WO2017203587A1

WO2017203587A1 - Biomass gasification apparatus

Info

Publication number: WO2017203587A1
Application number: PCT/JP2016/065229
Authority: WO
Inventors: 堂脇　直城; 潤一池田; 大輔人見; 忠秀齋藤; 康輔須田; 恒上内; 亀山　光男
Original assignee: 株式会社ジャパンブルーエナジー; Ａｂエナジー株式会社
Priority date: 2016-05-23
Filing date: 2016-05-23
Publication date: 2017-11-30
Also published as: JP6412261B2; TW201741446A; JPWO2017203587A1

Abstract

The present invention provides an apparatus which is for producing a hydrogen-containing gas from biomass, and which can optimize biomass pyrolysis temperature and pyrolysis gas modification temperature to reduce problems caused by tar. The present invention pertains to a biomass gasification apparatus which is provided with a biomass pyrolysis device, a pyrolysis gas modification device, and pyrolysis gas introduction pipes, wherein: the biomass pyrolysis device and the pyrolysis gas modification device include an introduction opening and a discharge opening for a heat carrier; biomass pyrolysis and pyrolysis gas modification are carried out by the heat of the heat carrier; the biomass pyrolysis device and the pyrolysis gas modification device are arranged in parallel; and the pyrolysis gas introduction pipes are provided on container side surfaces of both of the biomass pyrolysis device and the pyrolysis gas modification device below an upper surface of a heat carrier layer formed in each device, and the pyrolysis gas introduction pipes are horizontally positioned.

Description

Biomass gasifier

The present invention relates to a biomass gasification apparatus, and more specifically, a biomass pyrolyzer that pyrolyzes biomass, and a pyrolysis gas reformer that reforms by mixing the gas generated in the biomass pyrolyzer with steam. And a biomass gasification apparatus.

Starting from the Great East Japan Earthquake that occurred on March 11, 2011, the operation of many nuclear power generation facilities has been stopped since then in terms of safety. Along with this, there is a concern about the shortage of power supply, and as an alternative to nuclear power generation, power generation facilities using renewable energy such as solar power generation, wind power generation, geothermal power generation, hydroelectric power generation, tidal power generation, and biomass power generation are attracting attention. Yes.

Under such circumstances, the Government of Japan decided on the “Fourth Energy Basic Plan” on April 11, 2014, mainly to accelerate the introduction of renewable energy, and to disperse fuel cell technology, etc. It was decided to expand the spread of type energy systems. In addition, the “Hydrogen / Fuel Cell Strategy Roadmap Revision” compiled on March 22, 2016 will examine technical and economic issues related to the utilization of hydrogen derived from renewable energy. It was included.

Among renewable energies, solar power generation, wind power generation, and tidal power generation are expected as temporary power supply sources, but cannot be expected as stable power supply facilities because the amount of power generation is not stable. In addition, hydropower generation and tidal power generation are expected to have a certain level of demand if they are small-scale facilities, but there is a problem that the installation location is limited in order to construct large-scale facilities.

On the other hand, biomass such as timber, sewage sludge, livestock excrement, etc. exists uniformly in Japan. In particular, due to the collapse of houses and forest collapse due to the Great East Japan Earthquake, large amounts of woody biomass such as construction wood waste, fallen forest wood, unwanted forest land residue, and thinned wood are generated. It is expected that these woody biomass will be effectively used as renewable energy.

In the woody biomass gasifier, for example, biomass is supplied from the upper part of a vertical gasifier, and a packed moving bed of biomass is formed in the gasifier, and gasified from the lower part of the gasifier. In a biomass gasification apparatus equipped with a gasification furnace that supplies the agent and pyrolyzes the biomass descending the packed moving bed with the ascending gasifying agent and thermally decomposes it, the biomass is classified to a predetermined size Biomass gas having a vibration sieve that obtains a particle size distribution-adjusted biomass whose weight ratio of fine particles of biomass below the diameter is a predetermined value or less, and a biomass supply device that supplies the particle size distribution-adjusted biomass from the vibration sieve to the gasifier An apparatus has been proposed (Patent Document 1). According to the gasifier, a uniform high-temperature gas upward flow can be formed in the packed moving bed, and the pressure loss in the packed moving bed can be reduced, so that stable gasification can be maintained. However, there is no guarantee that the supplied biomass will be pyrolyzed uniformly. Moreover, it is necessary to obtain the particle size distribution-adjusted biomass as described above, and an apparatus for that purpose must be provided, leading to high costs.

