TW201741446A - Biomass gasifier device - Google Patents

Abstract

The present invention provides an apparatus for producing hydrogen-containing gas from biomass, which optimizes a biomass pyrolysis temperature and a pyrolysis gas reforming temperature, and may reduce problems due to tar. The present invention relates to an apparatus for gasifying biomass comprising a biomass pyrolyzer, a pyrolysis gas reformer and a pyrolysis gas introduction pipe, wherein the biomass pyrolyzer and the pyrolysis gas reformer further comprise an introduction port and an exhaust port for a heat carrier, biomass pyrolysis and pyrolysis gas reforming are performed by heat of the heat carrier, wherein the biomass pyrolyzer and the pyrolysis gas reformer are arranged in parallel, for both of the biomass pyrolyzer and the pyrolysis gas reformer, the pyrolysis gas introduction pipe is arranged on a side surface of a vessel and below an upper surface of a heat carrier layer formed inside the biomass pyrolyzer and the pyrolysis gas reformer, respectively, and the pyrolysis gas introduction pipe is arranged horizontally.

Description

Biomass gasification unit

The present invention relates to a biomass gasification device, and more particularly to a biomass thermal decomposition device having thermal decomposition of biomass, and mixing the gas generated in the biomass thermal decomposition device with steam for upgrading. A gasification device for the thermal decomposition of a gas reformer.

As a result of the Great East Japan Earthquake that occurred on March 11, 2011, the operation of multiple nuclear power generation equipment was stopped according to safety and other viewpoints. As a result, there is a fear of insufficient power supply. As a substitute for nuclear power generation, power generation equipment such as solar power generation, wind power generation, geothermal power generation, hydroelectric power generation, tidal power generation, and biomass power generation are attracting attention.

Under such circumstances, the Japanese government decided at the cabinet meeting on April 11, 2014, the "Fourth Energy Basic Plan", which mainly decided to accelerate the introduction of renewable energy and expand the decentralized energy system such as fuel cell technology. popular. In addition, the "Renewable Version of the Hydrogen and Fuel Cell Strategy Blueprint", which was compiled on March 22, 2016, incorporates the use of hydrogen derived from renewable energy sources to study technical and economic issues.

Solar power generation, wind power generation, and tidal power generation in renewable energy are expected as temporary power supply sources. However, since power generation is unstable, it cannot be expected as a stable power supply equipment. In addition, hydropower and tidal power generation are small-scale The plan can expect a certain degree of demand, but there is a problem of limited installation space due to the construction of large-scale equipment.

On the other hand, biomass such as wood, sewage sludge, and livestock excreta are evenly distributed in Japan. In particular, due to the collapse of houses caused by the Great East Japan Earthquake and the destruction of forests, there have been a large number of woody biomass such as woody waste materials in construction, fallen trees in forests, abandoned forest farms, and thin wood. . It is expected that these woody biomass can be effectively utilized as a renewable energy source.

In a gasification device for woody biomass, for example, a gasification device for raw biomass (Patent Document 1) is proposed, and the gasification device for the biomass is provided with a gasifier, which is a gas of a vertical type. The upper part of the furnace is supplied with biomass, and a filling and moving layer of the raw material is formed in the gasification furnace, and a gasifying agent is supplied from the lower part of the gasification furnace to lower the biomass and rise in the filling moving layer. The gas is convectively contacted and thermally decomposed to obtain a gas to be produced, and the gasification device of the biomass has a vibrating sieve which classifies the biomass to obtain a weight ratio of the fine particles of the biomass below the predetermined particle diameter to a predetermined value. The following particle size distribution adjusts the biomass; and a biomass supply device that supplies the particle size distribution adjusted biomass from the shaker to the gasifier. According to the gasification apparatus, an upward flow of uniform high-temperature gas can be formed in the filling moving layer, and pressure loss in the filling moving layer can be reduced, so that stable gasification can be maintained. However, there is no guarantee that the supplied biomass is thermally decomposed uniformly. Further, since the particle size distribution adjustment raw material must be obtained as described above, it is necessary to provide a device for this purpose, resulting in high cost.

There is proposed a biomass gasification apparatus (Patent Document 2) comprising: a thermal decomposition unit in the form of an external thermal rotary crucible, which indirectly heats raw material biomass to thermally decompose to produce a tar-containing component a thermally decomposed gas and carbon; and a gasification portion for the pyrolysis gas containing the tar component extracted from the thermal decomposition portion and Carbon, an oxidizing gas is introduced, the tar component is thermally decomposed, and carbon is gasified. The apparatus is characterized in that after the biomass is thermally decomposed, the tar and carbon contained in the pyrolysis gas are burned and removed by the oxidizing gas. However, the equipment is not only complicated, but also complicated in operation. Further, when the tar is burned, there is a fear that a part of the fuel gas is also burned and lost. As another apparatus, for example, there is proposed a thermal decomposition gasification system (Patent Document 3), which has a carbonization device for carbonizing sewage sludge or woody biomass, and includes and includes a carbonization device. The high-temperature gasification unit in which the carbide gas is gasified and the two-stage gasification furnace in which the gas reforming unit of the flammable thermal decomposition gas containing tar is volatilized during the formation of the carbide is modified. This thermal decomposition gasification system is complicated not only by having a carbonization apparatus but also a two-stage gasification furnace, and the operation operation is complicated. Further, when the tar is burned, there is a fear that a part of the fuel gas is also burned and lost.

As a gasification method of an organic substance such as woody biomass, a method of using a heat carrier medium (heat carrier) has been disclosed. For example, a method for producing a product gas having a high calorific value from an organic substance and a mixture of substances has been proposed (Patent Document 4), which is a method of manufacturing a high calorific value from an organic substance and a mixture of substances, and making the cycle The heat carrier medium is passed through a heating belt, a reaction belt, a thermal decomposition zone, and a separation step, and then returned to the heating belt. At this time, the organic substance or substance mixture is contacted with the heated heat carrier medium in the thermal decomposition zone. And separating into a solid carbon-containing residue and a thermal decomposition gas as a volatile phase, and after passing through the thermal decomposition zone, separating the solid carbon-containing residue from the heat-carrying medium in the separation step, and separating the thermally decomposed gas and Mixing water vapor as a reaction medium to heat the product gas having a higher calorific value by exchanging part of the heat contained in the heated heat carrying medium in the reaction zone And the method is to decompose water vapor in a thermal decomposition zone The gas is mixed, and the carbon residue of all the solids is supplied to another combustion device, where it is burned, so that the hotter exhaust gas of the combustion device passes through the deposition of the heat carrier medium existing in the heating belt. Most of the sensible heat is imparted to the heat carrying medium. In the method, after leaving the thermal decomposition reactor, the mixture containing the thermal decomposition coke and the heat carrier medium is separated, and the obtained thermal decomposition coke is burned in a combustion device, thereby utilizing the sensible heat generated thereby. The heat carrier medium is heated in the tropics, whereby the product gas having a high calorific value is obtained at a low cost. Moreover, this method is characterized in that each of the tandem connection type and the parallel connection type can be configured by independently providing a thermal decomposition device having a thermal decomposition zone and a gas reformer having a reaction zone. By. Further, in order to maintain the heating efficiency of the heat-carrying medium (heat carrier) in the preheater of the heating belt and to stabilize the quality of the generated gas, a system for designing the preheater in the above method has been proposed ( Patent Document 5). However, even in such methods and systems using a heat-carrying medium (heat carrier), failure due to tar generated during thermal decomposition cannot be sufficiently avoided.

[Previous Technical Literature] [Patent Literature]

Patent Document 1: Japanese Patent Laid-Open Publication No. 2011-231193

Patent Document 2: Japanese Patent Laid-Open Publication No. 2007-177106

Patent Document 3: Japanese Patent Laid-Open No. 2011-68893

Patent Document 4: Japanese Patent Laid-Open Publication No. 2003-510403

Patent Document 5: Japanese Patent Laid-Open No. 2011-144329

The present invention provides a biomass gasification device which can optimize not only thermal decomposition but also thermal decomposition temperature of the biomass and the reforming temperature of the generated thermal decomposition gas. The amount of gas generated increases the production amount of the hydrogen-containing gas as the final product, and the amount of tar and coal dust generated can be reduced. Further, the present invention provides a biomass gasification device which efficiently gasifies the produced tar and efficiently recovers tar and coal dust remaining without gasification, thereby making it remarkable Reduce the failure of equipment caused by tar and coal dust.

In a conventional method of thermally decomposing biomass and modifying the generated thermal decomposition gas by using heat of a heat carrying medium (heat carrier), although the biomass is encapsulated in the heat carrier layer for heating, However, the biomass can be thermally decomposed relatively uniformly, but operational failures caused by tar and coal dust generated during thermal decomposition cannot be avoided. In the conventional method, the heat carrier is preheated to a predetermined temperature and then introduced into a pyrolysis gas reformer, where the heat carrier is in contact with the pyrolysis gas and steam introduced by the autothermal pyrolysis device, thereby thermally decomposing the gas. The steam is reformed and taken out as a product. On the other hand, after the heat carrier passes through the pipe and is lowered, it is introduced into the biomass pyrolysis reactor to generate thermal decomposition of the biomass. The gas generated by the thermal decomposition of the biomass is introduced into the thermal decomposition gas reformer after rising in the pipe. However, since the pyrolysis gas contains tar, coal dust, or the like, the tar, coal dust, and the like adhere to the inner wall of the introduction pipe and the valve to the thermal decomposition gas reformer, and may also convect the pyrolysis gas. The problem that the contact heat carrier is fixed and blocked in the pipe. In order to solve this problem, it is considered to increase the diameter of the introduction pipe. However, this means cannot be an essential solution even if it only extends the time until it blocks. Further, in order to solve the problem of clogging in the piping of the heat carrier, it is considered to provide a means for separately piping the heating decomposition gas and the heating carrier, but even if According to this means, it is also impossible to avoid a clogging failure due to adhesion of the inner wall of the pipe and the valve or the like which rises toward the heating decomposition gas such as tar or coal dust. Moreover, the method of arranging the separate pipes as such causes the device and the operation to be significantly complicated.

Further, in a conventional method of thermally decomposing biomass and reforming the generated gas by utilizing the heat of the heat carrying medium (heat carrier), the thermal decomposition gas reformer and the biomass thermal decomposition device are used. Since they are connected in series, it is not possible to individually control the temperatures inside the respective reactors, that is, the biomass pyrolysis reactor and the pyrolysis gas reformer. For example, when the thermal decomposition temperature of the raw material is lowered, there is a problem that the internal temperature of the biothermal pyrolyzer cannot be improved even if the thermal decomposition temperature is increased, and the internal temperature of the thermal decomposition gas reformer is maintained. In the case where the thermal decomposition temperature of the biomass is increased, even if the temperature inside the biothermal pyrolyzer is to be lowered, the temperature of the thermal decomposition gas reformer is maintained, and the thermal decomposition of the biomass cannot be performed. The internal temperature of the device is reduced. Therefore, it is not easy to continuously optimize the thermal decomposition temperature of the biomass and the reforming temperature of the generated thermal decomposition gas. Finally, there is a problem that the amount of thermal decomposition gas generated and the production amount of the hydrogen-containing gas of the final product are reduced. . Further, there is a problem that the amount of generation of tar, coal dust, and the like increases. It is reasonable to expect that the temperature control of the biothermal pyrolyzer and the thermal decomposition gas reformer can be performed individually.

Patent Document 4 proposes a method in which a biothermal pyrolyzer and a pyrolysis gas reformer are arranged side by side with respect to a flow of a heat carrier medium (heat carrier). According to this method, since the temperature of the biomass pyrolyzer and the temperature of the pyrolysis gas reformer can be individually controlled, the above problem can be solved. In this method, the thermal decomposition gas system generated by the biomass thermal decomposition device is introduced into the thermal decomposition gas reformer by means of a pipe at the upper portion of the pyrolysis thermal decomposition device. In the method of introducing the pyrolysis gas, there is a problem in that the tar and the coal dust adhere to the piping through which the pyrolysis gas rises and falls. The inner wall and the valve, etc., so that the resulting blocking failure cannot be avoided.

If the temperature of the biothermal pyrolyzer and the thermal decomposition gas reformer can be individually controlled, the thermal decomposition temperature of the biomass and the reforming temperature of the pyrolysis gas can be set to optimum values, respectively, so that it can be effectively The amount of tar and coal dust generated when the biomass is thermally decomposed is reduced, and the pyrolysis gas can be efficiently generated, and the generated pyrolysis gas can be efficiently modified under optimum conditions. Therefore, the adhesion of the tar, the coal dust, and the like to the inner wall of the pipe, the valve, and the like can be remarkably reduced, and the production amount of the reformed gas can be greatly increased. However, the device configuration described in Patent Document 4 can individually control the temperature of the pyrolysis thermodegrader and the pyrolysis gas reformer, but reforms the pyrolysis gas autogenic pyrolyzer to the pyrolysis gas. The thermal decomposition gas introduction pipe introduced into the device causes adhesion of tar and coal dust to the inner wall and the valve, and finally, a blockage failure of the thermal decomposition gas introduction pipe occurs.

Therefore, the inventors of the present invention individually control the internal temperature of each of the biomass pyrolyzer and the thermal decomposition gas reformer to appropriately set the thermal decomposition temperature of the biomass and the reforming temperature of the thermal decomposition gas. The value, not only increases the amount of thermal decomposition gas generated, but also increases the production amount of the hydrogen-containing gas as the final product, and reduces the amount of tar and coal dust generated, in addition, in order to avoid the adhesion of tar and coal dust to the heat of the biomass The thermal decomposition gas generated in the decomposer is introduced into the inner wall of the thermal decomposition gas introduction pipe of the thermal decomposition gas reformer, a valve, or the like, and the thermal decomposition gas introduction pipe is blocked, and the gasification device should be configured. I tried various studies.

As a result, it has been found that the biothermal pyrolyzer and the thermal decomposition gas reformer can be arranged side by side with respect to the flow of a plurality of granular materials and/or agglomerates [heat carrier medium (heat carrier)], and Introducing a thermal decomposition gas into the tube on both sides of the biomass pyrolysis reactor and the thermal decomposition gas reformer, and disposed in the biothermal decomposition device and the thermal decomposition gas reformer The surface of the thermal carrier layer on the upper surface of the thermal carrier layer and the side surface of the thermal decomposition gas reformer are disposed, and the thermal decomposition gas introduction pipe is set as a horizontal pipe to solve the above problem. That is, it has been found that by arranging the biothermal pyrolyzer and the pyrolysis gas reformer in parallel with the flow of the heat carrier, the internal temperature can be individually controlled, and the hot decomposition gas can be introduced into the gas suction port of the tube ( a gas inlet) and a gas introduction port (gas outlet) are disposed in the heat carrier layer, and the heat carrier in the biomass pyrolyzer and the thermal decomposition gas reformer is introduced into the thermal decomposition gas introduction pipe, and then The thermally decomposed gas is introduced into the heat carrier layer held in the tube by the pyrolysis gas, and tar, coal dust, and the like are efficiently removed, and the tar is efficiently thermally decomposed. Further, it has been found that the heat carrier intruding into the thermal decomposition gas introduction pipe is accompanied by the top-down movement of the heat carrier in the biomass pyrolysis device and the thermal decomposition gas reformer in order. By replacing this, the heat carrier does not cause clogging of the heat carrier due to tar or the like in the thermal decomposition gas introduction pipe, and the tar and coal dust are remarkably efficiently removed, and the tar is thermally decomposed, preferably modified. Further, it has been found that it is preferable to prevent the heat carrier flowing in the biomass pyrolyzer and the pyrolysis gas reformer from being thermally decomposed more effectively by projecting the bottom surface of the thermal decomposition gas introduction pipe upward. The gas introduction pipe flows into the other container, and the heat carrier in the thermal decomposition gas introduction pipe is effectively replaced, so that tar, coal dust, and the like can be removed more efficiently.

That is, the present invention relates to (1) a biomass gasification device comprising: a biomass pyrolysis device having a raw material supply port, a non-oxidizing gas supply port, and/or a steam injection port; and a pyrolysis gas; a reformer having a steam injection inlet and a reformed gas discharge port; and a thermal decomposition gas introduction pipe that introduces the pyrolysis gas generated in the biomass pyrolysis device to the thermal decomposition gas reformer, and is equipped with The above-mentioned biomass thermal decomposition device and the above thermal decomposition gas reformer Further, the biomass pyrolyzer and the pyrolysis gas reformer further include an introduction port and a discharge port of a plurality of granular materials and/or blocks which are preheated, respectively, by the plurality of particles The heat of the substance and/or the mass of the mass, and the thermal decomposition of the biomass and the modification of the thermal decomposition gas generated by the thermal decomposition of the biomass; the gasification device of the above biomass is characterized in that And the thermal decomposition gas reformer and the pyrolysis gas reformer are arranged side by side with respect to the flow of the plurality of granular materials and/or the mass, and the thermal decomposition gas introduction pipe is connected to the biomass thermal decomposition device and the above The two sides of the thermal decomposition gas reformer are disposed on the upper surface of the plurality of granular and/or block layers respectively formed in the biomass pyrolysis device and the thermal decomposition gas reformer The side of the biomass pyrolyzer and the pyrolysis gas reformer, and the pyrolysis gas introduction pipe is disposed substantially horizontally with respect to the direction of gravity.

