas having a high hydrogen gas concentration (high purity). Can be generated.

  Therefore, the pyrolysis furnace 30 includes a gland packing 37 provided so as to be in contact with the upper plate 31d below the upper plate 31d of the main body 31, and a bottom plate 31e above the bottom plate 31e of the main body 31. And a gland packing 38 having an inner peripheral surface 38 d that contacts the outer peripheral surface 32 d of the reaction tube 32. As a result, when the reaction tube 32 in which the pyrolysis reaction is performed inside is thermally expanded by the combustion gas flowing between the main body portion 31 and the outer surface 32d of the upper surface 31d of the main body portion 31 and the reaction tube 32, The combustion gas is prevented from flowing out from the gap, and the combustion gas is prevented from flowing out from the gap between the bottom plate 31e of the main body 31 and the outer peripheral surface 32d of the reaction tube 32. In addition, the various packings described in the embodiments can be used in combination to prevent the combustion gas from flowing out and to efficiently generate the water gas.

  Further, the pyrolysis furnace 30 is provided with a combustion gas supply part 35 for supplying combustion gas to the combustion gas flow path 30a above the main body 31, and a combustion gas discharge part 36 for discharging the combustion gas from the combustion gas flow path 30a. The reaction tube 32 constituting the pyrolysis furnace 30 is further provided with a center pipe 32a formed in a cylindrical shape extending along the axis Z, and housed therein and supplied from the upper end. A plurality of first inclined plates 32f and a plurality of second inclined plates 32g that promote the thermal decomposition reaction between the carbide and the superheated steam by guiding the carbides from the upper end to the lower end portion 32c step by step, and a plurality of these holding plates It has a thermal decomposition promotion mechanism consisting of a holding rod 32h. As a result, the time during which the carbide stays in the reaction tube 32 becomes longer, and accordingly, the thermal decomposition reaction is promoted and the yield of the water gas is improved.

  Further, the char that is discharged from the water gas outlet nozzle 34 of the pyrolysis furnace 30 to the outside of the pyrolysis furnace 39 is recovered and supplied again to the reaction tube head 33 of the pyrolysis furnace 30. A recovery device 41 is provided, and the unreacted carbide recovered by the char recovery device 41 is thermally decomposed again, thereby further improving the yield of the water gas.

  Thus, since the water gas generator A-2 of the present invention supplies the water gas to the hydrogen purifier A-3 efficiently, stably and with high purity, the hydrogen gas is efficiently produced. The

  On the other hand, the organic waste supply device A-1 and the water gas generation device A-2 constituting the hydrogen gas generation system A of the present invention are used as a problem of the conventional water gas generation system, that is, as a gasifying agent for carbides. Since a dedicated heat source is used as a heat source that generates superheated steam and a heat source that dries organic waste, it solves the problem of low thermal efficiency of the entire system. As a result, the productivity of the hydrogen station system can be increased and the cost of hydrogen gas can be reduced.

  Therefore, first, the water gas generator A-2 is configured as follows. The carbonization furnace 20 partially burns organic waste to generate carbides and combustion gases, and the carbides are supplied to the reaction tube head 33 of the pyrolysis furnace 30 and reacted together with superheated steam supplied to the reaction tube head 33. The pipe 32 is supplied into the center pipe 32a from the upper end side of the center pipe 32a. On the other hand, the combustion gas discharged from the carbonization furnace 20 to the combustion gas flow path 200a is supplied to the combustion gas supply port 35 of the pyrolysis furnace 30 while maintaining a high temperature. The combustion gas supplied from the combustion gas supply port 35 to the combustion gas flow path 30a is guided downward while heating the upper end side of the center pipe 32a of the reaction tube 32, and is combusted from the combustion gas discharge port 36 on the lower end side of the center pipe 32a. It is discharged to the channel 200b. Thus, since the inside of the reaction tube 32 is maintained at a high temperature by the combustion gas, the thermal decomposition reaction between the carbide and the superheated steam is promoted therein, and the yield of the water gas can be improved.