An externally heated rotary kiln type pyrolysis section that thermally decomposes raw biomass by indirect heating and pyrolyzing to generate a tar containing pyrolysis gas, and a pyrolysis gas containing tar extracted from the pyrolysis section, and A biomass gasification apparatus has been proposed that includes an oxidizing gas introduced into char to thermally decompose the tar content and a gasification section that gasifies the char (Patent Document 2). The apparatus thermally decomposes biomass and then removes tar and char contained in the pyrolyzed gas by burning with oxidizing gas. However, the equipment is not only complicated, but also the operation is complicated. Moreover, when burning tar, there is a concern that a part of the fuel gas is burned and lost. Other devices include, for example, a carbonization device that carbonizes sewage sludge, woody biomass, etc., a high-temperature gasification section that gasifies the carbide generated from the carbonization device, and a combustible pyrolysis containing tar volatilized when the carbide is generated There has been proposed a pyrolysis gasification system including a two-stage gasification furnace including a gas reforming section that performs gas reforming (Patent Document 3). The pyrolysis gasification system is not only complicated because it includes a carbonization apparatus and a two-stage gasification furnace, but also requires complicated operation. Moreover, when burning tar, there is a concern that a part of the fuel gas is burned and lost.

As a method for gasifying organic substances such as woody biomass, a method using a heat carrier medium (heat carrier) is disclosed. For example, a method for producing a product gas having a high calorific value from an organic substance and a substance mixture, in which a circulating heat-carrying medium passes through a heating zone, a reaction zone, a pyrolysis zone and a separation step, and subsequently enters the heating zone. In return, the organic substance or substance mixture is separated into pyrolysis gas as a solid carbon-containing residue and volatile phase by contact with a heated support medium heated in the pyrolysis zone, after passing through the pyrolysis zone The solid carbon-containing residue is separated from the heat-carrying medium in the separation step, the pyrolysis gas is mixed with water vapor as the reaction medium, and a part of the heat contained in the heat-carrying medium heated in the reaction zone is exchanged In a method for producing a product gas having a high calorific value from an organic substance and a mixture of substances, further heating to produce a product gas having a high calorific value, Mixed with pyrolysis gas in the zone and fed all solid carbon-containing residue to another combustion device where it is burned, and the hot exhaust gas of this combustion device is deposited on the heat carrier medium present in the heating zone. There has been proposed a method for producing a product gas having a high calorific value from an organic substance and a substance mixture, in which a large amount of sensible heat is applied to the heat carrier medium at that time (Patent Document 4). In this method, immediately after leaving the pyrolysis reactor, a mixture comprising pyrolysis coke and a heat-carrying medium is separated, and the obtained pyrolysis coke is burned in a combustion apparatus, and the sensible heat generated thereby is utilized. Thus, the heat carrier medium is heated in the heating zone, and thereby, a product gas having a high calorific value is obtained at a low cost. In addition, it is basically provided with a pyrolyzer having a pyrolysis zone and a gas reformer having a reaction zone separately, and thus can be configured as either a serial connection type or a parallel connection type. It is characterized by. In addition, a system has been proposed in which the preheater in the above method is devised for the purpose of maintaining the heating efficiency of the heat carrier medium (heat carrier) in the preheater in the heating zone and stabilizing the quality of the product gas. (Patent Document 5). However, even in the method and system using these heat-carrying media (heat carriers), troubles due to tar generated during thermal decomposition could not be sufficiently avoided.

JP 2011-231193 A JP 2007-177106 A JP 2011-68893 A Special table 2003-510403 gazette JP2011-144329A

The present invention optimizes the pyrolysis temperature of biomass and the reforming temperature of the generated pyrolysis gas, thereby increasing the generation amount of pyrolysis gas and increasing the production amount of hydrogen-containing gas that is the final product. The present invention provides a biomass gasification apparatus that can reduce the generation amount of tar and dust. In addition, the generated tar gas can be effectively gasified, and the remaining tar and dust remaining without being gasified can be efficiently recovered, thereby significantly reducing equipment troubles due to tar and dust. An apparatus is provided.