(2) The gasification device according to the above (1), wherein the inner bottom surface of the pyrolysis gas introduction pipe has a structure that protrudes upward; (3) as described above (1) In the gasification device of the above-mentioned thermal decomposition gas introduction pipe, the inner bottom surface of the pyrolysis gas introduction pipe has a structure in which both sides of the pyrolysis thermodegrader and the pyrolysis gas reformer protrude upward toward the center portion; (4) The gasification device according to the above (1), wherein the inner bottom surface of the pyrolysis gas introduction pipe has 5 to 45 degrees to the center portion of both sides of the pyrolysis thermodegrader and the pyrolysis gas reformer. (5) The gasification device of the above-mentioned (1), wherein the inner bottom surface of the pyrolysis gas introduction pipe has two types of a pyrolysis thermal decomposition device and a thermal decomposition gas reformer. (6) The gasification device of the raw material of the above (1), wherein the thermal decomposition gas is introduced The inner bottom surface of the tube has a structure in which both sides of the autothermal pyrolyzer and the thermal decomposition gas reformer protrude upward from the center portion with a slope of 15 to 25 degrees; (7) as in the above (1) to (6) The gasification device of any one of the above, wherein the thermal decomposition gas introduction pipe is substantially circular or substantially polygonal outside a cross section perpendicular to the longitudinal direction (flow direction of the thermal decomposition gas); (8) as described above ( The gasification device of the raw material according to any one of (1), wherein the pyrolysis gas introduction pipe has a substantially quadrangular shape in a direction perpendicular to a longitudinal direction (a flow direction of the pyrolysis gas); (9) The gasification device according to any one of the above (1) to (8), wherein the pyrolysis gas introduction pipe is provided with 1 to 3; (10) as in the above (1) to (8) A biomass gasification device, wherein the thermal decomposition gas introduction pipe is provided with one or two; (11) a biomass gasification device according to any one of the above (1) to (10), wherein The pyrolysis gas introduction pipe retains the plurality of granules and/or lumps in the interior thereof; (12) as in any one of the above (1) to (11) The gasification device of the raw material, wherein the steam injection inlet is provided in one or more selected from the group consisting of a free biomass pyrolysis reactor and its vicinity, a pyrolysis gas reformer and its vicinity, and a thermal decomposition gas introduction pipe. (13) The biomass gasification apparatus according to any one of (1) to (11) above, wherein the steam injection inlet is provided in or near the biomass pyrolysis reactor, and the thermal decomposition gas reformer And a biomass gasification device according to any one of the above (1) to (11), wherein the steam injection port is in the vicinity of the biomass pyrolysis reactor , the thermal decomposition gas reformer or its vicinity, and the thermal decomposition gas introduction pipe are respectively equipped with 1~3; (15) The biomass gasification apparatus according to any one of (1) to (11) above, wherein the steam injection port is in the vicinity of the biomass pyrolysis reactor, the thermal decomposition gas reformer, or the vicinity thereof, And a biomass gasification device according to any one of the above (1) to (15), wherein the plurality of granules and/or blocks are used. The preheating preheater is further provided on the upper portion of the biomass pyrolyzer and the thermal decomposition gas reformer; (17) the biomass gasification device according to any one of (1) to (16) above, Wherein, the inlets of the plurality of granules and/or lumps are disposed above the biomass pyrolyzer and the pyrolysis gas reformer; (18) as in any one of the above (1) to (16) a biomass gasification device, wherein the inlet ports of the plurality of granular materials and/or blocks are provided on top of a biomass pyrolysis reactor and a pyrolysis gas reformer; (19) as described above (1) The gasification device of any one of (18), wherein the discharge ports of the plurality of granular materials and/or blocks are disposed below the biomass thermal decomposition device and the thermal decomposition gas reformer; (20) The gasification apparatus of any of the above-mentioned (1) to (18), wherein the discharge ports of the plurality of granular materials and/or masses are provided in a biomass thermal decomposition device and a thermal decomposition gas reforming (21) The biomass gasification device according to any one of (1) to (20) above, wherein the granules and/or lumps are selected from the group consisting of metal balls and ceramic balls. (22) The gasification device of the above-mentioned (21), wherein the metal ball is made of stainless steel, and (23) the gasification device of the above (21), wherein the ceramic ball system comprises Selecting one or more materials selected from the group consisting of alumina, ceria, tantalum carbide, tungsten carbide, zirconium oxide and tantalum nitride; (24) The gasification apparatus of the raw material according to any one of the above (1) to (23) wherein the gas phase temperature of the biomass pyrolyzer is 400 to 700 ° C; (25) as described above (1) The biomass gasification device according to any one of (23), wherein the gas phase temperature of the biomass pyrolyzer is 500 to 700 ° C; (26) any one of the above (1) to (23) The biomass gasification device, wherein the gas phase temperature of the biomass pyrolyzer is 550 to 650 ° C; (27) the biomass gasification device according to any one of (1) to (26) above, The gasification device of the above-mentioned thermal decomposition gas reformer is a gasification device of any one of the above (1) to (26), wherein the pyrolysis gas is modified The gasification device of the biomass of any one of the above (1) to (26), wherein the gas phase temperature of the pyrolysis gas reformer is (30) The biomass gasification device according to any one of (1) to (29), wherein the biomass is selected from the group consisting of plant biomass, biological biomass, and living mixed. Biomass resources in a group of food and food waste .

Moreover, the present invention is a method for gasification of a biomass using a biomass gasification device according to the above (1). That is, the present invention is the method (31) of a method for gasification of a biomass, which is provided with a biomass pyrolyzer which heats a raw material in a non-oxidizing gas atmosphere or a mixed gas atmosphere of a non-oxidizing gas and steam. And a pyrolysis gas reformer that heats the gas generated in the biomass pyrolyzer in the presence of steam, and puts a plurality of pre-heated particles and/or cakes into the biomass The thermal decomposition device and the thermal decomposition gas reformer perform thermal decomposition of biomass and thermal decomposition gas generated by thermal decomposition of biomass by using heat of the plurality of granular materials and/or masses a modified gasification method, and The plurality of granules and/or lumps are individually supplied to the above-described biomass pyrolyzer and the pyrolysis gas reformer which are arranged side by side with respect to the flow of the plurality of granules and/or lumps And the pyrolysis gas generated in the biomass pyrolysis device is introduced into the pyrolysis gas reformer through a pyrolysis gas introduction pipe, and the pyrolysis gas introduction pipe is connected to the biomass pyrolysis device and the above The two sides of the thermal decomposition gas reformer are disposed on the upper surface of the plurality of granular and/or block layers respectively formed in the biomass pyrolysis device and the thermal decomposition gas reformer The side of the above-described biothermal pyrolyzer and the above-described pyrolysis gas reformer are arranged substantially horizontally with respect to the direction of gravity.

The gasification method of the raw material of the above-mentioned (31), wherein the inner bottom surface of the pyrolysis gas introduction pipe has a structure that protrudes upward; (33) as described above (31). The gasification method of the raw material, wherein the inner bottom surface of the pyrolysis gas introduction pipe has a structure in which both sides of the autothermal decomposition machine and the thermal decomposition gas reformer protrude upward toward the center portion; (34) The gasification method of the raw material according to the above (31), wherein the inner bottom surface of the pyrolysis gas introduction pipe has 5 to 45 degrees toward the center portion of both sides of the pyrolysis thermodegrader and the thermal decomposition gas reformer. (35) The gasification method of the raw material of the above-mentioned (31), wherein the inner bottom surface of the pyrolysis gas introduction pipe has two of a pyrolysis thermal decomposition device and a thermal decomposition gas reformer. (36) The gasification method of the raw material of the above-mentioned (31), wherein the inner bottom surface of the pyrolysis gas introduction tube has autothermal decomposition And thermal decomposition gas reformer a structure in which both sides of the center portion protrude upward from a slope of 15 to 25 degrees toward the center portion; (37) The gasification method of the raw material according to any one of the above (31) to (36), wherein the thermal decomposition gas introduction pipe is formed to be perpendicular to a longitudinal direction (flow direction of the thermal decomposition gas) The gasification method of the raw material of any one of the above-mentioned (31) to (36), wherein the thermal decomposition gas introduction pipe is perpendicular to the longitudinal direction (the flow of the thermal decomposition gas) The gasification method of the raw material of any one of the above-mentioned (31) to (38), wherein the thermal decomposition gas introduction pipe is provided with 1 to 3; The method of gasification of a biomass according to any one of the above (31), wherein the pyrolysis gas introduction pipe is provided with 1 or 2; (41) as described above (31) to (40) The method for gasification of any of the above, wherein the pyrolysis gas introduction pipe retains the plurality of granules and/or lumps therein; (42) as in the above (31) to (41) The gasification method of any one of the raw materials, wherein the steam injection inlet is provided in the vicinity of the free biomass thermal decomposition device, the thermal decomposition gas reformer, and the attachment thereof And a method of gasification of a biomass according to any one of the above (31) to (41), wherein the steam injection system is Equipped with a biomass pyrolysis reactor or its vicinity, a thermal decomposition gas reformer or its vicinity, and a pyrolysis gas introduction pipe; (44) a gasification of the biomass according to any one of the above (31) to (41) The method, wherein the steam injection inlet is in the vicinity of the biomass pyrolysis reactor, the thermal decomposition gas reformer or the vicinity thereof, and the thermal decomposition gas introduction pipe are respectively provided with 1 to 3; (45) as described above (31) The method of gasification of the raw material of any one of (41), wherein the steam injection inlet is from or near the biothermal decomposition machine, the thermal decomposition gas reformer or its attachment And a method for gasification of a biomass according to any one of the above (31) to (45), wherein a plurality of granules and/or Or a preheating preheater of the block is further provided on the upper part of the biomass pyrolyzer and the pyrolysis gas reformer; (47) the gasification of the biomass according to any one of the above (31) to (46) The method, wherein the inlets of the plurality of granules and/or blocks are disposed above the biomass pyrolyzer and the pyrolysis gas reformer; (48) as in (31) to (46) above A method for gasification of a biomass, wherein the inlets of the plurality of granules and/or blocks are provided on top of a biomass pyrolysis reactor and a pyrolysis gas reformer; (49) as described above ( The gasification method of the raw material of any one of the above-mentioned, wherein the plurality of granules and/or the block discharge port are provided in the raw material thermal decomposition device and the thermal decomposition gas reformer. (50) The gasification method of the raw material according to any one of the above (31) to (48), wherein the plurality of granules and/or the block discharge port are provided in the biomass thermal decomposition device And hot points The method of gasification of a biomass according to any one of the above (31) to (50), wherein the granules and/or lumps are selected from the group consisting of metal spheres and ceramics. (52) The gasification method of the raw material of the above (51), wherein the metal ball is made of stainless steel; (53) the gasification method of the raw material of (51) above, wherein the ceramic ball a material comprising one or more selected from the group consisting of free alumina, cerium oxide, tantalum carbide, tungsten carbide, zirconium oxide and tantalum nitride; (54) as in any one of the above (31) to (53) a gasification method of the biomass, wherein the gas phase temperature of the biomass pyrolysis device is 400 to 700 ° C; (55) The gasification method of the biomass according to any one of the above (31) to (53) wherein the gas phase temperature of the biomass pyrolyzer is 500 to 700 ° C; (56) as described above (31) The gasification method of the raw material of any one of (53), wherein the gas phase temperature of the above-mentioned biothermal pyrolyzer is 550 to 650 ° C; (57) any one of the above (31) to (56) The gasification method of the biomass, wherein the gas phase temperature of the pyrolysis gas reformer is 700 to 1,000 ° C; (58) the gasification method of the biomass according to any one of the above (31) to (56) The method of gasification of the biomass of any one of the above (31) to (56), wherein the pyrolysis gas is a gasification method of the above-mentioned thermal decomposition gas reformer The method of gasification of the biomass of any of the above-mentioned (31) to (59), wherein the above-mentioned biomass is free of plant biomass and organisms. It is a biomass resource selected from the group consisting of biomass, mixed living waste and food waste.

The present inventors have conceived the idea of introducing a pyrolysis gas introduction tube for introducing a pyrolysis gas generated in a biomass pyrolyzer into a thermal decomposition gas reformer, similarly to the configuration of the first device described above. That is, the gas suction port (gas inlet) of the pyrolysis gas introduction pipe is on the side of the biothermal decomposition device, and is disposed on the side of the biomass pyrolyzer which is located below the upper surface of the heat carrier layer formed in the biothermal separator. In the heat carrier layer, even if a plurality of granules and/or lumps [heat carrier medium (heat carrier)] are introduced only into the biomass pyrolyzer, the biomass is thermally decomposed and The generated thermal decomposition gas is introduced into a conventional heat exchanger type thermal decomposition gas reformer, and the modification of the thermal decomposition gas is performed, and the same effects as described above can be obtained. Therefore, the inventors of the present invention have carried out various studies on the configuration of the apparatus, and have found that even if the apparatus is configured, it is not inferior to the first apparatus configuration, and the object of the present invention can be solved.

That is, the present invention relates to (61) a biomass gasification device comprising: a biomass pyrolysis device having a raw material supply port, a non-oxidizing gas supply port, and/or a steam injection port; and a pyrolysis gas; a reformer having a steam injection inlet and a reformed gas discharge port; and a thermal decomposition gas introduction pipe that introduces the pyrolysis gas generated in the biomass pyrolysis device to the thermal decomposition gas reformer, and is equipped with The biothermal pyrolyzer is connected to the pyrolysis gas reformer; and the biothermal pyrolyzer further includes an inlet and a discharge port of a plurality of granular materials and/or blocks which are preheated, and The thermal decomposition of the biomass is performed by the heat of the plurality of granules and/or the lumps; on the other hand, the pyrolysis gas reformer further has a preheated gas on the outside or a flow path of a liquid heat medium, and a heat decomposition gas generated by thermal decomposition of the biomass is performed by heat of the heat medium, and the gasification device of the biomass is characterized in that the thermal decomposition is The gas introduction tube is attached to the above biomass heat The resolver side is provided on a side surface of the above-mentioned biomass pyrolyzer which is disposed below the upper surface of the plurality of granular materials and/or the bulk layer formed in the biomass pyrolysis device.

The gasification device of the above-mentioned (61), wherein the pyrolysis gas introduction pipe has the biomass pyrolysis device and the pyrolysis gas reformer. The biomass pyrolyzer side is disposed substantially horizontally with respect to the direction of gravity, and then rises upward toward the thermal decomposition gas reformer; (63) the gasification of the biomass as described in (61) above. In the apparatus, the pyrolysis gas introduction pipe is disposed substantially horizontally with respect to a gravity direction between the biomass pyrolysis device and the pyrolysis gas reformer, and an inner bottom surface of the pyrolysis gas introduction pipe has an upward direction Prominent structure; (64) The biomass gasification device according to the above (61), wherein the pyrolysis gas introduction pipe is substantially horizontally disposed between the biomass pyrolysis device and the pyrolysis gas reformer with respect to a gravity direction. Further, the inner bottom surface of the pyrolysis gas introduction pipe has a structure in which both sides of the pyrolysis thermodegrader and the pyrolysis gas reformer protrude upward toward the center portion with a slope; (65) the biomass of the above (61) The gasification device, wherein the pyrolysis gas introduction pipe is disposed substantially horizontally with respect to a gravity direction between the biomass pyrolysis device and the pyrolysis gas reformer, and an inner bottom surface of the pyrolysis gas introduction pipe a structure having a self-generating thermal decomposition device and a thermal decomposition gas reformer which protrude upward from the center portion at a slope of 5 to 45 degrees; (66) a biomass gasification device according to the above (61), wherein The thermal decomposition gas introduction pipe is disposed substantially horizontally with respect to the gravity direction between the biomass pyrolysis device and the thermal decomposition gas reformer, and the internal bottom surface of the thermal decomposition gas introduction pipe has a self The biomass thermal decomposition device and the thermal decomposition gas reformer have a structure in which the both sides of the thermal decomposition gas reforming device have a slope of 10 to 30 degrees toward the center portion; (67) the gasification device of the raw material of the above (61), wherein The pyrolysis gas introduction pipe is disposed substantially horizontally with respect to the gravity direction between the biomass pyrolyzer and the pyrolysis gas reformer, and the inner bottom surface of the pyrolysis gas introduction pipe has a self-generated thermal decomposition device and A gasification device of the biomass of any one of the above (61) to (67), wherein the both sides of the thermal decomposition gas reformer have a structure that protrudes upward from the center portion by a slope of 15 to 25 degrees, (68) Wherein the thermal decomposition gas introduction pipe is substantially circular or substantially polygonal except for a cross section perpendicular to the longitudinal direction (flow direction of the thermal decomposition gas); (69) as in any one of the above (61) to (67) Biomass gasification device, wherein The gasification device of the raw material of any one of the above (61) to (69), wherein the thermal decomposition gas introduction pipe is formed in a substantially quadrangular shape in a direction perpendicular to the longitudinal direction (flow direction of the thermal decomposition gas); The gasification device of the raw material of any one of the above-mentioned (61) to (69), wherein the pyrolysis gas introduction pipe is equipped with The gasification device of the raw material of any one of the above-mentioned (61) to (71), wherein the pyrolysis gas introduction pipe holds the plurality of granules and/or therein (73) The biomass gasification apparatus according to any one of the above (61) to (72), wherein the steam injection port is provided in the vicinity of the free biomass pyrolyzer and the thermal decomposition gas is modified. And a gasification device of any one of the above (61) to (72), wherein the steam is selected from the group consisting of: The injection inlet is provided at or near the biothermal decomposition machine, the thermal decomposition gas reformer or its vicinity, and the thermal decomposition gas introduction pipe; (75) The biomass gasification device according to any one of (61) to (72), wherein the steam injection port is in the vicinity of the biomass pyrolysis reactor, the thermal decomposition gas reformer or the vicinity thereof, and the thermal decomposition gas introduction The gasification device of the raw material of any one of the above-mentioned (61) to (72), wherein the steam injection port is in the vicinity of the biomass pyrolyzer or thermally decomposed The gas reformer or the vicinity thereof, and the pyrolysis gas introduction pipe are respectively provided with one; (77) a biomass gasification device according to any one of the above (61) to (76), wherein a granule and/or a block preheated preheater is further provided on the upper part of the biomass pyrolysis device; The gasification device of any of the above-mentioned (61) to (77), wherein the inlet of the plurality of granular materials and/or the mass is provided above the biomass pyrolyzer The gasification device of any of the above-mentioned (61) to (77), wherein the inlets of the plurality of granules and/or lumps are provided in a biomass thermal decomposition device. (80) The biomass gasification apparatus according to any one of the above (61) to (79), wherein the plurality of granules and/or the block discharge ports are provided in the biomass thermal decomposition device The gasification device of any of the above-mentioned (61) to (79), wherein the plurality of granules and/or the block outlets are provided for thermal decomposition of biomass The gasification device of any of the above-mentioned (61) to (81), wherein the granules and/or the lumps are selected from the group consisting of metal balls and ceramic balls. The gasification device of the above-mentioned (82), wherein the metal ball is made of stainless steel; (84) the gasification device of the above-mentioned (82), wherein the ceramic ball system contains free Alumina, cerium oxide, A gasification device of a biomass of any one of the above-mentioned (61) to (84), wherein The above-mentioned preheated gas-like or liquid-like heat medium is a high-temperature hot air; (86) The biomass gasification device according to any one of the above (61) to (85), wherein the biomass pyrolysis gas is The gasification device of the biomass of any one of the above (61) to (85), wherein the gas phase temperature of the biomass pyrolyzer is 500 to 700 ° C; (88) The biomass gasification apparatus according to any one of the above (61) to (85) wherein the gas phase temperature of the biomass pyrolyzer is 550 to 650 ° C; (89) as described above (61) The gasification device of any one of (88), wherein the pyrolysis gas reformer has a gas phase temperature of 700 to 1,000 ° C; (90) The gasification apparatus according to any one of the above (61) to (88), wherein the pyrolysis gas reformer has a gas phase temperature of 850 to 950 ° C; (91) as described above (61) The gasification apparatus of any one of (88), wherein the pyrolysis gas reformer has a gas phase temperature of 880 to 930 ° C; (92) as in the above (61) to (91) A biomass gasification device, wherein the biomass is selected from the group consisting of plant biomass, biomass biomass, living mixed emissions, and food waste.