  Further, the combustion gas used for promoting the pyrolysis reaction in the pyrolysis furnace 30 is used as a heat source for the steam superheater 81 and then used as a heat source for the steam generator 80. The steam superheater 81 generates superheated steam having a temperature equal to or higher than the saturation temperature by heating the saturated steam generated by the steam generator 80 at an equal pressure, and the steam generator 80 is configured to convert water that is liquid. Heating produces saturated water vapor. Therefore, since the steam superheater 81 requires a heat source having a temperature higher than that of the steam generator 80, the steam is generated from the liquid water by supplying the combustion gas to the steam generator 80 after the steam superheater 81. It can be heated to produce superheated steam and supplied to the pyrolysis furnace 30 as a gasifying agent. Therefore, by generating superheated steam that has been raised to an appropriate temperature by the steam superheater 90, even if the temperature of the superheated steam decreases in the pyrolysis furnace 30 due to a thermal decomposition reaction (endothermic reaction), the steam is decomposed in the pyrolysis furnace 30. Since the combustion gas used for promoting the pyrolysis reaction in the pyrolysis furnace 30 is also used as a heat source for generating superheated steam from water, Compared with the case where a dedicated heat source is used as a heat source for generating steam, the overall thermal efficiency of the water gas generator A-2 can be improved.

  Next, the combustion gas used as a heat source for generating water vapor by the steam generator 80 is also supplied to the dryer 10 by the combustion gas flow path 200d in the organic waste supply apparatus A-1, and the woody biomass is supplied. It is used to reduce the water content of organic waste such as. Compared with the case where a dedicated heat source is used as a heat source for drying organic waste, the thermal efficiency of the entire water gas generation system 100 can be improved.

  Even more preferably, the combustion gas discharged from the carbonization furnace 20 is used as a heat source for the pyrolysis furnace 30, the steam superheater 81, the steam generator 81, and the dryer 10, and then the exhaust gas cooling and cleaning device 13 is used. Supplied to. The exhaust gas cooling and cleaning device l3 needs to lower the temperature of the combustion gas in order to discharge the combustion gas into the atmosphere, but the temperature of the combustion gas supplied to the exhaust gas cooling and cleaning device 13 dries the organic waste. Since it is used as a heat source and is in a sufficiently lowered state, the exhaust gas cooling and cleaning device 13 can be manufactured at low cost.

  Thus, the thermal decomposition reaction in the pyrolysis furnace 30 can be promoted without using a dedicated heat source for generating superheated steam used as a carbide gasifying agent, and the water gas generation system 100 is provided. can do. At the same time, the combustion gas is used as a heat source for drying the organic waste, and can improve the overall thermal efficiency of the organic waste supply device A-1 and the water gas generation device A-2. Can be manufactured at low cost.

  As described above, the hydrogen gas generation system A according to the present invention has a high combustion efficiency, a carbonization furnace having a high carbonization efficiency that discharges carbides whose temperature of the burned carbides has been appropriately reduced, and the outflow of the heating gas is suppressed. By applying a pyrolysis furnace in which a decomposition reaction proceeds, and a combustion gas flow path that can effectively use combustion gas generated in a carbonization furnace, high-purity water gas can be efficiently generated. In addition, since hydrogen gas can be efficiently separated by the hydrogen purifier, a hydrogen gas generation system preferable for the hydrogen station system can be provided.

  The on-line hydrogen station system of the present invention can be installed in the same manner as a gasoline station for refueling gasoline and diesel vehicles, and can be used as a fuel refueling station for fuel cell vehicles. It can also be used as a fuel replenishment (hydrogen supply) system when expanded to railway vehicles, jet aircraft, ships, industrial vehicles, and the like. Furthermore, it can be used as a hydrogen supply system when a hydrogen power generation system using a fuel cell is also used in industrial / commercial facilities and power generation facilities.