In the conventional method that uses the heat of a heat carrier medium (heat carrier) to pyrolyze biomass and reforms the generated pyrolysis gas, the biomass is wrapped in the heat carrier layer and heated. Therefore, biomass can be pyrolyzed relatively uniformly, but operational troubles due to tar and dust generated during pyrolysis could not be avoided. In the conventional method, the heat carrier is preheated to a predetermined temperature and introduced into the pyrolysis gas reformer, where the heat carrier contacts the pyrolysis gas and steam introduced from the biomass pyrolyzer. Then, the pyrolysis gas is steam reformed and taken out as a product. On the other hand, the heat carrier descends through the pipe and is introduced into the biomass pyrolyzer to cause thermal decomposition of the biomass. The gas generated by the pyrolysis of biomass rises in the pipe and is introduced into the pyrolysis gas reformer. However, since the pyrolysis gas contains tar and soot and the like, the tar and soot and the like adhere to the inner wall and valve of the introduction pipe to the pyrolysis gas reformer, and sometimes the pyrolysis gas The problem is that the heat carrier that is in countercurrent contact with the pipe is also stuck and clogged in the pipe. In order to solve this problem, it is conceivable to increase the diameter of the introduction pipe. However, even though this means can simply extend the time to blockage, it cannot be an essential solution. Further, in order to solve the blockage problem in the heat carrier pipe, there can be considered a means for separating the pipe where the pyrolysis gas rises and the pipe where the heat carrier descends. It was not possible to avoid troubles such as clogging due to tar and dust adhering to the inner wall of the pipe and valves etc. In addition, such a method of installing separate pipes significantly complicates the apparatus and operation.

Moreover, in the conventional method of thermally decomposing biomass and reforming the generated gas using the heat of the heat carrier medium (heat carrier), the pyrolysis gas reformer and the biomass pyrolyzer Are connected in series up and down, it has been impossible to separately control the temperature inside each reactor, ie, the biomass pyrolyzer and pyrolysis gas reformer. For example, when the pyrolysis temperature of biomass decreases, even if an attempt is made to increase the pyrolysis temperature, the biomass pyrolyzer internal temperature cannot be increased due to the necessity of maintaining the pyrolysis gas reformer internal temperature. On the contrary, when the pyrolysis temperature of biomass rises, if the temperature inside the biomass pyrolyzer is lowered, it is necessary to maintain the temperature of the pyrolysis gas reformer as well. For this reason, there is a problem that the internal temperature of the biomass pyrolyzer cannot be lowered. Therefore, it is not easy to continuously optimize the pyrolysis temperature of biomass and the reforming temperature of the generated pyrolysis gas. As a result, the generation amount of pyrolysis gas and the production amount of hydrogen-containing gas in the final product There was a problem that would decrease. Along with this, there has also been a problem that the amount of tar and dust generated increases. Originally, it is desirable that the biomass pyrolyzer and the pyrolysis gas reformer can be temperature controlled separately.

Patent Document 4 proposes a method in which a biomass pyrolyzer and a pyrolysis gas reformer are arranged in parallel to the flow of a heat carrier medium (heat carrier). According to this method, the temperature of the biomass pyrolyzer and the temperature of the pyrolysis gas reformer can be controlled separately, so that the above problem can be solved. In this method, the pyrolysis gas generated in the biomass pyrolyzer has been introduced into the pyrolysis gas reformer by piping from the upper part of the biomass pyrolyzer. Such a method of introducing pyrolysis gas has a problem that tar and dust etc. adhere to the inner wall and valve of the pipe through which the pyrolysis gas rises and falls to prevent clogging troubles from occurring. Was.

If the temperature of the biomass pyrolyzer and the pyrolysis gas reformer can be controlled separately, the biomass pyrolysis temperature and the pyrolysis gas reforming temperature can be set to optimum values. The amount of tar and dust generated during pyrolysis can be effectively reduced, pyrolysis gas can be generated efficiently, and the generated pyrolysis gas can be efficiently used under optimum conditions. Can be modified. Accordingly, it is possible to remarkably reduce the adhesion of tar, dust, etc. to the inner wall of the pipe and the valve, and to greatly increase the production amount of the reformed gas. However, in the apparatus configuration as described in Patent Document 4 above, the temperatures of the biomass pyrolyzer and the pyrolysis gas reformer can be controlled separately, but the biomass pyrolyzer and the pyrolysis gas can be controlled separately. In the pyrolysis gas introduction pipe that introduces pyrolysis gas into the reformer, tar and dust adhere to the inner wall and valves, etc., and eventually the pyrolysis gas introduction pipe is closed. .