Further, the present invention is a method for producing a biomass gasification method using the biomass gasification device of the above (61). In other words, the present invention provides a method for gasification of a biomass, which comprises a biomass pyrolyzer that heats the biomass in a non-oxidizing gas atmosphere or a mixed gas atmosphere of a non-oxidizing gas and steam, And a thermal decomposition gas reformer that heats the gas generated in the biomass pyrolyzer in the presence of steam, and puts a plurality of pre-heated particles and/or masses into the above-mentioned biomass heat The decomposer performs thermal decomposition of the biomass by the heat of the plurality of granules and/or the blocks; on the other hand, the preheated gas or liquid heat medium is passed through the heat Decomposing the flow path of the heat medium on the outer side of the gas reformer, and performing the modification of the thermal decomposition gas generated by the thermal decomposition of the biomass by the heat of the gas-like or liquid heat medium, the biomass In the gasification method, the pyrolysis gas generated in the biomass pyrolysis device is introduced into the thermal decomposition gas reformer through a pyrolysis gas introduction pipe, and the thermal decomposition gas introduction pipe system is provided in the gasification process. Biomass decomposition Wherein said plurality of particulate matter within and / or on the surface of the mass layer closer to the side surface of the biomass is below the thermal decomposition.

In a preferred embodiment, the gasification method of the raw material of the above (93), wherein the pyrolysis gas guide is used The inlet pipe has the above-mentioned biomass pyrolyzer side between the biomass pyrolysis device and the pyrolysis gas reformer, and is disposed substantially horizontally with respect to the gravity direction, and then laterally upward toward the pyrolysis gas reformer (95) The gasification method of the raw material according to the above (93), wherein the pyrolysis gas introduction pipe is between the biomass pyrolysis device and the pyrolysis gas reformer in relation to the gravity direction The internal surface of the thermal decomposition gas introduction pipe has a structure that protrudes upward; (96) The gasification method of the raw material of the above (93), wherein the pyrolysis gas introduction pipe is in the above-mentioned biomass The thermal decomposition device and the pyrolysis gas reformer are disposed substantially horizontally with respect to the gravity direction, and the inner bottom surface of the thermal decomposition gas introduction pipe has two sides of a pyrothermal pyrolyzer and a thermal decomposition gas reformer. (97) The method for gasification of a biomass according to the above (93), wherein the pyrolysis gas introduction pipe is in the biomass pyrolysis device and the heat The gas reforming device is disposed substantially horizontally with respect to the direction of gravity, and the inner bottom surface of the pyrolysis gas introduction pipe has 5 to 45 sides from the both sides of the autothermal decomposition device and the thermal decomposition gas reformer to the central portion. (98) The method for gasification of a biomass according to the above (93), wherein the pyrolysis gas introduction pipe is in the biomass pyrolysis device and the pyrolysis gas reformer The intermediate system is disposed substantially horizontally with respect to the direction of gravity, and the inner bottom surface of the pyrolysis gas introduction pipe has a slope of 10 to 30 degrees toward the center portion of both sides of the autothermal decomposition catalyst and the thermal decomposition gas reformer. (99) The gasification method of the raw material according to the above (93), wherein the pyrolysis gas introduction pipe is opposed to the pyrolysis gas reformer and the pyrolysis gas reformer The gravity direction is substantially horizontally disposed, and the inner bottom surface of the pyrolysis gas introduction pipe has a structure in which both sides of the pyrolysis thermodegrader and the pyrolysis gas reformer protrude upward toward the center portion with a slope of 15 to 25 degrees; (100) The gasification method of the raw material according to any one of the above-mentioned (93), wherein the thermal decomposition gas introduction pipe is formed to be perpendicular to a longitudinal direction (flow direction of the thermal decomposition gas) The gasification method of the raw material of any one of the above-mentioned (93) to (99), wherein the thermal decomposition gas introduction pipe is perpendicular to the longitudinal direction (the flow of the thermal decomposition gas) The gasification method of the raw material of any one of the above-mentioned (93) to (101), wherein the thermal decomposition gas introduction pipe is provided with 1 to 3; The gasification method of the biomass according to any one of the above (93), wherein the pyrolysis gas introduction pipe is provided with 1 or 2; (104) as described above (93) to (101) The gasification method of any of the above, wherein the pyrolysis gas introduction pipe is inside (105) A method for gasification of a biomass according to any one of the above (93) to (104), wherein the steam injection port is provided for free thermal decomposition One or more selected from the group consisting of the device and its vicinity, the pyrolysis gas reformer and its vicinity, and the pyrolysis gas introduction pipe; (106) as in any one of the above (93) to (104) a method of gasification of a biomass, wherein the steam injection port is provided in or near a biomass pyrolysis reactor, a thermal decomposition gas reformer or its vicinity, and a pyrolysis gas introduction pipe; (107) as described above (93) to ( 104) The method of gasification of a raw material according to any one of the preceding claims, wherein the steam injection port is in or near the biomass pyrolysis reactor, the thermal decomposition gas reformer or an attached thereto And a gasification method of the raw material of any one of the above-mentioned (93) to (104), wherein the steam injection port is thermally decomposed by the biomass. a gasification method of the biomass or the vicinity thereof, the thermal decomposition gas reformer or the vicinity thereof, and the thermal decomposition gas introduction pipe are respectively provided; (109) the biomass of any of the above (93) to (108) , wherein a preheater for preheating the plurality of granules and/or the block is further provided on the upper portion of the biomass pyrolyzer; (110) as in any one of the above (93) to (109) a method for gasification of a biomass, wherein the inlets of the plurality of granules and/or lumps are disposed above the biothermal pyrolyzer; (111) as in any one of the above (93) to (109) The gasification method of the raw material, wherein the inlets of the plurality of granules and/or lumps are provided on top of the biothermal pyrolyzer; (112) as in the above (93) to (111) A method for gasification of a biomass, wherein the discharge ports of the plurality of granules and/or lumps are disposed below the biothermal pyrolyzer; (113) as in the above (93) to (111) Any one a method for gasification of a biomass, wherein the discharge ports of the plurality of granules and/or lumps are provided at the bottom of the biothermal pyrolyzer; (114) as in any one of the above (93) to (113) The gasification method of the biomass, wherein the granules and/or the lumps are selected from the group consisting of metal spheres and ceramic spheres; (115) the gasification method of the biomass of (114) above, wherein (116) The method for gasification of a raw material according to (114) above, wherein the ceramic ball system comprises free alumina, cerium oxide, lanthanum carbide, tungsten carbide, zirconium oxide and tantalum nitride. The gasification method of the raw material of any one of the above-mentioned (93) to (116), wherein the preheated gas or liquid heat medium is High temperature hot air The gasification method of the raw material of any one of the above-mentioned (93) to (117), wherein the gas phase temperature of the above-mentioned biothermal pyrolyzer is 400 to 700 ° C; (119) as described above (93) The gasification method of the raw material of any one of (117), wherein the gas phase temperature of the above-mentioned biothermal pyrolyzer is 500 to 700 ° C; (120) any one of the above (93) to (117) The gasification method of the biomass, wherein the gas phase temperature of the biomass pyrolyzer is 550 to 650 ° C; (121) the gasification method of the biomass according to any one of the above (93) to (120), The method of gasification of the biomass of any one of the above-mentioned (93) to (120), wherein the pyrolysis gas is modified by the gasification method of the pyrolysis gas reformer. The method of gasification of a biomass of any one of the above-mentioned (93) to (120), wherein the gas phase temperature of the pyrolysis gas reformer is The method of gasification of a biomass according to any one of the above (93) to (123), wherein the above-mentioned biomass is a free plant biomass, a biomass biomass, and a living mixed discharge. And a group of food waste The biomass resources selected in the selection.

In the apparatus of the present invention, since the temperature of the biothermal pyrolyzer and the thermal decomposition gas reformer can be individually controlled, the thermal decomposition temperature of the biomass and the temperature of the thermal decomposition gas generated can be easily changed. And optimized for a long time. Thereby, not only the amount of generation of the pyrolysis gas but also the production amount of the hydrogen-containing gas as the final product can be increased, and the amount of tar and coal dust generated by thermal decomposition of the biomass can be reduced as much as possible. Further, the thermal decomposition gas generated in the biomass pyrolysis device is introduced into the gas suction port (gas inlet) of the thermal decomposition gas introduction pipe of the thermal decomposition gas reformer, and is disposed in the heat carrier layer of the biothermal decomposition machine. And the gas introduction port of the thermal decomposition gas introduction pipe Since the (gas outlet) is provided in the heat carrier layer of the thermal decomposition gas reformer, the heat carrier flows into the thermal decomposition gas introduction pipe, and the heat carrier is held in the thermal decomposition gas introduction pipe. Further, since the pyrolysis gas introduction pipe system is disposed substantially horizontally with respect to the gravity direction, the heat carrier in the thermal decomposition gas introduction pipe is generated, and the thermal decomposition gas and the thermal decomposition gas reformer are upwardly oriented. The replacement of the moving heat carrier and the avoidance of the heat carrier flowing into the thermal decomposition gas introduction pipe from the pyrolysis thermal decomposition device into the thermal decomposition gas reformer; on the other hand, the self-heating decomposition gas reformer can be avoided The heat carrier that has flowed into the thermal decomposition gas introduction pipe is mixed into the biothermal decomposition machine. Therefore, when the pyrolysis gas generated in the biomass pyrolyzer is introduced into the pyrolysis gas reformer through the pyrolysis gas introduction pipe, the tar and coal dust contained in the pyrolysis gas are efficiently captured by the heat carrier. Further, the tar is effectively gasified, and the residual tar and coal dust are kept attached to the heat carrier, and are released by the bottom of the pyrolysis thermodegrader and the pyrolysis gas reformer. Therefore, the malfunction of the device caused by the tar and the coal dust can be remarkably reduced, and the gasification rate of the produced tar can be maximized, thereby producing the hydrogen-containing gas according to the high thermal efficiency and the low-cost self-generating.

₁ , 1 ₁ , 1 ₂ ‧ ‧ preheater

2‧‧‧ Thermal decomposition gas reformer

3‧‧‧Biomass thermal decomposition machine

4‧‧‧ Raw material supply port

5‧‧‧Exhaust disposal device

6‧‧‧ Thermal decomposition residue (carbon) discharge

7‧‧‧Several granules and / or lumps [heat carrier medium (heat carrier)]

8‧‧‧Modified gas discharge

9‧‧‧ Thermal decomposition gas introduction tube

9-2‧‧‧The thermal decomposition gas introduction side gas inlet port (gas outlet) of the thermal decomposition gas introduction pipe

9-3‧‧‧The gas inlet (gas inlet) of the thermal decomposition device side of the thermal decomposition gas introduction pipe

10 ₁ , 10 ₂ ‧‧‧Hot media inlet and outlet

11 ₁ , 11 ₂ , 11 ₃ ‧ ‧ steam injection

12‧‧‧ Non-oxidizing gas supply port

13‧‧‧ Surfaces on the surface of several granular and/or bulk layers formed in the thermal decomposition reactor and the thermal decomposition gas reformer

g‧‧‧Flow direction of thermal decomposition gas

h‧‧‧The height of the protruding part of the bottom surface of the thermal decomposition gas introduction pipe

h ₁ ‧‧‧The width (height) of the vertical direction of the gas suction port of the thermal decomposition gas introduction pipe

h ₂ ‧‧‧The width (height) of the vertical direction of the gas inlet of the thermal decomposition gas introduction pipe

θ‧‧‧The angle of inclination of the inner bottom protrusion of the thermal decomposition gas introduction pipe

A‧‧‧ gasifier

B‧‧‧Electrical heater

C‧‧‧Electric heater

D‧‧‧Alumina ball (heat medium)

E‧‧‧Nick Catalyst

100‧‧‧Material supply piping

200‧‧‧ Thermal decomposition zone

300‧‧‧Modified area

400‧‧‧Steam inlet

500‧‧‧Modified gas export

600‧‧‧氦 import port

Fig. 1 is a view showing a raw material of the present invention comprising a first device in which a plurality of granular materials and/or agglomerates which have been previously heated are introduced into a biomass pyrolysis reactor and a thermal decomposition gas reformer; A schematic diagram of one embodiment of a gasification device.

Fig. 2 is a view showing the raw material of the present invention comprising a first device in which a plurality of granular materials and/or agglomerates which have been heated in advance are introduced into a biomass pyrolysis reactor and a thermal decomposition gas reformer; A schematic view of another embodiment of a gasification unit.

Figure 3 is a view showing that only a plurality of granules and/or lumps which have been preheated are provided A schematic view of one embodiment of a biomass gasification apparatus of the present invention constructed by a second means of entering a thermal decomposition machine.

4(I) to (X) are schematic views showing a plurality of different embodiments of the thermal decomposition gas introduction pipe provided between the raw pyrolysis reactor and the thermal decomposition gas reformer.

Fig. 5 is a schematic view showing a conventional gasification apparatus for use in a comparative example.

The gasification device (first device configuration) of the present invention includes a raw material thermal decomposition device having a raw material supply port, a non-oxidizing gas supply port and/or a steam injection port, and a thermal decomposition gas reformer. a steam injection inlet and a reformed gas discharge port; and a thermal decomposition gas introduction pipe that introduces the pyrolysis gas generated in the biomass pyrolysis device to the thermal decomposition gas reformer, and is equipped with the thermal decomposition of the biomass And the pyrolysis gas reformer and the pyrolysis gas reformer respectively have a plurality of granular materials and/or masses which are preheated, that is, hot load Hold the inlet and outlet of the medium (heat carrier). Further, the plurality of granules and/or lumps which are preheated are introduced into the biomass pyrolysis reactor and the pyrolysis gas reformer, and the plurality of granules and/or lumps have Heat, the thermal decomposition of the biomass and the modification of the thermal decomposition gas generated by the thermal decomposition of the biomass. Here, in the gasification apparatus of the present invention, the biomass pyrolysis reactor and the thermal decomposition gas reformer are arranged side by side with respect to the flow of a plurality of granular materials and/or masses. Thus, the tandem thermal decomposition device and the thermal decomposition gas reformer are arranged in series with each other with respect to a plurality of granular and/or massive streams, as they are arranged side by side, rather than a conventional gasification device. Equipped, a plurality of granules and/or lumps can be individually introduced into the biomass pyrolyzer and the pyrolysis gas reformer, so that the temperature of each can be individually controlled.

In the gasification device of the present invention, the thermal decomposition gas introduction pipe is connected to the raw Both sides of the thermal decomposition device and the thermal decomposition gas reformer are provided in a plurality of granular and/or block layers which are respectively formed in the biomass pyrolysis device and the thermal decomposition gas reformer, that is, heat The side of the upper layer of the carrier layer is located below the surface of the thermal decomposition device and the thermal decomposition gas reformer. That is, a gas suction port (gas inlet) of a pyrolysis gas introduction pipe is provided in a layer containing a plurality of granular materials and/or blocks formed in the biothermal pyrolyzer on the side of the biothermal decomposition machine. And on the side of the pyrolysis gas reformer, a gas introduction port (gas outlet) of the pyrolysis gas introduction pipe is provided in a layer containing a plurality of particles and/or blocks formed in the pyrolysis gas reformer. . Further, the pyrolysis gas generated in the biothermal decomposition machine is introduced into the pyrolysis gas reformer through the pyrolysis gas introduction pipe. In this way, since the suction port of the pyrolysis gas of the pyrolysis gas introduction pipe is disposed in a layer containing a plurality of granular materials and/or agglomerates, the plurality of granular materials present in the biothermal pyrolyzer and And a part of the block may intrude into the inside of the pyrolysis gas introduction pipe, and the gas introduction port of the pyrolysis gas introduction pipe facing the pyrolysis gas reformer is disposed in a plurality of granules and/or blocks In the layer of the material, a part of the plurality of granules and/or blocks present in the thermal decomposition gas reformer may intrude into the interior of the pyrolysis gas introduction pipe, so that the pyrolysis gas introduction pipe can be There are several granules and/or lumps in the interior. Further, since the pyrolysis gas introduction pipe is disposed substantially horizontally with respect to the direction of gravity, a plurality of granules and/or lumps easily intrude into the inside of the pyrolysis gas introduction pipe, and the number of the pyrolysis gas introduction pipe is retained inside. The granules and/or masses may be in the flow of a plurality of granules and/or lumps that move from top to bottom in accordance with gravity in a biomass pyrolyzer and a pyrolysis gas reformer. The plurality of granules and/or lumps that move from top to bottom are continuously replaced. Further, by this, a plurality of granules and/or lumps held in the inside of the pyrolysis gas introduction pipe can be maintained in a new state. Further, it is possible to prevent a plurality of granules and/or blocks from flowing into the pyrolysis gas introduction pipe by the pyrothermal pyrolyzer The material is mixed into the thermal decomposition gas reformer, and on the other hand, a plurality of particles and/or blocks which flow from the thermal decomposition gas reformer into the thermal decomposition gas introduction pipe can be prevented from being mixed into the thermal decomposition of the biomass. In the device. Since a plurality of granules and/or lumps are retained in the inside of the pyrolysis gas introduction pipe, the tar and coal dust contained in the pyrolysis gas introduced into the pyrolysis gas reformer through the pyrolysis gas introduction pipe are collected. It is captured by contact with the plurality of granules and/or lumps. Moreover, a portion or a majority of the captured tar is thermally decomposed and gasified by the heat of the plurality of granules and/or masses, preferably modified. Further, the tar and coal dust remaining without being gasified remain attached to a plurality of granular materials and/or chunks, and are discharged from the bottom of the pyrolysis pyrolyzer and the bottom of the pyrolysis gas reformer. Thereby, tar and coal dust can be effectively removed from the pyrolysis gas.