A Hydrogen gas generation system A-1 Organic waste supply device including wood chips A-2 Hydrogen gas generation device A-3 Hydrogen purification device B Hydrogen gas supply system B-1 Compressor B-2 Pressure accumulator B-3 Dispenser B -4 Filling device C Pressure control device D Flow rate control device 10 Dryer 20 Carbonization furnace 20a Gap 21 Body portion 22 Cylindrical portion (cylinder portion)
23 Organic waste input section (input section)
24 Carbide discharge part 24a Turntable (rotary body)
24b Drive unit 24c Carbide discharge port (discharge port)
24d Clinker Crusher 25 Primary air supply unit (first air supply unit)
25a Primary combustion fan (air blower)
25b Cover part 25c Air supply port 25d Closed space 25e Radiation fin (heating part)
26 Secondary air supply unit (second air supply unit)
26a Secondary combustion fan 26b Cover part 26c Air supply port 26d Closed space 27 Combustion gas discharge part 28a, 28b, 28c Temperature sensor (temperature detection part)
28d Level sensor (deposition amount detector)
29 Carbonization furnace control unit (control unit)
30 Pyrolysis furnace 30a Combustion gas passage (heating gas passage)
31 Main body 32 Reaction tube 32a Center vip (tubular member)
32b Top flange (third flange)
32c Lower end portion 32f First inclined plate 32g Second inclined plate 32h Holding rod (holding portion)
33 Reaction tube head (supply unit)
33a Bottom flange (4th flange)
33d Fastening bolt (fastening member)
34 Water gas outlet nozzle (water gas outlet)
35 Combustion gas supply section (heating gas supply section)
36 Combustion gas discharge part (heating gas discharge part)
DESCRIPTION OF SYMBOLS 40 Temperature reducer 41 Char collection device 60 Water gas cooling device 70 Water gas holder 80 Steam generator 81 Steam superheater 82 Water supply device 90 Control device 100 Water gas generation system 102,103,104 Water gas supply path 200a, 200b, 200c , 200d, 200e Combustion gas flow path R1 Carbide refining / cooling region R2 Primary combustion region R3 Raw material input region R4 Secondary combustion region W, X, Y, Z axes

Claims (5)