Therefore, the inventors separately control the internal temperatures of the biomass pyrolyzer and the pyrolysis gas reformer, and set the biomass pyrolysis temperature and the pyrolysis gas reforming temperature to appropriate values, respectively. In addition to increasing the generation amount of pyrolysis gas and increasing the production amount of the hydrogen-containing gas that is the final product, the generation amount of tar and dust is reduced, in addition to biomass. Tar, dust, etc. adhere to the inner wall and valve of the pyrolysis gas introduction pipe for introducing the pyrolysis gas generated in the pyrolysis gas into the pyrolysis gas reformer, and the pyrolysis gas introduction pipe is blocked. In order to avoid this, various investigations have been attempted regarding the configuration of the gasifier.

As a result, the biomass pyrolyzer and the pyrolysis gas reformer are arranged in parallel with respect to the flow of a plurality of granular materials and / or bulk materials [heat carrier medium (heat carrier)], and the pyrolysis gas The introduction pipe is formed in the biomass pyrolyzer and the pyrolysis gas reformer on both sides of the biomass pyrolyzer and the pyrolysis gas reformer, and the biomass pyrolyzer below the upper surface of the heat carrier layer and It has been found that the above problem can be solved by installing on the side surface of the pyrolysis gas reformer and making the pyrolysis gas introduction pipe a horizontal pipe. That is, by arranging the biomass pyrolyzer and the pyrolysis gas reformer in parallel with the heat carrier flow, the internal temperature can be controlled separately and the pyrolysis gas introduction pipe By providing a gas inlet (gas inlet) and a gas inlet (gas outlet) in the heat carrier layer, a heat carrier in the biomass pyrolyzer and pyrolytic gas reformer is provided in the pyrolysis gas introduction pipe. Then, the pyrolysis gas passes through the heat carrier layer held in the pyrolysis gas introduction pipe, so that tar and dust are efficiently removed, and the tar is effectively heated. It was found that it was decomposed. In addition, surprisingly, the heat carrier that has entered the pyrolysis gas introduction pipe is sequentially replaced as the heat carrier moves from the top to the bottom in the biomass pyrolysis gas reformer and pyrolysis gas reformer, As a result, the tar and dust are remarkably efficiently removed and the tar is pyrolyzed and preferably reformed without the heat carrier being fixed and clogged with tar or the like in the pyrolysis gas introduction pipe. Was found. Preferably, if the inner bottom surface of the pyrolysis gas introduction tube is protruded upward, the heat carriers flowing in the biomass pyrolysis device and the pyrolysis gas reformer respectively pass through the pyrolysis gas introduction tube. It is found that not only can the flow into the other container be prevented more effectively, but also the heat carrier in the pyrolysis gas introduction pipe can be effectively replaced and tar and dust can be removed more efficiently. It was.

That is, the present invention
(1) Biomass pyrolyzer having a biomass supply port, and a non-oxidizing gas supply port and / or a steam inlet, and a pyrolysis gas reformer having a steam inlet and a reformed gas outlet, A pyrolysis gas inlet pipe provided between the biomass pyrolyzer and the pyrolysis gas reformer, which introduces the pyrolysis gas generated in the biomass pyrolyzer into the pyrolysis gas reformer; And the biomass pyrolyzer and the pyrolysis gas reformer each further comprise a plurality of preheated granules and / or lump inlets and outlets, and the plurality of granules. And / or a biomass gasification apparatus that performs pyrolysis of biomass and reforming of pyrolysis gas generated by pyrolysis of biomass by the heat of the lump. A gas reformer is provided in parallel with the plurality of granular and / or massive flows, and the pyrolysis gas introduction pipe is provided with the biomass pyrolyzer and the pyrolysis gas reformer. The biomass pyrolyzer and the heat below the upper surfaces of the plurality of granular and / or lump layers formed in the biomass pyrolyzer and the pyrolysis gas reformer on both sides of the mass device, respectively. The biomass gasification apparatus is provided on a side surface of the cracked gas reformer, and the pyrolysis gas introduction pipe is provided substantially horizontally with respect to the direction of gravity.