In the gasification apparatus of the present invention, it is preferable that the inner bottom surface of the pyrolysis gas introduction pipe has a structure that protrudes upward. In this way, since the bottom surface of the thermal decomposition gas introduction pipe has a structure that protrudes upward, it is possible to more effectively prevent the intrusion of the autothermal decomposition machine into the plurality of granular materials and/or masses of the thermal decomposition gas introduction pipe, and The number of particles and/or blocks of the pyrolysis gas reformer intruding into the thermal decomposition gas introduction pipe can more effectively prevent the inflow of the pyrothermal pyrolyzer into the thermal decomposition gas introduction pipe. The granules and/or the lumps are mixed into the thermal decomposition gas reformer, and on the other hand, the granules and/or the lumps which flow from the thermal decomposition gas reformer into the thermal decomposition gas introduction pipe The substance is mixed into the biothermal decomposition machine. More preferably, the inner bottom surface of the pyrolysis gas introduction pipe has a structure in which both sides of the pyrolysis thermodegrader and the thermal decomposition gas reformer protrude upward toward the center portion with a slope. The angle (θ) of the above slope is preferably 5 to 45 degrees, more preferably 10 to 30 degrees, and still more preferably 15 to 25 degrees. The angle (θ) of the slope may be the same on both sides of the biomass pyrolyzer and the thermal decomposition gas reformer, or may be different. Because of this slope, it can prevent autothermal decomposition and thermal decomposition of gases. Both of the reformer invade the plurality of granules and/or lumps of the pyrolysis gas introduction tube to stagnate at the junction of the two, thereby promoting the thermal decomposition of several granules and/or lumps. Replacement in the gas introduction tube. In the thermal decomposition gas introduction pipe, the cross section perpendicular to the longitudinal direction, that is, the cross section perpendicular to the flow direction of the pyrolysis gas is preferably substantially circular or substantially polygonal, and more preferably substantially quadrangular. The inner diameter of the thermal decomposition gas introduction pipe is not particularly limited as long as a plurality of granules and/or lumps can easily flow into the thermal decomposition gas introduction pipe and flow out. Further, the pyrolysis gas introduction pipe is preferably provided in the range of 1 to 3, more preferably 1 or 2, between the biomass pyrolysis reactor and the pyrolysis gas reformer.

In the gasification apparatus of the present invention, the steam injection port is preferably provided in a group selected from the group consisting of a biomass pyrolysis reactor and its vicinity, a pyrolysis gas reformer and its vicinity, and a pyrolysis gas introduction pipe. More than one location. More preferably, the steam injection port is provided in the vicinity of the biomass pyrolysis reactor or its vicinity, the thermal decomposition gas reformer or its vicinity, and the thermal decomposition gas introduction pipe. Thereby, the thermal decomposition of the biomass and the modification of the thermal decomposition gas can be achieved more satisfactorily. The number of the steam injection ports is not particularly limited, but it is preferably one to three in the vicinity of the biomass pyrolysis reactor or the vicinity thereof, the thermal decomposition gas reformer or the vicinity thereof, and the thermal decomposition gas introduction pipe. It is better to equip one each.

In the gasification apparatus of the present invention, a preheater for preheating a plurality of granules and/or lumps is provided on the upper portion of the biomass pyrolysis reactor and the pyrolysis gas reformer. Thereby, the plurality of granules and/or lumps are heated to a predetermined temperature. The preheater can be disposed on the upper part of the biomass pyrolyzer and the thermal decomposition gas reformer, and here, all the granules and/or the masses are heated to a predetermined temperature, and the heating is performed to the same The granules and/or chunks of the temperature are individually introduced into the biomass thermal decomposition machine and the thermal decomposition gas reformer. In addition, the preheater can be modified in the thermal decomposition machine and the thermal decomposition gas. Each of the upper devices is provided in a single unit, that is, a total of two units, and each of the preheaters is heated to a temperature suitable for each of the biomass pyrolysis reactor and the pyrolysis gas reformer, and then individually introduced into the biomass. Thermal decomposer and thermal decomposition gas reformer. In any of the above configurations, the effect can be sufficiently achieved. According to the former configuration, the cost of the device can be reduced, and when the biomass thermal decomposition temperature is controlled by the amount of steam introduced into the biothermal pyrolyzer, the thermal decomposition can be more efficiently performed by introducing steam. Upgraded. On the other hand, if the latter form is employed, temperature control can be easily performed, and the energy required for heating the granular material and/or the bulk material can be reduced.

Further, on the upper (upper), preferably the top, of the raw pyrolysis reactor and the pyrolysis gas reformer, a plurality of inlets of granules and/or lumps are provided, and on the other hand, heat is generated. The lower (lower), preferably bottom, of the decomposer and the pyrolysis gas reformer are provided with a plurality of discharge ports for the granules and/or blocks. The introduction port and the discharge port of a plurality of granules and/or lumps are, for example, a so-called two-stage valve type in which one valve is provided on the upper and lower sides of the pipe. However, this introduction and release method is an example and is not limited to this mode.

Preferably, the plurality of granules and/or lumps, that is, the heat-carrying medium (heat carrier), comprise one or more materials selected from the group consisting of metals and ceramics. The metal is preferably selected from the group consisting of iron, stainless steel, nickel alloy steel, and titanium alloy steel, and more preferably stainless steel. Further, the ceramic is selected from the group consisting of alumina, ceria, lanthanum carbide, tungsten carbide, zirconia, and tantalum nitride, and more preferably alumina. The shape of the plurality of granules and/or lumps is preferably a spherical shape (ball), but it is not necessary to be a true ball, and may be a spherical shape having an elliptical or oblate cross-sectional shape. The diameter (maximum diameter) of the ball is preferably from 3 to 25 mm, more preferably from 8 to 15 mm. If the above upper limit is exceeded, the fluidity inside the biothermal pyrolyzer and the pyrolysis gas reformer may be impaired, that is, In the case of the fall property, there is a case where the ball is stationary and blocked inside the pyrolysis gas cracker and the pyrolysis gas reformer. On the other hand, if the lower limit is not satisfied, the ball itself may be fixed by adhesion to tar or coal dust of the ball, and may cause clogging. For example, if the diameter of the ball is less than 3 mm, there is a concern that the ball is attached to the inner wall of the biothermal pyrolyzer and grows due to the influence of the tar and coal dust adhering to the ball. In the case of a poor condition, the biothermal resolver is blocked. Further, when the ball to which the tar is attached is released from the valve at the bottom of the pyrolysis thermodegrader and the pyrolysis gas reformer, the ball having a thickness of less than 3 mm is light and adheres to the tar. Unnaturally falling on the floor is fixed inside the valve to encourage blockage.

The term "raw quality" as used in the present invention refers to a biomass resource which is generally referred to. Here, the term "living resources" refers to plant-based biomass such as thinned wood from forestry, wood waste materials, pruned branches, forest residue, unused trees, vegetable residues from agricultural waste, and fruit tree residues. , rice straw, wheat straw and rice husk, other marine plants, construction waste wood, etc.; biological biomass such as livestock excreta represented by livestock waste and sewage sludge; and domestic wastes and foods such as garbage Waste, etc. Preferably, the apparatus of the present invention is suitable for the gasification of plant biomass and biomass biomass.

Hereinafter, the biomass gasification device of the present invention will be described based on the accompanying drawings. Fig. 1 is a view showing that a plurality of granular materials and/or agglomerates (7) which are preheated, that is, a heat carrying medium (heat carrier), are supplied to a biomass pyrolysis device (3) and a thermal decomposition gas is modified. A schematic view of one embodiment of the biomass gasification device of the present invention comprising the first device of the two of the devices (2). In the gasification apparatus of the biomass, the flow of the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) with respect to a plurality of granules and/or lumps (7), ie, heat carriers Side by side. Moreover, for pre-preparing a plurality of granules and/or lumps (7) The preheater (1) that is heated first is equipped with one set on the top of the biomass pyrolyzer (3) and the thermal decomposition gas reformer (2). Further, a thermal decomposition gas introduction pipe (9) is provided between the biomass pyrolysis reactor (3) and the thermal decomposition gas reformer (2), whereby the biomass thermal decomposition device (3) is produced. The thermal decomposition gas is introduced into the thermal decomposition gas reformer (2). Here, the pyrolysis gas introduction pipe (9) is disposed on both sides of the biomass pyrolysis device (3) and the pyrolysis gas reformer (2), and is separately formed in the biomass pyrolysis device (3) and Thermal decomposition gas reformer (2) of several granules and / or block (7) layer above the surface (13) below the biomass thermal decomposition device (3) and thermal decomposition gas reformer (2) The side. That is, the gas decomposition port (gas inlet) (9-3) and the thermal decomposition gas reformer (2) side gas introduction port (gas outlet) of the pyrolysis gas introduction pipe (9) (9-2) are all disposed in a plurality of granules and/or lumps (7) layers. Further, the pyrolysis gas introduction pipe (9) is provided substantially horizontally with respect to the direction of gravity. Moreover, it is preferable that the inner bottom surface of the pyrolysis gas introduction pipe (9) has a structure that protrudes upward. However, the inner bottom surface may also be of a flat configuration.

A plurality of granules and/or lumps (7), ie, heat carriers, are introduced into the preheater (1) before being introduced into the biomass pyrolyzer (3) and the pyrolysis gas reformer (2). It is heated in advance. The heat carrier (7) is preferably heated to 1,000 to 1,100 ° C, more preferably 1,050 to 1,100 ° C. If the lower limit is not exceeded, there is a case where the gas generated by the thermal decomposition of the biomass cannot be sufficiently modified in the thermal decomposition gas reformer (2). On the other hand, when the above-mentioned upper limit is exceeded, the light is given excessive heat, but the apparent effect cannot be expected to increase, and the cost alone is caused. Moreover, it also causes the thermal efficiency of the equipment to decrease.

The heat carrier (7) heated to the above-mentioned predetermined temperature in the preheater (1) is then individually introduced into the biomass thermal decomposition device (3) and the thermal decomposition gas which are arranged side by side with respect to the flow direction of the heat carrier (7). Quality device (2). In the raw pyrolysis reactor (3), the heat carrier (7) is separately supplied to the biomass of the biomass pyrolysis device (3) in contact with the pyrosol supply port (4). Here, the raw material supply port (4) may be disposed in the biothermal pyrolyzer (3) itself, or as shown in Fig. 1, disposed near the biothermal pyrolyzer (3), for example, the heat carrier (7) The distribution pipe of the biothermal decomposition device (3). Further, in the raw material thermal decomposition device (3), a non-oxidizing gas such as nitrogen gas and any steam are supplied from the non-oxidizing gas supply port (12) and the steam injection port (11 ₁ ), thereby maintaining non-oxidation. A gaseous environment, or a mixed gas environment of non-oxidizing gases and steam. Then, the biomass is heated and thermally decomposed by contact of the heat carrier (7) with the biomass to form a pyrolysis gas. By setting the biothermal pyrolyzer (3) to a non-oxidizing gas atmosphere, the combustion of the biomass can be prevented, and the biomass can be thermally decomposed with good efficiency. The generated thermal decomposition gas system is introduced into the thermal decomposition gas reformer (2) through the thermal decomposition gas introduction pipe (9). At this time, the tar and coal dust contained in the generated pyrolysis gas are trapped by the heat carrier (7) held in the pyrolysis gas introduction pipe (9), and a part or most of the tar is heated by the heat carrier (7). The residual tar and coal dust are kept attached to the heat carrier (7) and discharged from the bottom of the pyrolysis thermal cracker (3) or the thermal decomposition gas reformer (2). The upper limit of the gas phase temperature of the biomass pyrolyzer (3) is preferably 700 ° C, more preferably 650 ° C, and the lower limit is preferably 400 ° C, more preferably 500 ° C, and still more preferably 550 ° C. If the lower limit is not exceeded, there is a case where the thermal decomposition of the biomass cannot progress. If the above upper limit is exceeded, heavy tar is produced. Therefore, the heavy tar cannot be sufficiently reformed by steam, and thus there is a case where the device malfunctions due to tar. Here, the gas phase temperature of the biomass pyrolyzer (3) refers to the preheated heat carrier (7) charged into the biothermal pyrolyzer (3), the raw material as a raw material, and non-oxidizing property. The gas phase temperature inside the biomass pyrolyzer (3) which is produced by mixing the gas with the arbitrarily injected steam and the radiant heat of the heat carrier (7) layer. The gas phase temperature of the biothermal pyrolyzer (3) can be obtained by the supply rate and release rate of the heat carrier (7), the volume of the heat carrier layer in the biothermal decomposition device (3), and its occupancy, and the biomass. The supply amount, the supply amount of the non-oxidizing gas and/or steam, and the like are appropriately controlled. In general, the supply rate and the release rate of the heat carrier (7) can be determined according to the amount of the raw material supplied, and then the volume of the heat carrier layer in the biomass pyrolyzer (3) and its occupancy rate can be gradually changed while being appropriately changed. The supply amount of the non-oxidizing gas and/or steam is used to control the gas phase temperature of the biomass pyrolyzer (3) to a predetermined temperature.

The pyrolysis gas generated by thermally decomposing the biomass in the thermal decomposition machine (3) is introduced into the thermal decomposition gas reformer (2) through the thermal decomposition gas introduction pipe (9). The introduced thermal decomposition gas system is heated in contact with the heat carrier (7) in the presence of steam. Thereby, the pyrolysis gas and the steam can be reacted to reform the pyrolysis gas into a hydrogen-rich gas. Here, the steam for gas upgrading is provided in the vicinity of the free biomass pyrolyzer (3) and its vicinity, the thermal decomposition gas reformer (2) and its vicinity, and the biomass thermal decomposition device (3). The steam injection ports (11 ₁ , 11 ₂ , 11 ₃ ) at one or more selected ones of the group consisting of the pyrolysis gas introduction pipes (9) between the thermal decomposition gas reformers (2) are introduced. Preferably, the steam injection port (11 ₁ , 11) is provided from the raw material thermal decomposition device (3) or its vicinity, the thermal decomposition gas reformer (2) or its vicinity, and the thermal decomposition gas introduction pipe (9). ₂ , 11 ₃ ) All imported. The upper limit of the gas phase temperature in the thermal decomposition gas reformer (2) is preferably 1,000 ° C, more preferably 950 ° C, still more preferably 930 ° C, and the lower limit is preferably 700 ° C, more preferably 850 ° C, and thus Good for 880 ° C. If the lower limit is not exceeded, there is a case where the reforming reaction cannot progress. On the other hand, even if the above upper limit is exceeded, an increase in the apparent effect cannot be expected, and the amount of heat required for heating the heat carrier increases, resulting in high cost. The gas phase temperature in the thermal decomposition gas reformer (2) is 850 ° C or higher as the above-mentioned lower limit value, and the modification of one of the carbon oxides by the steam becomes remarkable, and is more preferably 880 ° C or more as a lower limit. The methane reformation by steam has become remarkable. Therefore, in order to efficiently reform both carbon monoxide and methane, the gas phase temperature in the thermal decomposition gas reformer (2) is further preferably 880 ° C or higher. The upper limit of the gas phase temperature in the thermal decomposition gas reformer (2) is preferably 950 ° C, and the pyrolysis gas can be sufficiently reformed at or below this temperature. However, in order to reduce the amount of fuel used, it is preferably 930. Below °C. Here, the gas phase temperature of the pyrolysis gas reformer (2) is a mixture of a preheated heat carrier (7), a pyrolysis gas, and steam which are introduced into the pyrolysis gas reformer (2). The temperature of the gas phase inside the thermal decomposition gas reformer (2) which is comprehensively generated by the temperature and the radiant heat of the self-heating carrier (7) layer. The gas phase temperature of the thermal decomposition gas reformer (2) can be obtained by the supply temperature of the heat carrier (7), the supply rate and release rate of the heat carrier (7), and the heat carrier in the thermal decomposition gas reformer (2). The volume of the layer and its occupancy rate, the amount of thermal decomposition gas supplied from the pyrothermal pyrolyzer (3), the supply amount of steam, and the like are appropriately controlled. In general, the heat carrier (7) can be fixed by preliminarily setting the supply speed and discharge rate of the heat carrier (7), the volume of the heat carrier layer in the pyrolysis gas reformer (2), and the occupancy thereof. The supply temperature is preferably higher than the required gas phase temperature by 100 to 400 ° C, more preferably 150 to 200 ° C higher, and the steam supply amount is appropriately changed, and the biomass thermal decomposition device (3) is used. The phase temperature is controlled to a predetermined temperature.