An organic waste supply device including wood chips,
A water gas generator that generates water gas by heating the carbide generated by partial combustion of the organic waste supplied from the organic waste supply device together with water vapor; and
A hydrogen gas generation system comprising: a hydrogen purification device for producing hydrogen by removing impurities from the water gas generated by the water gas generation device;
A compressor for bringing the hydrogen produced by the hydrogen gas generation system to a predetermined pressure;
A pressure accumulator for storing hydrogen brought to a predetermined pressure by the compressor;
A hydrogen gas supply system comprising a dispenser for supplying the hydrogen while controlling the flow rate and pressure of the hydrogen stored in the pressure accumulator,
Between the organic waste supply device and the pressure accumulator,
A pressure control device that controls the pressure of the pressure accumulator that varies with the amount of hydrogen consumed, and that indicates the supply amount of the organic waste according to the change;
A hydrogen station system comprising: a flow rate control device that controls the supply amount of the organic waste according to the instruction. In the hydrogen station system, the hydrogen gas generation system includes:
A carbonization furnace for partially burning the organic waste to generate the carbide and combustion gas;
A pyrolysis furnace for generating the water gas by heating the carbide produced by the carbonization furnace together with steam with the combustion gas;
A steam generator for generating water vapor by heating water with the combustion gas;
A steam superheater that superheats the steam generated by the steam generator with the combustion gas and supplies the steam that has been superheated to the pyrolysis furnace;
A dryer for drying the organic waste with the combustion gas and supplying the dried organic waste to the carbonization furnace;
An exhaust gas cooling and cleaning device for removing harmful substances from the combustion gas discharged from the dryer to render them harmless;
The combustion gas generated by the carbonization furnace is supplied to the pyrolysis furnace, the combustion gas discharged from the pyrolysis furnace is supplied to the steam superheater, and the combustion gas discharged from the steam superheater is Combustion gas flow path for supplying to the steam generator, supplying the combustion gas discharged from the steam generator to the dryer, and supplying the combustion gas discharged from the dryer to the exhaust gas cooling and cleaning device When,
A char recovery device that recovers unreacted carbide discharged from the pyrolysis furnace and supplies the unreacted carbide again to the pyrolysis furnace;
A temperature reducer for cooling the water gas generated in the pyrolysis furnace;
A cyclone for removing residues from the water gas supplied from the temperature reducer;
A residue collection device for collecting the residue removed by the cyclone;
A water gas cooling device for cooling the water gas from which the residue is removed by the cyclone;
The hydrogen station system according to claim 1, further comprising: a water gas holder that stores the water gas cooled by the water gas cooling device. In the hydrogen station system, the carbonization furnace includes:
A main body formed in a cylindrical shape extending along the axis;
A cylindrical portion having an outer peripheral surface which is formed in a cylindrical shape extending along the axis and which forms a gap for carbonizing the organic waste between the inner peripheral surface of the main body portion;
A charging unit for charging the organic waste into the gap formed by the main body and the tube;
An air supply section for supplying combustion air for the organic waste deposited in the gap formed by the main body section and the cylinder section;
A combustion gas discharge unit for discharging combustion gas generated by the combustion of the organic waste;
A carbide discharge part for discharging carbide formed by burning the organic waste from the gap formed by the main body part and the cylinder part;
The hydrogen station system of Claim 2 provided with the carbonization furnace control part which controls the combustion conditions of the said organic waste. In the hydrogen station system, the carbonization furnace includes:
A main body formed in a cylindrical shape extending along the axis;
A cylindrical portion having an outer peripheral surface which is formed in a cylindrical shape extending along the axis and which forms a gap for carbonizing the organic waste between the inner peripheral surface of the main body portion;
A charging unit for charging the organic waste into the gap formed by the main body and the tube;
A carbide discharge part for discharging carbide formed by carbonization of the organic waste from the gap formed by the main body part and the cylinder part;
A first air supply section for supplying primary combustion air for partially burning the organic waste deposited in the gap formed by the main body section and the cylinder section;
A second air supply unit for supplying secondary combustion air for burning a combustible gas contained in a combustion gas generated by the combustion of the organic waste to the inside of the main body unit;
A combustion gas discharge part for discharging the combustion gas;
A combustion gas temperature detection unit for detecting the temperature of the combustion gas discharged from the combustion gas discharge unit;
A primary combustion region temperature detector for detecting the temperature of the atmosphere in the primary combustion region;
A carbide temperature detecting unit for detecting a temperature of the carbide deposited on the lower end side of the gap formed by the main body part and the cylinder part;
A deposition amount detection unit that detects a deposition amount of the organic waste deposited in the gap formed by the main body and the cylindrical portion;
The primary combustion region temperature detected by the primary combustion region temperature detector, the combustion gas temperature detected by the combustion gas temperature detector, the carbide temperature detected by the carbide temperature detector, and the deposit amount detector Each of the first air supply unit, the second air supply unit, and a carbonization furnace control unit that controls the discharge amount of the carbide discharged by the carbide discharge unit according to the amount of deposition to be performed. The hydrogen station system according to claim 2. In the hydrogen station system, the pyrolysis furnace comprises:
A main body formed in a cylindrical shape extending along the axis;
It has an outer peripheral surface that is formed in a cylindrical shape extending along the axis and forms a heating gas passage for circulating a heating gas between the inner peripheral surface of the main body, and the upper end is the A reaction tube protruding from the upper surface of the main body,
A supply unit configured to supply the carbide and the water vapor to the inside of the reaction tube in order to generate the water gas inside the reaction tube;
A heating gas supply unit that is provided above the main body and supplies the heating gas to the heating gas channel;
A water gas outlet that is attached to the lower end of the reaction tube and guides the water gas generated by the pyrolysis reaction of the carbide inside the reaction tube to the outside;
A heating gas discharge part which is provided below the main body part and discharges the heating gas from the heating gas flow path;
The carbide contained in the reaction tube and supplied from the upper end of the reaction tube is led stepwise from the upper end side to the lower end side of the reaction tube to promote the thermal decomposition reaction of the carbide and water vapor. A mechanism for promoting thermal decomposition;
The inner surface is provided below the upper surface of the main body so as to be in contact with the upper surface, and has an inner peripheral surface that contacts the outer peripheral surface of the reaction tube, and is configured to block outflow of the heating gas from the upper surface of the main body. 1 seal part;
The lower end portion of the reaction tube protrudes from the bottom surface of the main body portion, and is provided so as to be in contact with the bottom surface above the bottom surface of the main body portion and has an inner peripheral surface that contacts the outer peripheral surface of the reaction tube. ,
A second seal portion for blocking outflow of the heating gas from the bottom surface of the main body portion;
At the mounting position of the lower end portion of the reaction tube and the water gas outlet portion, it has an inner peripheral surface that comes into contact with each of the outer peripheral surface of the reaction tube and the outer peripheral surface of the water gas outlet portion. The hydrogen station system according to any one of claims 2 to 4, further comprising a third seal portion that blocks outflow of the water gas from the water.

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