As a preferred embodiment,
(2) The biomass gasification apparatus according to (1), wherein an inner bottom surface of the pyrolysis gas introduction pipe has a structure protruding upward.
(3) The inner bottom surface of the pyrolysis gas introduction pipe has a structure projecting upward with an inclination from both sides of the biomass pyrolyzer and the pyrolysis gas reformer to the central portion, (1) The biomass gasification apparatus according to (1),
(4) A structure in which the inner bottom surface of the pyrolysis gas introduction pipe projects upward with an inclination of 5 to 45 degrees from both sides of the biomass pyrolyzer and pyrolysis gas reformer to the center. The biomass gasification apparatus according to the above (1),
(5) A structure in which the inner bottom surface of the pyrolysis gas introduction pipe protrudes upward with an inclination of 10 to 30 degrees from both sides of the biomass pyrolyzer and pyrolysis gas reformer to the center. The biomass gasification apparatus according to the above (1),
(6) A structure in which the inner bottom surface of the pyrolysis gas introduction pipe protrudes upward with an inclination of 15 to 25 degrees from both sides of the biomass pyrolyzer and pyrolysis gas reformer to the center. The biomass gasification apparatus according to the above (1),
(7) Any one of the above (1) to (6), wherein the outer shape of the cross section perpendicular to the longitudinal direction (the direction of flow of the pyrolysis gas) of the pyrolysis gas introduction tube is substantially circular or polygonal. A gasifier for biomass as described in
(8) The biomass according to any one of (1) to (6) above, wherein the outer shape of the cross section perpendicular to the longitudinal direction (flow direction of the pyrolysis gas) of the pyrolysis gas introduction pipe is substantially square Gasifier,
(9) The biomass gasification apparatus according to any one of (1) to (8), wherein 1 to 3 pyrolysis gas introduction pipes are provided.
(10) The biomass gasification apparatus according to any one of (1) to (8), wherein one or two pyrolysis gas introduction pipes are provided,
(11) The biomass gasification according to any one of (1) to (10), wherein the pyrolysis gas introduction pipe has the plurality of granular materials and / or agglomerates therein. apparatus,
(12) The steam injection port is provided at one or more positions selected from the group consisting of a biomass pyrolyzer and its vicinity, a pyrolysis gas reformer and its vicinity, and a pyrolysis gas introduction pipe, (1) to the biomass gasification apparatus according to any one of (11),
(13) Any one of the above (1) to (11), wherein the steam inlet is provided in the biomass pyrolyzer or the vicinity thereof, the pyrolysis gas reformer or the vicinity thereof, and the pyrolysis gas introduction pipe. Gasification apparatus for biomass as described in
(14) One to three steam inlets are provided in the biomass pyrolyzer or the vicinity thereof, the pyrolysis gas reformer or the vicinity thereof, and the pyrolysis gas introduction pipe, respectively. (11) The biomass gasification apparatus according to any one of
(15) The above-mentioned (1) to (11), wherein one steam inlet is provided in each of the biomass pyrolyzer or the vicinity thereof, the pyrolysis gas reformer or the vicinity thereof, and the pyrolysis gas introduction pipe. ) The biomass gasification device according to any one of
(16) Any of the above (1) to (15), wherein a preheater for preheating a plurality of granular materials and / or agglomerates is further provided in the upper part of the biomass pyrolyzer and the pyrolysis gas reformer A biomass gasification apparatus according to claim 1,
(17) In any one of the above (1) to (16), an inlet for the plurality of granular materials and / or agglomerates is provided above the biomass pyrolyzer and the pyrolysis gas reformer. The biomass gasifier described in the above,
(18) In any one of the above (1) to (16), the introduction port for the plurality of granular materials and / or agglomerates is provided at the top of the biomass pyrolyzer and the pyrolysis gas reformer. The biomass gasifier described in the above,
(19) In any one of the above (1) to (18), the plurality of granular and / or lump discharge ports are provided below the biomass pyrolyzer and the pyrolysis gas reformer. The biomass gasifier described in the above,
(20) In any one of the above (1) to (18), the plurality of granular and / or lump discharge ports are provided at the bottom of the biomass pyrolyzer and pyrolysis gas reformer. The biomass gasifier described in the above,
(21) The biomass gasification apparatus according to any one of (1) to (20) above, wherein the granular and / or lump is selected from the group consisting of metal balls and ceramic balls,
(22) The biomass gasification apparatus according to (21), wherein the metal ball is made of stainless steel,
(23) The biomass gasification apparatus according to (21), wherein the ceramic ball is made of one or more materials selected from the group consisting of alumina, silica, silicon carbide, tungsten carbide, zirconia, and silicon nitride.
(24) The biomass gasifier according to any one of (1) to (23), wherein the biomass pyrolyzer has a gas phase temperature of 400 to 700 ° C.
(25) The biomass gasifier according to any one of (1) to (23), wherein the biomass pyrolyzer has a gas phase temperature of 500 to 700 ° C.
(26) The biomass gasification apparatus according to any one of (1) to (23), wherein the biomass pyrolyzer has a gas phase temperature of 550 to 650 ° C.
(27) The biomass gasification apparatus according to any one of (1) to (26), wherein the pyrolysis gas reformer has a gas phase temperature of 700 to 1,000 ° C.
(28) The biomass gasification apparatus according to any one of (1) to (26) above, wherein the pyrolysis gas reformer has a gas phase temperature of 850 to 950 ° C.
(29) The biomass gasification apparatus according to any one of (1) to (26) above, wherein the pyrolysis gas reformer has a gas phase temperature of 880 to 930 ° C.
(30) The biomass as described in any one of (1) to (29) above, wherein the biomass is a biomass resource selected from the group consisting of plant biomass, biological biomass, daily waste, and food waste A biomass gasification apparatus can be mentioned.