The thermal decomposition of the biomass in the above-mentioned biothermal pyrolyzer (3) and the heat required for the reformation of the thermal decomposition gas in the thermal decomposition gas reformer (2) are almost always heated to the above temperature The granules and/or the lumps (7), that is, the heat of the heat-carrying medium (heat carrier), are supplied. Introduction of heat carrier (7) to biothermal pyrolyzer (3) and thermal decomposition gas reformer (2), and heat carrier (7) autothermal decomposition device (3) and thermal decomposition gas reformer (2) The release is performed by, for example, a so-called two-stage valve method (not shown) having one valve for each of the two pipes. The operation of the two-stage valve method will be briefly described. The upper and lower valves are closed in advance. First, the upper valve is opened to cause the heat carrier (7) to fall inside the pipe, and the heat carrier (7) is filled to the lower valve. Between the upper valve and the upper valve. Then, by closing the upper valve, the lower valve is opened, and the heat carrier (7) will be filled between the two valves. It is introduced into the raw thermal decomposition machine (3) and the thermal decomposition gas reformer (2), or the pyrolysis thermal decomposition device (3) and the thermal decomposition gas reformer (2). By repeating such a valve operation, the heat carrier (7) is introduced almost continuously into the biomass pyrolyzer (3) and the pyrolysis gas reformer (2), and the autothermal decomposition device (3) and The thermal decomposition gas reformer (2) is discharged almost continuously. This introduction and release method is an example and is not limited to this mode. The heat can be formed in the biomass pyrolyzer (3) by controlling the introduction of the heat carrier (7) into the biomass pyrolyzer (3) and the release rate of the heat carrier (7) autogenic thermal decomposition device (3). The carrier layer is controlled to a suitable value, and the temperature of the biomass pyrolyzer (3) is controlled to the above-mentioned predetermined temperature. The same is true for the thermal decomposition gas reformer (2). Thus, the thermal decomposition gas reformer (2) and the biothermal pyrolyzer (3) can be individually controlled by arranging the thermal decomposition gas reformer (2) in parallel with the biothermal pyrolyzer (3). The internal temperature. Thereby, the reforming reaction in the pyrolysis gas reformer (2) can be carried out at a reasonable temperature, and the thermal decomposition of the biomass in the biothermal pyrolyzer (3) can be performed at a reasonable temperature. Further, the thermal efficiency can be improved. Further, the thermal decomposition gas reformer (2) and the biomass pyrolyzer (3) are arranged side by side with respect to the flow direction of the heat carrier, and the respective containers (2, 3) are preferably arranged in a vertical shape. The heat carrier is naturally dropped by gravity, and an energy-saving and efficient gasification device can be made without the power for moving the heat carrier.

Here, if the heat carrier (7) self-generating thermal decomposition device (3) and the thermal decomposition gas reformer (2) are discharged too fast, the biomass thermal decomposition device (3) and the thermal decomposition gas reformer ( 2) The temperature becomes high. On the other hand, if the discharge rate is too slow, the heat carrier dissipates heat, and the temperature of the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) becomes low. The supply rate and the release rate of the heat carrier (7) to the biomass pyrolyzer (3) depend on the amount of the raw material supplied as the raw material, the type thereof, and the moisture and ash content of the raw material, but usually for the raw material. The amount of supply is determined. Usually, it is set as the dry raw material, that is, the dry biomass is divided into the raw heat score. The supply speed of the decoupling device (3) is 5 to 60 times the mass. It is preferably set to 5 to 30 mass times, more preferably 10 to 20 mass times, of the supply rate of the dry biomass to the biomass pyrolyzer (3). If the lower limit is not exceeded, the amount of heat required to thermally decompose the biomass cannot be supplied. On the other hand, if the upper limit is exceeded, only the supply amount of the heat carrier (7) becomes excessive. Therefore, it is necessary to increase the mass spectrometer (3) to more than necessary, and further, the heat carrier (7) is heated. Need extra calories. Further, the supply rate and the release rate of the thermal decomposition gas reformer (2) of the heat carrier (7) are controlled depending on the amount of the pyrolysis gas to be supplied and the temperature thereof, the temperature of the steam, the supply amount thereof, and the like. However, it is preferable to determine the amount of supply of the raw material in advance, and to control at any time based on the fluctuation of the above factors or the like in the operation stage. Usually, it is set to 5 to 30 mass times of the supply speed of the dry raw material, that is, the dry biomass to the biomass thermal decomposition device (3). Preferably, it is set to be 5 to 15 times the mass of the supply rate of the dry biomass to the biomass pyrolyzer (3), and more preferably set to 10 to 15 times the mass. If the lower limit is not exceeded, the amount of heat required to reform the pyrolysis gas cannot be supplied. On the other hand, if the upper limit is exceeded, only the supply amount of the heat carrier (7) becomes excessive. Therefore, it is necessary to increase the thermal decomposition gas reformer (2) to more than necessary, and the heat carrier (7) Heating requires extra heat.

The upper limit of the pressure in the thermal decomposition catalyst (3) and the thermal decomposition gas reformer (2) is preferably 104.33 kPa, more preferably 102.33 kPa, and the lower limit is preferably 100.33 kPa, more preferably 101.23 kPa. When the above upper limit is exceeded, the generated pyrolysis gas may leak from the raw material supply port (4) to the outside of the biomass pyrolyzer (3) in a countercurrent flow. On the other hand, if the lower limit is not satisfied, there is a case where the generated thermal decomposition gas system is unevenly dispersed and passes through the biomass pyrolysis reactor (3), the thermal decomposition gas reformer (2), and the thermal decomposition gas introduction pipe. (9) Inside the layer of the heat carrier (7), the thermal decomposition gas and the tar of the same gas cannot be sufficiently gasified and modified.

As described above, the steam injection ports (11 ₁ , 11 ₂ , 11 ₃ ) are preferably disposed at the bottom of the biothermal pyrolyzer (3), the bottom of the pyrolysis gas reformer (2), and the thermal decomposition machine (3). And a thermal decomposition gas introduction pipe (9) between the thermal decomposition gas reformer (2). When it is disposed in the biothermal pyrolyzer (3), it is preferably disposed on the upper portion of the biothermal pyrolyzer (3). Thereby, the contact of the steam introduced into the thermal decomposition machine (3) with the heat carrier (7) can be performed more efficiently, and not only the contact time of the steam with the gas generated by thermal decomposition of the biomass can be performed. It becomes longer and the contact time with the heat carrier (7) can be made longer. Then, as a result, gasification and upgrading of the pyrolysis gas and the tar adhering to the heat carrier can be efficiently performed. In Fig. 1, the steam injection port is connected to the lower part (11 ₂ ) of the pyrolysis gas reformer ( ₂ ), the upper part (11 ₁ ) of the biothermal pyrolyzer (3), and the pyrolysis gas introduction pipe (9). (11 ₃ ) One is provided separately, and a total of three are provided, but the present invention is not limited thereto. The steam injection port can also be provided in several places. The temperature of the supplied steam is not particularly limited, but is preferably 130 to 200 ° C, more preferably about 160 ° C. Further, superheated steam of 500 to 600 ° C can also be preferably used. For example, when steam is supplied at a temperature of about 160 ° C, the supply amount of steam is preferably substantially equal to the supply amount of the raw material as a raw material. However, since the amount of steam is increased or decreased depending on the amount of moisture of the raw material, it is not limited to the above.

The raw material supply port (4) is provided in the raw material thermal decomposition device (3) at a position where the raw material can be efficiently supplied. Preferably, it is preferably provided in a pipe in which the heat carrier (7) is placed above the pyrolysis pyrolyzer (3), that is, the preheater (1) is dropped to the raw material thermal decomposition device (3). Thereby, the mixing of the biomass and the heat carrier (7) can be performed efficiently, and the contact time in the inside of the biothermal pyrolyzer (3) can be appropriately ensured, and the biomass can be sufficiently thermally decomposed. In FIG. 1, one raw material supply port (4) is described, but it is not limited to this. The raw material supply port (4) is preferably one or more, more preferably one to five, further preferably one to three, and still more preferably one or two. It can be set up by several raw material supply ports (4), but also from various supplies. The mouth simultaneously supplies different traits of traits.

The residence time of the biomass in the biothermal pyrolyzer (3) is preferably from 5 to 60 minutes, more preferably from 10 to 40 minutes, and still more preferably from 15 to 35 minutes. If the lower limit is not exceeded, heat is not uniformly transferred to the raw material, so that uniform thermal decomposition is not performed, so that the amount of thermal decomposition gas generated is reduced. On the other hand, even if the above upper limit is exceeded, an increase in the apparent effect is not confirmed, and on the contrary, an increase in equipment cost is caused. Here, the residence time of the biomass in the biomass pyrolyzer (3) can be appropriately adjusted according to the moving speed of the heat carrier (7) and the amount of raw material supplied. Further, the residence time of the gas in the pyrolysis gas reformer (2) is preferably from 1 to 10 seconds, more preferably from 2 to 5 seconds. The residence time of the gas in the thermal decomposition gas reformer (2) can be set according to the moving speed and the filling amount of the heat carrier (7), the steam supply amount, and the predetermined amount of thermal decomposition gas. If the thermal decomposition gas reformer and the biothermal pyrolyzer are connected in series, as is conventionally known, it is not possible to individually control the residence time in each container, that is, the biomass used in the biomass thermal decomposer. The residence time of the thermal decomposition and the residence time of the tar decomposition in the thermal decomposition gas, and the residence time required for the modification reaction of the thermal decomposition gas and steam in the thermal decomposition gas reformer. However, by arranging the pyrolysis gas reformer (2) in parallel with the biothermal pyrolyzer (3) as in the present invention, the residence time in each container can be independently controlled, and therefore, no new energy is consumed. The temperature inside the respective containers (2, 3) can be independently controlled.

In the above manner, the heat carrier (7) of the biomass pyrolyzer (3) and the thermal decomposition residue (carbon) of the biomass, and the trace amount of tar and coal dust remaining after being thermally decomposed by the heat carrier (7) Wait for the same to be discharged from the bottom of the pyrothermal pyrolyzer (3). The treatment of the discharged effluent containing the heat carrier (7) is carried out by a previously known method of separating carbon in the effluent treating device (5) as shown in Fig. 1. For example, the methods and apparatuses described in the above Patent Documents 4 and 5 can be employed. On the other hand, through the thermal decomposition gas reformer (2) The heat carrier (7) is discharged from the bottom of the thermal decomposition gas reformer (2) together with a trace amount of tar and coal dust attached to the heat carrier (7). The treatment of the discharged effluent containing the heat carrier (7) is carried out with or without mixing with the heat carrier (7) discharged from the bottom of the pyrolysis pyrolyzer (3), and is carried out by a previously known method. For example, the methods and apparatuses described in Patent Documents 4 and 5 can be employed in the same manner as described above. The heat carrier (7) treated in this way is returned to the preheater (1) again and supplied to the biomass pyrolyzer (3) and the pyrolysis gas reformer (2).

2 is a view showing that a plurality of granular materials and/or agglomerates (7), that is, a heat-carrying medium (heat carrier), which are preheated, are supplied to a biomass pyrolyzer (3) and pyrolyzed gas is modified. A schematic view of another embodiment of the biomass gasification device of the present invention comprising the first device of the two of the devices (2). In the gasification device of the biomass, one unit is provided on each of the upper part of the biomass pyrolysis device (3) and the thermal decomposition gas reformer (2) for several particles and/or blocks. (7) Preheated preheater (1 ₁ , 1 ₂ ). The other device configuration is the same as the biomass gasification device shown in Fig. 1.

A plurality of granules and/or lumps (7), ie, heat carriers, are introduced into the biomass thermal decomposition device before being introduced into the biomass pyrolysis reactor (3) and the pyrolysis gas reformer (2). (3) The preheaters (1 ₂ ) and (1 ₁ ) in the upper part of each of the thermal decomposition gas reformers (2) are heated in advance. Provided in the thermal decomposition in biomass (3) of the upper portion of the preheater _(12), the heat carrier (7) is preferably heated to 700 ~ 800 ℃, more preferably 750 ~ 800 ℃. If the lower limit is not exceeded, the raw material cannot be sufficiently thermally decomposed in the biomass pyrolyzer (3). Even if it exceeds the above upper limit, as described in the above description of Fig. 1, the amount of steam injected into the biothermal decomposition machine (3) can be changed, and controlled to a reasonable temperature, and the thermal decomposition of the biomass can be efficiently performed. . However, when the number of the preheaters (1) is two, it is preferable to increase the thermal efficiency by setting the temperature of the heat carrier (7) to be equal to or lower than the above upper limit. On the other hand, in the preheater (1 ₁ ) provided on the upper portion of the pyrolysis gas reformer (2), the heat carrier (7) is heated to preferably 1,000 to 1,100 ° C, more preferably 1,050 to 1,100. °C. If the lower limit is not exceeded, the gas generated by the thermal decomposition of the biomass cannot be sufficiently modified in the thermal decomposition gas reformer (2). Moreover, if it exceeds the said upper limit, only the excess heat is provided, and the improvement of the obvious effect is not expectable, and only the high cost is contrary. Moreover, it also causes the thermal efficiency of the equipment to decrease.

Figure 4 shows a number of different embodiments (I, II, III,) of the thermal decomposition gas introduction pipe (9) provided between the biothermal pyrolyzer (3) and the pyrolysis gas reformer (2). A schematic diagram of IV, V, VI, VII, VIII, IX, X). Fig. 4 is a cross section showing a longitudinal direction of the pyrolysis gas introduction pipe (9) (a cross section along the flow direction of the pyrolysis gas). Further, in Fig. 4, (g) schematically shows the flow direction of the pyrolysis gas. In Fig. 4, the right side of the opposite direction is the biothermal pyrolyzer (3) (shown as 3 in Fig. 4), and the left side is the thermal decomposition gas reformer (2) (shown as 2 in Fig. 4) . Further, only the heat carrier (7) in the pyrolysis gas introduction pipe (9) is schematically represented by coloring, and the heat carrier in the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) is not shown. (7). Further, although not shown in Fig. 4, the thermally decomposed gas introduction pipe (9) may have a flat bottom surface which is a plane which does not protrude upward. All of the thermal decomposition gas introduction pipes (9) shown in Fig. 4 can be used for the thermal decomposition device of the biomass of the present invention, for example, the thermal decomposition device of the biomass shown in Figs. 1 and 2. That is, on both sides of the biothermal pyrolyzer (3) and the pyrolysis gas reformer (2), they are respectively formed in the biothermal pyrolyzer (3) and the pyrolysis gas reformer (2). The surface of the thermal carrier (7) above the surface (13) is located below the biomass pyrolyzer (3) and the side of the thermal decomposition gas reformer (2), and the thermal decomposition gas introduction tube (9) is opposed to gravity The direction is substantially horizontally disposed, and the inner bottom surface of the pyrolysis gas introduction pipe (9) has a structure that protrudes upward. The pyrolysis gas introduction pipe (9) shown in (I) and (VI) of Fig. 4 is such that the inner bottom surface thereof protrudes upward, and the height (h) of the protruding portion is lower than that of the pyrolysis gas introduction pipe (9). The width (height) (h ₁ , h ₂ ) of the suction port (gas inlet) and the gas introduction port (gas outlet) in the vertical direction. Therefore, the heat carrier (7) invading both the autothermal decomposition machine (3) and the thermal decomposition gas reformer (2) merges above the protruding portion. However, since the heat carrier (7) is a granule and/or agglomerate, it is not easily mixed with a liquid such as water or oil. Therefore, the heat carrier (7) that has entered the pyrolysis gas introduction pipe (9) by the autothermal decomposition machine (3) does not intrude into the inside of the pyrolysis gas reformer (2). Further, conversely, the heat carrier (7) that has entered the pyrolysis gas introduction pipe (9) from the pyrolysis gas reformer (2) does not intrude into the inside of the biomass pyrolyzer (3). However, it is expected that if the operation of the biomass thermal decomposition apparatus is continued for a relatively long period of time, it will be scarcely mixed. In order to surely avoid such a situation, it is preferable to set the pyrolysis gas introduction pipe (9) as shown in (II), (III) and (IV) and (VII), (VIII) and (IX) of Fig. 4 . Construction. That is, the height (h) of the protruding portion of the inner bottom surface of the pyrolysis gas introduction pipe (9) and the width (height) of the gas suction port and the inlet port of the pyrolysis gas introduction pipe (9) (h ₁ , h ₂ ) Structure (III, IV, VIII, IX) compared to the same structure (II, VII) or higher. More preferably, the height (h) of the protruding portion is higher than the width (height) (h ₁ , h ₂ ) of the vertical direction of the gas suction port and the inlet of the pyrolysis gas introduction pipe (9) (III, IV) , VIII, IX). With such a configuration, the mixing of the heat carrier (7) can be more reliably prevented. Further, in the case where the protruding portion extends perpendicularly from the bottom surface of the pyrolysis gas introduction pipe (9) as shown in (I) and (II) of Fig. 4, it exists in the pyrothermal pyrolyzer (3) and heat. The portion where the heat carrier (7) invading the gas reformer (2) merges with each other, or the portion where the heat carrier (7) contacts the protruding portion, the heat carrier (7) invaded from each of them is stagnated. Therefore, in order to avoid the stagnation, it is preferable to adopt a configuration in which the protruding portion has an inclination angle (θ) as in the case of (III), (IV), (VI), (VII), (VIII) and (IX) of FIG. 4 . . More preferably, the structures of (VII), (VIII) and (IX) of Fig. 4 are used. For example, as shown in FIG. 4(III), the structure having the inclination angle (θ) in two stages is less effective than the structure of FIG. 4 (VIII) having the same inclination angle (θ). The situation. Therefore, in the protruding portion of the shape which protrudes stepwise as shown in the left row of Fig. 4, it is more preferable to increase the number of the stages. The inclination angle (θ) is preferably 5 to 45 degrees, more preferably 10 to 30 degrees, and still more preferably 15 to 25 degrees. Further, as in the thermal decomposition gas introduction pipe (9) shown in FIGS. 4(IV) and (IX), the structure is basically a horizontal pipe, but it may be configured as follows: (IV) inside the pipe A concave portion is provided on the upper surface, or a concave portion having a slope is provided on the inner upper surface of the pipe as in (IX). Further, the width (height) (h ₁ , h ₂ ) of the gas inlet and the gas inlet of the pyrolysis gas introduction pipe (9) in the vertical direction may be the same or different. The inclination angle (θ) is also on either side of the biomass pyrolyzer and the thermal decomposition gas reformer, and may be the same or different. Further, as shown in FIGS. 4(V) and (X), a structure in which no space portion (gas accumulation portion) is provided in the upper portion of the pyrolysis gas introduction pipe (9) may be employed. In this case, the gas generated in the biothermal pyrolyzer (3) can be introduced into the thermal decomposition gas reformer through the gap of the heat carrier (7) layer existing inside the thermal decomposition gas introduction pipe (9). 2). That is, in the thermal decomposition gas introduction pipe (9) of the structure, the continuous operation of the biomass gasification device of the present invention can be sufficiently achieved. However, in order to carry out continuous operation for a relatively long period of time, it is preferable to use a thermal decomposition gas introduction pipe (9) provided with a space portion (gas accumulation portion) at the upper portion, for example, (I) of FIG. 4, from the viewpoint of safety. (II), (III), (IV), (VI), (VII), (VIII) and (IX). The thermal decomposition gas introduction pipe (9) shown in Fig. 4 is exemplified, and is not limited thereto. Further, the shape of the pyrolysis gas introduction pipe (9) perpendicular to the longitudinal direction (the cross section perpendicular to the flow direction of the pyrolysis gas) is as described above, preferably substantially circular or substantially polygonal, more preferably Roughly quadrangular. Further, the inner diameter of the thermal decomposition of the gas introducing tube, i.e., the vertical direction of the width of the gas inlet port (height) (h ₁₎ and a gas introduction width (height) in the vertical direction of the mouth (h ₂₎ based heat carrier (7) It is not particularly limited as long as it can easily flow into the pyrolysis gas introduction pipe and is easily discharged, and it is preferably 8 to 50 times, more preferably 10 to 40 times, the size (maximum diameter) of the heat carrier (7). It is preferably 10 to 30 times.

Further, the gasification device (second device configuration) of the present invention includes a raw material thermal decomposition device having a raw material supply port, a non-oxidizing gas supply port and/or a steam injection port, and a pyrolysis gas reformer. a steam injection inlet and a reformed gas discharge port; and a thermal decomposition gas introduction pipe that introduces the pyrolysis gas generated in the biomass pyrolysis device to the thermal decomposition gas reformer and is equipped with the above-mentioned biomass heat Between the decomposer and the pyrolysis gas reformer; and the biothermal pyrolyzer further comprises a plurality of granules and/or lumps which are preheated, that is, the introduction of the heat carrier medium (heat carrier) Further, the pyrolysis gas reformer further includes a flow path of a preheated gas or liquid heat medium on the outer side thereof. Moreover, the plurality of granules and/or lumps which are preheated are introduced into the biomass thermal decomposition device, and the heat of the biomass is performed by the heat of the plurality of granules and/or the lumps. Dissolving, on the other hand, introducing a preheated gas or liquid heat medium into a flow path of a gaseous or liquid heat medium provided on the outer side of the pyrolysis gas reformer, by which the heat medium has Heat, the modification of the thermal decomposition gas generated by the thermal decomposition of the biomass. Thus, in the gasification apparatus of the present invention, the thermal decomposition of the biomass in the biomass thermal decomposition device and the thermal decomposition gas in the thermal decomposition gas reformer are modified by a plurality of preheated particles. The block and/or the block are separately and separately heated from the preheated gas or liquid heat medium, so that the temperature of each can be individually controlled.

In the gasification apparatus of the present invention, the pyrolysis gas introduction pipe is attached to the side of the biomass pyrolysis reactor, and is provided in a plurality of granular and/or bulk layers formed in the thermal decomposition machine, that is, heat. The surface of the upper layer of the carrier layer is located below the surface of the biothermal resolver. That is, on the side of the biothermal decomposition machine, it contains several granular forms formed in the biothermal decomposition machine. The layer of the substance and/or the block is provided with a gas suction port (gas inlet) of the pyrolysis gas introduction pipe. Further, the pyrolysis gas generated in the biomass pyrolyzer is introduced into the pyrolysis gas reformer through the pyrolysis gas introduction pipe. In this way, since the suction port of the pyrolysis gas of the pyrolysis gas introduction pipe is provided in a layer containing a plurality of granules and/or lumps, a plurality of granules present in the biothermal decomposition machine and/or Or a portion of the block may intrude into the interior of the pyrolysis gas introduction pipe, so that the pyrolysis gas introduction pipe may hold a plurality of particles and/or agglomerates therein.

Further, the pyrolysis gas introduction pipe is preferably provided on the side of the biomass pyrolyzer between the biothermal pyrolyzer and the pyrolysis gas reformer, and is disposed substantially horizontally with respect to the gravity direction, and then, toward the pyrolysis gas. The structure in which the reformer rises laterally upward. In this way, since the thermal decomposition gas introduction pipe is disposed substantially horizontally with respect to the gravity direction on the side of the biomass pyrolysis reactor, a plurality of granular materials and/or masses easily intrude into the inside of the thermal decomposition gas introduction pipe, and are thermally decomposed. The plurality of granules and/or lumps held inside the gas introduction tube can flow in the biomass pyrolyzer with a plurality of granules and/or lumps that move by gravity from top to bottom. And gradually replacing a plurality of granules and/or lumps that move from top to bottom. Then, a plurality of granules and/or lumps held inside the pyrolysis gas introduction pipe can be maintained in a new state. On the other hand, the thermal decomposition gas introduction pipe is located downstream of the horizontal pipe, that is, on the side of the pyrolysis gas reformer, and has a structure that rises toward the side of the pyrolysis gas reformer, thereby preventing the inflow of the pyrothermal pyrolyzer. A plurality of granules and/or lumps in the thermal decomposition gas introduction pipe are mixed into the pyrolysis gas reformer. In this way, a plurality of granules and/or lumps are held inside the pyrolysis gas introduction pipe, and thus tar, coal dust, and the like contained in the pyrolysis gas introduced into the pyrolysis gas reformer are A plurality of granules and/or lumps are contacted and captured. Then, part or most of the captured tar is here by number The granules and/or the masses are thermally and thermally decomposed and gasified, preferably modified. Further, tar and coal dust remaining without being gasified remain attached to the bottom of the biomass pyrolyzer in a state of adhering to a plurality of granular materials and/or masses. Thereby, the self-heat decomposition gas such as tar and coal dust can be effectively removed.

The thermal decomposition gas introduction pipe system has a thermal decomposition gas reformer side between the raw material thermal decomposition device and the thermal decomposition gas reformer, and the horizontal pipe extending from the side of the pyrolysis thermal decomposition device faces the thermal decomposition gas reformer upward The structure of the square rise can be. The angle of rise is not particularly limited and is more than 0 degrees (horizontal) and is 90 degrees or less. For example, it may be raised upward at a substantially right angle and connected to the bottom of the pyrolysis gas reformer, or may be slightly raised from the level and connected to the side or bottom of the pyrolysis gas reformer. The angle of the rise is preferably 5 degrees or more, more preferably 10 degrees or more, and more preferably 15 degrees or more. Here, when the angle of the rise is large, for example, when the distance level exceeds 45 degrees, it is preferable that the bottom of the horizontal pipe at the rising portion has a side closer to the pyrolysis gas reformer side than the side of the pyrolysis gas reformer. Preferably, it is a protrusion of 5 to 45 degrees, more preferably 10 to 30 degrees, and further preferably 15 to 25 degrees of inclination angle (θ). Thereby, the replacement of a plurality of granules and/or lumps which invade into the pyrolysis gas introduction pipe can be promoted, and the stagnation of a plurality of granules and/or lumps in the ascending portion can be avoided. In the thermal decomposition gas introduction pipe, the cross section perpendicular to the longitudinal direction, that is, the cross section perpendicular to the flow direction of the pyrolysis gas is preferably substantially circular or substantially polygonal, and more preferably substantially circular. Further, the pyrolysis gas introduction pipe is preferably provided in the range of 1 to 3, more preferably 1 or 2, between the biomass pyrolysis reactor and the pyrolysis gas reformer. Further, even in the gasification device (second device configuration) of the present invention, the pyrolysis gas introduction pipe used in the first device configuration may be disposed substantially horizontally with respect to the gravity direction and the inner bottom surface may protrude upward. Heat The gas introduction pipe is decomposed and used as a thermal decomposition gas introduction pipe. For example, the thermal decomposition gas introduction pipe (II, III, IV, VII, VIII, IX) shown in Fig. 4 can be used. Preferably, the thermal decomposition gas introduction pipe (III, IV, VIII, IX) shown in Fig. 4 can be used. Since the thermal decomposition gas introduction pipe is horizontal and the inner bottom surface is protruded upward, it is possible to effectively prevent the intrusion of a plurality of granular materials and/or massive substances invaded by the pyrothermal pyrolyzer into the thermal decomposition gas reformer. However, in the case of a long time operation, there are cases where a plurality of granules and/or lumps invade into the pyrolysis gas reformer, and therefore, it is preferable to thermally decompose at the protruding portion of the hot decomposition gas introduction pipe. The bottom of the introduction tube on the side of the gas reformer or the inside of the pyrolysis gas reformer is provided with a plurality of granules and/or a block accumulation portion (capture portion), and the accumulated particles are periodically charged as needed. The material and/or the mass are discharged.

In the gasification apparatus of the present invention, a preheater for preheating a plurality of granules and/or lumps is provided on the upper portion of the biomass pyrolyzer. Thereby, the plurality of granules and/or lumps are heated to a predetermined temperature. Further, above the upper part (upper part), preferably the top part of the biomass thermal decomposition device, there are several inlet ports for granules and/or blocks; on the other hand, below the bottom of the biomass thermal decomposition device (bottom part) Preferably, the bottom is provided with a plurality of granules and/or slab outlets. The introduction port and the discharge port of a plurality of granules and/or lumps are, for example, a so-called two-stage valve type in which one valve is provided on the upper and lower sides of the pipe. However, the introduction and release method is an example, and is not limited to this mode. Moreover, even in the above-described accumulation portion (capture portion), it can be released in the same manner. On the other hand, the pyrolysis gas reformer is provided with a flow path of a preheated gas or liquid heat medium on the outside. The thermal decomposition gas reformer may be a conventional heat exchanger type thermal decomposition gas reformer, or may be either a multiple tube type or a double tube type.

Fig. 3 is a view showing the biomass of the present invention comprising the second device in which a plurality of granules and/or lumps which are preheated are supplied to a biomass pyrolyzer only A schematic diagram of one embodiment of the physical device. In the gasification apparatus of the biomass, there is provided a biomass pyrolyzer (3) which is heated by a plurality of granules and/or lumps (7) which are preheated, that is, heat carriers. Performing thermal decomposition of biomass; and heat exchanger type thermal decomposition gas reformer (2), which is generated by thermal decomposition of biomass by heat of a preheated gas or liquid heat medium The thermal decomposition of the gas is modified. Further, a preheater (1) for preheating a plurality of granules and/or lumps (7) is provided on the upper portion of the biomass pyrolyzer (3). Further, a thermal decomposition gas introduction pipe (9) is provided between the biomass pyrolysis reactor (3) and the thermal decomposition gas reformer (2), whereby the biomass thermal decomposition device (3) is produced. The thermal decomposition gas is introduced into the thermal decomposition gas reformer (2). Here, the pyrolysis gas introduction pipe (9) is attached to the side of the biomass pyrolyzer (3) and is provided in a plurality of granules and/or lumps formed in the biothermal decomposition machine (3) ( 7) The side of the upper surface of the layer (13) on the side of the biothermal resolver (3). That is, the bio-thermal separator (3) side gas suction port (gas inlet) (9-3) of the pyrolysis gas introduction pipe (9) is provided in a plurality of granular materials and/or a block (7) layer. . On the other hand, on the side of the pyrolysis gas reformer (2), the pyrolysis gas introduction pipe (9) is connected to the bottom of the pyrolysis gas reformer (2). Further, the pyrolysis gas introduction pipe (9) is disposed substantially horizontally with respect to the gravity direction on the side of the biomass pyrolyzer (3), and rises substantially perpendicularly toward the thermal decomposition gas reformer (2) on the downstream side thereof. Further, at the bottom of the horizontal pipe at the rising portion, an inclination angle (θ) of approximately 25 degrees from the bottom of the horizontal pipe to the side of the pyrolysis gas reformer (2) toward the pyrolysis gas reformer (2) is provided. The prominent part.

A plurality of granules and/or lumps (7), ie heat carriers, are supplied to the preheater provided above the biomass pyrolyzer (3) before being introduced into the biomass pyrolyzer (3) ( 1) is heated in advance. In the preheater (1) equipped on the upper portion of the biothermal pyrolyzer (3), the heat carrier (7) is preferably heated to 700 to 800 ° C, more preferably 750 to 800 ° C. If not When the lower limit is exceeded, there is a case where the biomass cannot be sufficiently thermally decomposed in the biomass pyrolyzer (3). Even if the above upper limit is exceeded, as described in the description of Fig. 1 above, the amount of steam injected into the biothermal pyrolyzer (3) can be changed to a reasonable temperature, thereby efficiently performing the heat of the biomass. break down. However, it is preferred to further increase the thermal efficiency by setting the temperature of the heat carrier (7) to be equal to or lower than the above upper limit.

In Fig. 3, the pyrolysis gas reformer (2) is a so-called heat exchanger type pyrolysis gas reformer. The thermal decomposition gas system introduced by the thermal decomposition gas introduction pipe (9) is mixed with the steam introduced from the steam injection inlet (11 ₂ ) and introduced into the jacket of the heat exchanger type thermal decomposition gas reformer (2). The heat medium, for example, high temperature hot air, is heat exchanged to be modified. The conditions of the gas phase temperature and pressure in the heat exchanger type thermal decomposition gas reformer (2) are the same as those shown in Fig. 1. Here, the gas phase temperature of the heat exchanger type pyrolysis gas reformer (2) means the gas phase temperature in the vicinity of the reformed gas discharge port (8) in the upper portion of the pyrolysis gas reformer (2). The gas phase temperature can be appropriately changed by the amount of the pyrolysis gas supplied from the steam injection port (11), and the amount of steam introduced from the steam injection port (11 ₂ , 11 ₃ ) can be appropriately changed by the pyrolysis gas. The temperature and flow rate of the jacketed heat medium of the massifier (2) are controlled.

Hereinafter, the present invention will be described in detail by way of examples, but the invention is not limited by the examples.

(Example) (Example 1)

The raw material used in Example 1 and the gasification apparatus for thermal decomposition and gas reforming of the raw material are as follows.

As a raw material for raw materials, construction waste wood is used. Smash the waste wood After use. The size of the shredded waste wood is the size of the sawdust, and the maximum size is about 2~6mm. The properties of the waste wood are shown in Table 1.

With respect to each value of Table 1, the moisture is measured according to JIS Z 7302-3:2009, the ash is obtained according to JIS Z 7302-4:2009, and the volatile component is determined according to JIS M 8812-7:2006. The high calorific value was measured in accordance with JIS Z 7302-2:1999.

Further, in the elemental composition, carbon (C), hydrogen (H), and nitrogen (N) are measured according to JIS Z 7302-8:2002, and sulfur (S) is determined according to JIS Z 7302-7:2002. And chlorine (C1) is measured according to JIS Z 7302-6:1999.

Further, oxygen (O) was obtained by subtracting each mass% of C, H, N, S, Cl, and ash from 100% by mass.

Here, the ash, the volatile component, the fixed carbon, and the elemental composition are all calculated by the drying standard. Further, the moisture is the one that receives the raw material.

As the gasification apparatus for the thermal decomposition of the raw material and the reformation of the generated thermal decomposition gas, the one shown in Fig. 1 is used. This gasification apparatus has a device in which a biomass pyrolyzer (3) and a pyrolysis gas reformer (2) are arranged side by side with respect to the flow of the heat carrier (7). A preheater (1) is provided on the upper part of the raw pyrolysis reactor (3) and the pyrolysis gas reformer (2), and the preheater (1) is supplied to the biothermal decomposition machine ( 3) The heat carrier (7) of both the thermal decomposition gas reformer (2) is preheated at one time. The biothermal pyrolyzer (3) has an inner diameter of about 180 mm, a height of about 1,000 mm, and an internal volume of about 25 liters. Further, the thermal decomposition gas reformer (2) has an inner diameter of about 180 mm, a height of about 2,350 mm, and an internal volume of about 60 liters. Further, as the pyrolysis gas introduction pipe (9), the structure shown in Fig. 4 (VIII) is used. Here, the angle (θ) of the inclination of the protruding portion is 25 degrees on both sides. The thermal decomposition gas introduction pipe (9) is disposed on both sides of the biomass thermal decomposition device (3) and the thermal decomposition gas reformer (2), and is disposed on the biomass thermal decomposition device (3) and the pyrolysis gas, respectively. The surface of the upper surface (13) of the heat carrier (7) in the reformer (2) is located on the side of the biomass pyrolyzer (3) and the thermal decomposition gas reformer (2). Further, the pyrolysis gas introduction pipe (9) is provided substantially horizontally with respect to the direction of gravity. The thermal decomposition gas introduction pipe (9) has a length of about 500 mm, a cross section perpendicular to the longitudinal direction, that is, a substantially square shape having a side length of 180 mm with respect to a cross section perpendicular to the flow direction of the pyrolysis gas, and the pyrolysis gas is introduced. The width (height) of the vertical direction of the gas suction port of the tube (h ₁ ) and the width (height) of the vertical direction of the gas introduction port (h ₂ ) are both 150 mm. As the heat carrier (7), a substantially spherical alumina ball having a diameter (maximum diameter) of 10 to 12 mm is used.

The heat carrier (7) is pre-filled to a height of about 70% of each container in the thermal decomposition device (3), the thermal decomposition gas reformer (2), and the preheater (1), and then, The heat carrier (7) is heated in the preheater (1) to a temperature of approximately 500 °C. Then, the top of the heat carrier (7) from the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) are individually introduced in an amount of 30 kg/hr, and the autothermal decomposition machine (3) The bottom of the thermal decomposition gas reformer (2) is separately released in an appropriate amount to start the circulation of the heat carrier (7). By the circulation of the heat carrier (7), the temperature of the gas phase inside the biothermal pyrolyzer (3) and the pyrolysis gas reformer (2) and the temperature of the vessel itself gradually rise. While continuing the circulation of the heat carrier (7), the temperature of the heat carrier (7) inside the preheater (1) was gradually raised to 1,050 °C. After the heat carrier (7) reaches the temperature, the circulation is further continued, and the gas phase temperature inside the biothermal pyrolyzer (3) and the pyrolysis gas reformer (2) is gradually increased, and the biomass thermal decomposition device ( 3) After the gas phase temperature exceeds 600 ° C, the raw material supply port (4), the non-oxidizing gas supply port (12), and the steam injection port (11 ₁ ) are respectively introduced into the raw material thermal decomposition device (3). Nitrogen and steam were controlled so that the temperature of the biomass pyrolyzer (3) became 600 °C. On the other hand, the vapor phase temperature of the pyrolysis gas reformer (2) is 950 ° C, and steam is introduced from the steam injection port (11 ₂ ) to control. At this time, the heat carrier (7) is in the biomass thermal decomposition device (3) and the thermal decomposition gas reformer (2), and is deposited layer by layer, and the deposition amount is a biomass thermal decomposition device (3) and The thermal decomposition gas reformer (2) has a volume content of about 60% by volume. The heat carrier (3) of the autogenic thermal decomposition device (3) and the thermal decomposition gas reformer (2) are released in the same amount as the supply amount, and are in the thermal decomposition device (3) and the thermal decomposition gas reformer. (2), respectively, 30 kg / hour. Further, the temperature of the heat carrier (7) at the time of discharge was 400 °C. However, the amount of release of the heat carrier (7) of the autothermal decomposition machine (3) and the pyrolysis gas reformer (2) can be individually controlled according to the temperature conditions of each.

In the above operation, the waste wood used as the raw material of the raw material is used, and the dosing feeder is used, and the self-generating supply port (4) is gradually increased to the biomass pyrolyzer (3), and the amount is gradually increased to about 4 The kg/hour (dry basis) is continuously introduced. The temperature of the biothermal pyrolyzer (3) is gradually reduced with the introduction of the raw material, but the nitrogen and superheated steam are simultaneously introduced into the biothermal pyrolyzer (3) while adjusting the supply amount thereof. The temperature of the thermal decomposition machine (3) was maintained at 600 °C. Further, the pressure in the biothermal pyrolyzer (3) was maintained at 101.3 kPa. Here, nitrogen gas is introduced from a non-oxidizing gas supply port (12) provided above the biomass pyrolyzer (3) at a final fixed amount of 60 liters/hour. Further, as the steam, superheated steam (160 ° C, 0.6 MPa) was used, and the steam injection port (11 ₁ ) provided in the upper portion of the biomass pyrolyzer (3) was introduced at a final fixed amount of 2 kg/hour. The residence time of the raw material in the biothermal pyrolyzer (3) is about 1 hour. Thereby, a gas generated by thermal decomposition in the biothermal decomposition machine (3) was obtained at 5.2 kg/hr. Further, carbon was discharged at a rate of 0.8 kg/hr from the thermal decomposition residue (carbon) discharge port (6).

The thermal decomposition gas obtained in the thermal decomposition machine (3) is then introduced into the thermal decomposition gas reforming unit (2) maintained at the above temperature through the thermal decomposition gas introduction pipe (9) at the lower portion of the autothermal decomposition machine (3). . At the beginning of the introduction of the thermal decomposition gas, the temperature in the biothermal pyrolyzer (3) becomes unstable, but by the steam injection port (11 ₂ ) provided at the lower portion of the pyrolysis gas reformer (2) The superheated steam (160 ° C, 0.6 MPa) was adjusted while adjusting the amount thereof, and the temperature was adjusted to 950 ° C. At this time, the pyrolysis gas reformer (2) was maintained at a pressure of 101.3 kPa. The superheated steam from the steam injection port (11 ₂ ) provided at the lower portion of the pyrolysis gas reformer (2) was introduced at a fixed amount of 2 kg/hr.

By the above operation, the biomass pyrolyzer (3) is maintained at a temperature of 600 ° C and a pressure of 101.3 kPa, and the pyrolysis gas reformer (2) is maintained at a temperature of 950 ° C and The pressure is 101.3 kPa. Thereby, a reforming gas having a temperature of 950 ° C was obtained from the reforming gas outlet (8) in an amount of 7.2 kg/hr.

The obtained modified gas was trapped in a rubber bag, and the gas composition was measured by a gas chromatograph [GC-14A (trademark) manufactured by Shimadzu Corporation). In Table 2, the composition of the modified gas obtained is shown. Moreover, this operation can be carried out for 3 consecutive days. During this operation, good continuous operation without failure, especially without tar-induced failure, can be maintained. Further, during the operation period, the heat carrier (7) is not blocked by the tar or the like in the thermal decomposition gas introduction pipe (9), thereby maintaining the pyrolysis thermal decomposition device (3) to the thermal decomposition gas reformer ( 2) The smooth introduction of the thermal decomposition gas. Further, the amount of tar in the reformed gas taken out from the outlet (8) of the thermal decomposition gas reformer (2) is about 0.5 g/m ³ -normal.

(Example 2)

The raw material used in Example 2 and the gasification apparatus for thermal decomposition and gas reforming of the raw material are as follows.

As a raw material for raw materials, oil palm waste materials are used. The waste material was coarsely pulverized and used. The oil palm waste material has a shape in which a plurality of soft strips having a thickness of about 1 to 2 mm and a length of about 3 to 30 mm are overlapped, in other words, as cotton. The form of the yarn is scattered. When it is roughly pulverized, it has a shape like a ball (fiber ball), and its maximum size is about 0 to 30 mm. The properties of the waste material are shown in Table 3.

With respect to each value of Table 3, the moisture is measured according to JIS Z 7302-3:2009, and the ash is obtained according to JIS Z 7302-4:2009, and the volatile component is based on JIS M 8812-7:2006, and high fever The amount is determined according to JIS Z 7302-2:1999.

Further, in the elemental composition, carbon (C), hydrogen (H) and nitrogen (N) are obtained according to JIS Z 7302-8:2002, and sulfur (S) is determined according to JIS Z 7302-7:2002. The chlorine (C1) was measured in accordance with JIS Z 7302-6:1999.

Further, oxygen (O) was obtained by subtracting each mass% of C, H, N, S, Cl, and ash from 100% by mass.

Here, the ash, the volatile component, the fixed carbon, and the elemental composition are all calculated by the drying standard. Further, the moisture is the one that receives the raw material.

The gasification apparatus for thermal decomposition and gas upgrading of the raw material is the same as that of the user in the first embodiment, and the one shown in Fig. 1 is used.

The temperatures of the pyrolysis gas reformer (2) and the biomass pyrolyzer (3) were set to 950 ° C and 600 ° C, respectively, by the same conditions and operation methods as in Example 1. Further, the temperature of the heat carrier (7) at the time of discharge was 400 °C.

In the operation of controlling the temperature of the pyrolysis gas reformer (2) and the biomass pyrolyzer (3) to the above-mentioned predetermined value, the oil palm waste material used as the raw material raw material is supplied by a dosing device and a self-generating material. The mouth (4) is continuously introduced into the biomass pyrolyzer (3) while gradually increasing the amount of supply on one side and finally becoming about 5 kg/hr (dry basis). The temperature of the biothermal pyrolyzer (3) is gradually reduced with the introduction of the raw material, but the nitrogen and superheated steam are simultaneously introduced into the biothermal pyrolyzer (3) while adjusting the supply amount thereof. The temperature of the thermal decomposition machine (3) was maintained at 600 °C. Further, the pressure in the biothermal pyrolyzer (3) was maintained at 101.3 kPa. Here, nitrogen gas is introduced from a non-oxidizing gas supply port (12) provided in the upper portion of the biothermal pyrolyzer (3), and is introduced at a final fixed amount of 6 liters/hour. Further, as the steam, superheated steam (160 ° C, 0.6 MPa) was used, and the steam injection port (11 ₁ ) provided in the upper portion of the biomass pyrolyzer (3) was introduced at a final fixed amount of 2 kg/hour. The residence time of the raw material in the biothermal pyrolyzer (3) is about 1 hour. Thereby, a gas generated by thermal decomposition in the biothermal pyrolyzer (3) was obtained at 6.1 kg/hr. Further, carbon was discharged at a rate of 0.9 kg/hr from the thermal decomposition residue (carbon) discharge port (6).

The thermal decomposition gas obtained in the thermal decomposition machine (3) is then introduced into the thermal decomposition gas introduction pipe (9) through the thermal decomposition gas introduction pipe (9), and is introduced into the thermal decomposition gas maintained at a temperature of 950 ° C and a pressure of 101.3 kPa. Quality device (2). At the beginning of the introduction of the pyrolysis gas, the temperature in the biothermal pyrolyzer (3) becomes unstable, but by the steam injection port (11 ₂ ) provided at the lower portion of the pyrolysis gas reformer ( ₂ ), The superheated steam (160 ° C, 0.6 MPa) was adjusted while being adjusted while being adjusted to a temperature of 950 ° C. At this time, the pyrolysis gas reformer (2) was maintained at a pressure of 101.3 kPa. The superheated steam from the steam injection port (11 ₂ ) provided at the lower portion of the pyrolysis gas reformer (2) was introduced at a final fixed amount of 3 kg/hr.

By the above operation, the biomass pyrolyzer (3) was maintained at a temperature of 600 ° C and a pressure of 101.3 kPa, and the pyrolysis gas reformer (2) was maintained at a temperature of 950 ° C and a pressure of 101.3 kPa. Thereby, a reforming gas having a temperature of 950 ° C was obtained from the reforming gas outlet (8) in an amount of 9.1 kg/hr.

The obtained modified gas was trapped in a rubber bag, and the gas composition was measured by a gas chromatograph [GC-14A (trademark) manufactured by Shimadzu Corporation). The composition of the modified gas obtained is shown in Table 4. Moreover, this operation can be carried out for 3 consecutive days. During this operation, good continuous operation without failure, especially without tar-induced failure, can be maintained. Further, during the operation period, the heat carrier (7) is not blocked by the tar or the like in the thermal decomposition gas introduction pipe (9), thereby maintaining the pyrolysis thermal decomposition device (3) to the thermal decomposition gas reformer ( 2) The smooth introduction of the thermal decomposition gas. Further, the amount of tar in the reformed gas taken out from the outlet (8) of the thermal decomposition gas reformer (2) is about 0.5 g/m ³ -normal.

[Table 4]

(Example 3)

The raw material used was the same as that of the user in Example 1. Further, the gasification apparatus for thermal decomposition and gas upgrading of the raw material is used as shown in Fig. 2 . The apparatus to be used is constituted by a device in which the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) are arranged side by side with respect to the flow of the heat carrier (7). A preheater (1 ₂ , 1 ₁ ) is provided in each of the upper part of the thermal decomposition device (3) and the thermal decomposition gas reformer (2), and the preheater (1 ₂ , 1 _{1 )} In the above, the heat carrier (7) supplied to the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) is separately heated in advance. Further, the size and capacity of the biomass pyrolysis device (3) and the pyrolysis gas reformer (2), the shape and size of the pyrolysis gas introduction pipe (9), and the pyrolysis gas introduction pipe (9) with respect to gravity The direction is substantially horizontally arranged, and the material and size of the heat carrier (7), and other systems are the same as in the first embodiment.

The heat carrier (7) is pre-filled to a height of about 70% of each container in the thermal decomposition device (3), the thermal decomposition gas reformer (2), and the preheater (1 ₂ , 1 ₁ ). Then, the heat carrier (7) is heated in advance to a temperature of approximately 500 ° C in each of the preheaters (1 ₂ , 1 ₁ ). Then, the tops of each of the heat carrier (7) autogenic pyrolyzer (3) and the pyrolysis gas reformer (2) are individually introduced in an amount of 30 kg/hr, and the autothermal decomposition device (3) The bottom of the thermal decomposition gas reformer (2) is separately released in an appropriate amount to start the circulation of the heat carrier (7). By the circulation of the heat carrier (7), the temperature of the gas phase inside the biothermal pyrolyzer (3) and the pyrolysis gas reformer (2) and the temperature of the vessel itself gradually rise. While continuing the circulation of the heat carrier (7), the temperature of the heat carrier (7) inside the preheater (1 ₂ ) was gradually raised to 800 ° C. On the other hand, the temperature of the heat carrier (7) inside the preheater (1 ₁ ) was gradually raised to 1,050 °C. After the respective heat carriers (7) reach the above temperature, further, the circulation is continued to gradually increase the gas phase temperature inside the biomass pyrolyzer (3) and the pyrolysis gas reformer (2), and the thermal decomposition of the biomass After the gas phase temperature of the device (3) exceeds 600 ° C, the pyrolysis supply port (4), the non-oxidizing gas supply port (12), and the steam injection port (11 ₁ ) are introduced into the biomass pyrolyzer (3), respectively. The raw material, nitrogen gas and steam were controlled so that the temperature of the biomass pyrolyzer (3) became 600 °C. On the other hand, the vapor phase temperature of the pyrolysis gas reformer (2) is 950 ° C, and steam is introduced from the steam injection port (11 ₂ ) to control. At this time, the heat carrier (7) is deposited layer by layer in the biomass pyrolysis reactor (3) and the thermal decomposition gas reformer (2), and the deposition amount thereof is a biomass thermal decomposition device (3) and heat. About 60% by volume of the internal volume of each of the decomposition gas reformers (2). The heat carrier (3) of the autogenic thermal decomposition device (3) and the thermal decomposition gas reformer (2) are released in the same amount as the supply amount, and are in the thermal decomposition device (3) and the thermal decomposition gas reformer. (2), respectively, 30 kg / hour. Further, the temperature of the heat carrier (7) at the time of discharge was 400 °C.

In the above operation, the waste wood used as the raw material of the raw material is used, and the dosing feeder is used, and the self-generating supply port (4) is gradually increased to the biomass pyrolyzer (3), and the amount is gradually increased to about 4 The kg/hour (dry basis) is continuously introduced. The temperature of the biothermal pyrolyzer (3) is gradually reduced with the introduction of the raw material, but the nitrogen and superheated steam are simultaneously introduced into the biothermal pyrolyzer (3) while adjusting the supply amount thereof. The temperature of the thermal decomposition machine (3) was maintained at 600 °C. Further, the pressure in the biothermal pyrolyzer (3) was maintained at 101.3 kPa. Here, nitrogen gas is introduced from a non-oxidizing gas supply port (12) provided above the biomass pyrolyzer (3) at a final fixed amount of 60 liters/hour. Further, as the steam, superheated steam (160 ° C, 0.6 MPa) was used, and the steam injection port (11 ₁ ) provided in the upper portion of the biomass pyrolyzer (3) was introduced at a final fixed amount of 2 kg/hour. The residence time of the raw material in the biothermal pyrolyzer (3) is about 1 hour. Thereby, a gas generated by thermal decomposition in the biothermal decomposition machine (3) was obtained at 5.2 kg/hr. Further, carbon was discharged at a rate of 0.8 kg/hr from the thermal decomposition residue (carbon) discharge port (6).

The thermal decomposition gas obtained in the thermal decomposition machine (3) is then introduced into the thermal decomposition gas reforming unit (2) maintained at the above temperature through the thermal decomposition gas introduction pipe (9) at the lower portion of the autothermal decomposition machine (3). . At the beginning of the introduction of the thermal decomposition gas, the temperature in the thermal decomposition gas reformer (2) becomes unstable, but by the steam injection port (11 ₂ ) provided at the lower portion of the pyrolysis gas reformer ( ₂ ), Further, the superheated steam (160 ° C, 0.6 MPa) was introduced while adjusting the amount thereof, and was adjusted so as to have a temperature of 950 ° C. At this time, the pyrolysis gas reformer (2) was maintained at a pressure of 101.3 kPa. The superheated steam from the steam injection port (11 ₂ ) provided at the lower portion of the pyrolysis gas reformer (2) was introduced at a fixed amount of 2 kg/hr.

By the above operation, the biomass pyrolyzer (3) was maintained at a temperature of 600 ° C and a pressure of 101.3 kPa, and the pyrolysis gas reformer (2) was maintained at a temperature of 950 ° C and a pressure of 101.3 kPa. Thereby, a reforming gas having a temperature of 950 ° C was obtained from the reforming gas outlet (8) in an amount of 7.2 kg/hr.

The obtained modified gas was trapped in a rubber bag, and the gas composition was measured by a gas chromatograph [GC-14A (trademark) manufactured by Shimadzu Corporation). The composition of the modified gas obtained is shown in Table 5. Moreover, this operation can be carried out for 3 consecutive days. During this operation, good continuous operation without failure, especially without tar-induced failure, can be maintained. Further, during the operation period, the heat carrier (7) is not blocked by the tar or the like in the thermal decomposition gas introduction pipe (9), thereby maintaining the pyrolysis thermal decomposition device (3) to the thermal decomposition gas reformer ( 2) The smooth introduction of the thermal decomposition gas. Further, the amount of tar in the reformed gas taken out from the outlet (8) of the thermal decomposition gas reformer (2) is about 0.5 g/m ³ -normal.

(Example 4)

The raw material used was the same as that of the user in Example 1. Further, the gasification apparatus for thermal decomposition and gas upgrading of the raw material is used as shown in Fig. 3 . The apparatus used is in the biothermal pyrolyzer (3), which thermally decomposes the biomass by the heat of the heat carrier (7) and is in the heat exchanger type thermal decomposition gas reformer (2). The gas generated by the thermal decomposition of the biomass is modified by a gaseous heat medium, that is, high-temperature hot air. Further, the size and capacity of the biomass pyrolysis device (3) and the pyrolysis gas reformer (2), and the material and size of the heat carrier (7) are the same as in the first embodiment. The thermal decomposition gas introduction pipe (9) is attached to the side of the biomass pyrolyzer (3) and is disposed below the upper surface (13) of the heat carrier (7) layer formed in the biothermal decomposition device (3). The side of the biothermal resolver (3). On the other hand, on the side of the pyrolysis gas reformer (2), the pyrolysis gas introduction pipe (9) is connected to the bottom of the pyrolysis gas reformer (2). Thermal decomposition gas introduction pipe (9) is attached to the thermal decomposition machine (3) The side is arranged substantially horizontally with respect to the direction of gravity, and rises substantially vertically toward the bottom of the pyrolysis gas reformer (2) on its downstream side. Further, at the bottom of the horizontal pipe at the rising portion, the side of the autothermal pyrolyzer (3) is provided toward the thermal decomposition gas reformer (2) side and has an inclination angle (θ) of approximately 25 degrees from the bottom of the horizontal pipe. Highlights. The thermal decomposition gas introduction pipe (9) has a length of about 1,000 mm (horizontal portion: about 500 mm, rising portion: about 500 mm), and a cross section perpendicular to the longitudinal direction, that is, a cross section perpendicular to the flow direction of the pyrolysis gas. The outline is approximately square with a length of 180 mm.

Inside the raw pyrolysis machine (3) and the preheater (1), the heat carrier (7) is pre-filled to a height of about 70% of each container, and then the heat carrier (7) is placed in the preheater. (1) Heating to a temperature of 500 °C. Then, the heat carrier (7) is introduced into the top of the pyrolysis pyrolyzer (3) at a rate of 30 kg/hr, and an appropriate amount is released from the bottom of the autothermal pyrolyzer (3) to start the heat carrier (7). The cycle. By the circulation of the heat carrier (7), the temperature of the gas phase inside the raw pyrolysis reactor (3) and the temperature of the container itself gradually rise. While continuing the circulation of the heat carrier (7), the temperature of the heat carrier (7) inside the preheater (1) was gradually raised to 800 °C. After the heat carrier (7) reaches the temperature, further, the circulation is continued to gradually increase the gas phase temperature inside the raw pyrolysis reactor (3), and the gas phase temperature of the biomass pyrolyzer (3) exceeds 600 °C. Thereafter, the raw material supply port (4), the non-oxidizing gas supply port (12), and the steam injection port (11 ₁ ) are respectively introduced into the raw material thermal decomposition device (3) into raw materials, nitrogen gas, and steam, and the biomass is produced. The temperature of the thermal decomposition device (3) was controlled to be 600 °C. On the other hand, in the thermal decomposition gas reformer (2), one side of the hot medium inlet (10 ₁ ) is sprayed with a high-temperature hot air of 1,200 ° C in an amount of about 2 m ³ /hour, and a thermal decomposition gas reformer is used. (2) The gas phase temperature is 950 ° C, and further, steam is introduced from the steam injection port (11 ₂ ) for control. At this time, the heat carrier (7) is deposited layerwise in the biomass pyrolyzer (3), and is deposited in an amount of about 60% by volume of the internal volume of the biomass pyrolyzer (3). The amount of the heat carrier (7) released from the pyrolysis pyrolyzer (3) was the same as the amount supplied, and was 30 kg/hr in the biomass pyrolyzer (3). Further, the temperature of the heat carrier (7) at the time of discharge was 400 °C.

In the above operation, the construction waste wood used as the raw material of raw material is gradually increased by the amount of supply from the raw material supply port (4) to the biomass pyrolysis device (3), and finally becomes about 4 The kg/hour (dry basis) is continuously introduced. The temperature of the biothermal pyrolyzer (3) is gradually reduced with the introduction of the raw material, but the nitrogen and superheated steam are simultaneously introduced into the biothermal pyrolyzer (3) while adjusting the supply amount thereof. The temperature of the thermal decomposition machine (3) was maintained at 600 °C. Further, the pressure in the biothermal pyrolyzer (3) was maintained at 101.3 kPa. Here, the nitrogen gas is introduced from the non-oxidizing gas supply port (12) provided above the biomass pyrolyzer (3) at a final fixed amount of 60 liters/hour. Further, as the steam, superheated steam (160 ° C, 0.6 MPa) was used, and the steam injection port (11 ₁ ) provided in the upper portion of the biomass pyrolyzer (3) was introduced at a final fixed amount of 2 kg/hour. The residence time of the raw material in the biothermal pyrolyzer (3) is about 1 hour. Thereby, a gas generated by thermal decomposition in the biothermal pyrolyzer (3) was obtained at 5.1 kg/hr. Further, carbon was discharged at a rate of 0.9 kg/hr from the thermal decomposition residue (carbon) discharge port (6).

The thermal decomposition gas obtained in the biomass thermal decomposition device (3) is then introduced into the heat exchanger type thermal decomposition gas reformer (2) through the thermal decomposition gas introduction pipe (9) through the lower portion of the pyrolysis thermal decomposition device (3). In the pyrolysis gas reformer (2), a high-temperature hot air heated to about 1,200 ° C in advance is introduced from the high-temperature hot air inlet (10 ₁ ) to the heat medium flow provided on the outer side of the pyrolysis gas reformer (2). The road is heat-exchanged with the pyrolysis gas flowing inside the pyrolysis gas reformer (2), and then discharged from the high-temperature hot air outlet (10 ₂ ) at about 700 °C. At the beginning of the introduction of the thermal decomposition gas, the temperature in the thermal decomposition gas reformer (2) becomes unstable, but the amount of the high-temperature hot air is gradually increased while being adjusted, and is set in the thermal decomposition gas reformer ( 2) The lower steam injection port (11 ₂ ) is introduced while adjusting the amount of superheated steam (160 ° C, 0.6 MPa), and the temperature in the thermal decomposition gas reformer ( 2 ) is adjusted to 950 ° C. At this time, the pyrolysis gas reformer (2) was maintained at a pressure of 101.3 kPa. The superheated steam from the steam injection port (11 ₂ ) provided at the lower portion of the pyrolysis gas reformer (2) was introduced at a final fixed amount of 2 kg/hr.

By the above operation, the biomass pyrolyzer (3) was maintained at a temperature of 600 ° C and a pressure of 101.3 kPa, and the pyrolysis gas reformer (2) was maintained at a temperature of 950 ° C and a pressure of 101.3 kPa. Thereby, a reforming gas having a temperature of 900 ° C was obtained from the reforming gas outlet (8) in an amount of 7.1 kg/hr.

The obtained modified gas was trapped in a rubber bag, and the gas composition was measured by a gas chromatograph [GC-14A (trademark) manufactured by Shimadzu Corporation). The composition of the modified gas obtained is shown in Table 6. Moreover, this operation can be carried out for 3 consecutive days. During this operation, good continuous operation without failure, especially without tar-induced failure, can be maintained. Further, during the operation period, the heat carrier (7) is not blocked by the tar or the like in the thermal decomposition gas introduction pipe (9), thereby maintaining the pyrolysis thermal decomposition device (3) to the thermal decomposition gas reformer ( 2) The smooth introduction of the thermal decomposition gas. Further, the amount of tar in the reformed gas taken out from the outlet (8) of the thermal decomposition gas reformer (2) was about 0.8 g/m ³ -normal.

[Table 6]

(Comparative Example 1)

As a gasification apparatus used for the thermal decomposition of a raw material raw material, and the modification of the thermal decomposition gas generate|occur|produce, it is set as FIG. That is, it is a device which is provided in the upper part of the thermal decomposition zone (200), and has the modified region (300) in the up-and-down arrangement. In other words, the device is a device in which a biomass pyrolyzer and a pyrolysis gas reformer are connected in series. In the comparative example, about one-tenth of the experimental small device of the actual machine was used. The gasification apparatus used is as shown in FIG. The material of the gasifier (A) body is a nickel-chromium alloy. The gasification furnace (A) is a cylindrical shape having an inner diameter of 100 mm and a height of 650 mm, and 300 mm apart from the bottom of the gasification furnace (A) is a thermal decomposition region (200), and 300 mm from the top is a modified region (300). In the thermal decomposition zone (200), alumina balls (D) (5 to 15 mm in diameter) were used as the heat medium. The upper portion of the modified region (300) is filled with a nickel catalyst (E). A steam introduction port (400) is provided between the thermal decomposition zone (200) and the modified zone (300). Further, electric heaters (B) and (C) capable of temperature control are provided on the outer wall of the gasification furnace in the thermal decomposition zone (200) and the reforming zone (300).

As the raw material, the same construction waste wood as in Example 1 was used. The raw material is supplied from the raw material supply pipe (100) by the airflow, and is intermittently introduced into the thermal decomposition zone (200) of the gasification furnace (A) every 0.11 g at intervals of 30 to 40 seconds. The thermal decomposition zone (200) of the gasification furnace (A) uses oxygen as a heat medium by using an electric heater (B) The aluminum ball is heated and controlled at a temperature of 550 °C. Further, the thermal decomposition zone (200) was introduced into the helium gas at 0.50 liter/min from the bottom (600) to maintain the pressure at 0.103 MPa. The gas system generated by thermally decomposing the waste wood is introduced into a reforming zone (300) of the gasification furnace (A) maintained at the same pressure, and mixed with steam.

The temperature of the reforming zone (300) of the gasification furnace (A) was 1,000 ° C, and the temperature of the gas in the outlet portion (500) of the reforming zone (300) was 947 °C. The temperature of the modified region (300) is controlled to be constant by the electric heater (C). The composition of the resulting reformed gas is shown in Table 7. Further, the amount of tar in the reformed gas on the outlet side of the modified region (300) is about 5 g/m ³ -normal. In this apparatus, the operation can be carried out for three consecutive days, but since the second day has elapsed, the pressure in the thermal decomposition zone (200) slightly starts to rise. After the end of the operation, the alumina ball (D) layer was inspected to confirm the deposition of the tar. Therefore, it is presumed that there is a problem in continuous operation for a long time.

Examples 1 and 2 are those in which the raw material is changed. Even if any raw material can continue to perform a good continuous operation without tar-induced failure during the operation period, it does not cause a failure of the heat carrier (7) to be blocked by tar or the like in the pyrolysis gas introduction pipe (9). Thereby, the smooth introduction of the pyrolysis gas of the pyrolysis thermodecomposer (3) to the pyrolysis gas reformer (2) is maintained. Moreover, the amount of tar in the resulting reformed gas is extremely small. In the third embodiment, a gasification device is provided which is separately provided with a preheater (1 ₂ , 1 ) on the upper part of the biomass pyrolyzer ( 3 ) and the pyrolysis gas reformer ( 2 ). ₁ ), and heating the heat carrier (7) to different temperatures, and then supplying to the biomass pyrolyzer (3) and the pyrolysis gas reformer (2). In the same manner as in Examples 1 and 2, good operation was ensured, and the amount of tar in the obtained reformed gas was extremely small. In the fourth embodiment, a heat exchanger type reformer heated by high-temperature hot air is used as the thermal decomposition gas reformer (2). Good operation can be ensured in the same manner as in the first to third embodiments. Further, although the amount of tar in the obtained reformed gas is slightly increased, it does not hinder the smooth operation of the apparatus. Comparative Example 1 used a conventional device. The deposition of tar on the alumina ball (D) layer can be confirmed, so that there is a problem in continuous operation for a long time. Further, according to the results of Examples 1 to 4 and Comparative Example 1, it is understood that the reformed gas compositions are substantially equal in any of the examples, and if the gasification apparatus of the present invention is used, the conventional vertical tandem two-stage gas can be used. The furnace is gasified to the same extent. Further, the amount of tar in the reformed gas is remarkably reduced in the apparatus of the present invention, and it is useful to exhibit a gasification apparatus as a raw material.

(industrial availability)

According to the biomass gasification device of the present invention, by optimizing the thermal decomposition temperature of the biomass and the reforming temperature of the generated thermal decomposition gas, not only the amount of thermal decomposition gas can be increased, but also The production amount of the hydrogen-containing gas as the final product is increased, and the amount of tar and coal dust generated can be reduced. Further, the generated tar is effectively gasified, and the tar and coal dust remaining without being gasified are efficiently recovered, whereby the malfunction of the device due to tar and coal dust can be remarkably reduced. Therefore, the gasification apparatus of the present invention is expected to be widely used for gasification of biomass in the future. Further, the present invention is also expected to be utilized in a hydrogen production business and a power generation business.

1‧‧‧Preheater

2‧‧‧ Thermal decomposition gas reformer

3‧‧‧Biomass thermal decomposition machine

4‧‧‧ Raw material supply port

5‧‧‧Exhaust disposal device

6‧‧‧ Thermal decomposition residue (carbon) discharge

7‧‧‧Several granules and / or lumps [heat carrier medium (heat carrier)]

8‧‧‧Modified gas discharge

9‧‧‧ Thermal decomposition gas introduction tube

9-2‧‧‧The thermal decomposition gas introduction side gas inlet port (gas outlet) of the thermal decomposition gas introduction pipe

9-3‧‧‧The gas inlet (gas inlet) of the thermal decomposition device side of the thermal decomposition gas introduction pipe

11 ₁ , 11 ₂ , 11 ₃ ‧ ‧ steam injection

12‧‧‧ Non-oxidizing gas supply port

13‧‧‧ Surfaces on the surface of several granular and/or bulk layers formed in the thermal decomposition reactor and the thermal decomposition gas reformer

Claims (12)

A biomass gasification device comprising: a biomass pyrolysis device having a raw material supply port, a non-oxidizing gas supply port and/or a steam injection port; and a thermal decomposition gas reformer having a steam injection port And a reformed gas discharge port; and a pyrolysis gas introduction pipe that introduces the pyrolysis gas generated in the biomass pyrolysis device to the pyrolysis gas reformer, and is provided in the biomass pyrolysis device and the heat And separating the gas thermal reformer and the pyrolysis gas reformer, respectively, further comprising an introduction port and a discharge port of the plurality of granular materials and/or blocks heated in advance, The thermal decomposition of the biomass and the thermal decomposition gas generated by the thermal decomposition of the biomass are performed by the heat of the plurality of granules and/or the masses, and the gasification device of the biomass is The pyrolysis gas decomposer and the pyrolysis gas reformer are arranged side by side with respect to the flow of the plurality of granular materials and/or the mass, and the pyrolysis gas introduction pipe is attached to the biomass Thermal decomposition device and the above heat The two sides of the decomposition gas reformer are disposed below the upper surface of the plurality of granular materials and/or block layers respectively formed in the biomass pyrolysis device and the thermal decomposition gas reformer The side of the biomass pyrolysis device and the pyrolysis gas reformer, and the pyrolysis gas introduction pipe is disposed substantially horizontally with respect to the direction of gravity. The gasification device according to claim 1, wherein the inner bottom surface of the pyrolysis gas introduction pipe has a structure that protrudes upward. The gasification device according to claim 1, wherein the inner bottom surface of the pyrolysis gas introduction pipe has a structure in which both sides of the pyrolysis thermodegrader and the pyrolysis gas reformer protrude upward toward the center portion with a slope. . The gasification device according to any one of claims 1 to 3, wherein the pyrolysis gas introduction pipe has a substantially quadrangular shape in addition to a cross section perpendicular to the longitudinal direction. The biomass gasification device according to any one of claims 1 to 4, wherein the pyrolysis gas introduction pipe is provided with one or two. The gasification apparatus according to any one of claims 1 to 5, wherein the pyrolysis gas introduction pipe retains the plurality of granules and/or lumps in the interior thereof. A biomass gasification device comprising: a biomass pyrolysis device having a raw material supply port, a non-oxidizing gas supply port and/or a steam injection port; and a thermal decomposition gas reformer having a steam injection port And a reformed gas discharge port; and a pyrolysis gas introduction pipe that introduces the pyrolysis gas generated in the biomass pyrolysis device to the pyrolysis gas reformer, and is provided in the biomass pyrolysis device and the heat Decomposing between the gas reformers; and the above-mentioned biothermal pyrolyzer further comprises a plurality of granules and/or a plurality of granules and/or a plurality of pre-heated inlets and outlets, and the plurality of granules and And/or the heat of the mass, and performing thermal decomposition of the biomass; on the other hand, the pyrolysis gas reformer further has a flow path of a preheated gas or liquid heat medium on the outside thereof, and The modification of the thermal decomposition gas generated by the thermal decomposition of the biomass is performed by the heat of the heat medium, and the gasification device of the biomass is characterized in that the thermal decomposition gas introduction pipe is attached to the biomass heat Decomposer side, equipped with As to the number of granular materials within the above-described thermal decomposition of biomass and / or a layer on the surface of the mass closer to the thermal decomposition of biomass under the control of the side surface. The gasification device according to claim 7, wherein the thermal decomposition gas introduction pipe has a side of the biomass pyrolyzer between the biomass pyrolysis device and the pyrolysis gas reformer, and is opposite to gravity The direction is provided substantially horizontally, and then the structure is raised toward the side of the above-described pyrolysis gas reformer. The gasification apparatus according to claim 7 or 8, wherein the pyrolysis gas introduction pipe holds the plurality of granules and/or lumps therein. A method for gasification of biomass, comprising a biomass pyrolyzer for heating a raw material in a non-oxidizing gas atmosphere or a mixed gas atmosphere of a non-oxidizing gas and steam, and the above-mentioned biomass thermal decomposition device a pyrolysis gas reformer that heats the gas generated in the presence of steam, and puts a plurality of pre-heated pellets and/or masses into the biomass pyrolysis reactor and the thermal decomposition gas The massifier uses the heat of the above-mentioned several granules and/or lumps to perform the thermal decomposition of the biomass and the reformation of the biomass of the pyrolysis gas generated by the thermal decomposition of the biomass. The method of gasification of the biomass is characterized in that the plurality of granules and/or lumps are individually placed in parallel with the flow of the plurality of granules and/or lumps. In the above-described thermal decomposition gas reformer, the thermal decomposition gas generated in the biomass pyrolysis device is introduced into the thermal decomposition gas reformer through a thermal decomposition gas introduction pipe to be reformed, and the heat is modified. Decomposition gas introduction pipe is attached to The two sides of the pyrolysis gas decomposer and the pyrolysis gas reformer are disposed on the plurality of particles and/or blocks respectively formed in the biomass pyrolysis device and the pyrolysis gas reformer The side surface of the above-mentioned thermal decomposition catalyst and the above-mentioned thermal decomposition gas reformer are disposed below the upper surface of the layer, and are disposed substantially horizontally with respect to the direction of gravity. The gasification method of the raw material of claim 10, wherein the inner bottom surface of the pyrolysis gas introduction pipe has a structure that protrudes upward. The method of gasification according to claim 10 or 11, wherein the pyrolysis gas introduction pipe retains the plurality of granules and/or lumps therein.