Moreover, this invention is the gasification method of biomass using the biomass gasification apparatus of said (1) description. That is, the present invention
(31) A biomass pyrolyzer that heats biomass in a non-oxidizing gas atmosphere or a mixed gas atmosphere of non-oxidizing gas and steam, and a gas generated in the biomass pyrolyzer in the presence of steam A plurality of preheated granulates and / or lumps are put into the biomass pyrolyzer and the pyrolysis gas reformer, and the plurality of the pyrolysis gas reformers to be heated are provided. In the biomass gasification method, in which the pyrolysis of biomass and the reforming of pyrolysis gas generated by the pyrolysis of biomass are performed by the heat of the granules and / or the chunks, the plurality of granules and / or chunks described above Is separately fed to the biomass pyrolyzer and the pyrolysis gas reformer provided in parallel with the plurality of granular and / or lump flows, The pyrolysis gas generated in the biomass pyrolyzer is formed in the biomass pyrolyzer and the pyrolysis gas reformer on both sides of the biomass pyrolyzer and the pyrolysis gas reformer, respectively. Pyrolysis gas provided on the side surfaces of the biomass pyrolyzer and pyrolysis gas reformer below the upper surface of the plurality of granular and / or lump layers and provided substantially horizontally with respect to the direction of gravity This is a method for gasifying biomass that is introduced into the pyrolysis gas reformer through the introduction pipe and reformed.

As a preferred embodiment,
(32) The biomass gasification method according to (31), wherein the inner bottom surface of the pyrolysis gas introduction pipe has a structure protruding upward.
(33) The inner bottom surface of the pyrolysis gas introduction pipe has a structure projecting upward with an inclination from both sides of the biomass pyrolyzer and the pyrolysis gas reformer to the center portion, (31) The biomass gasification method according to (31),
(34) A structure in which the inner bottom surface of the pyrolysis gas introduction pipe projects upward with an inclination of 5 to 45 degrees from both sides of the biomass pyrolyzer and pyrolysis gas reformer to the center. The biomass gasification method according to (31) above,
(35) A structure in which the inner bottom surface of the pyrolysis gas introduction pipe protrudes upward with an inclination of 10 to 30 degrees from both sides of the biomass pyrolyzer and pyrolysis gas reformer to the center. The biomass gasification method according to (31) above,
(36) A structure in which the inner bottom surface of the pyrolysis gas introduction pipe projects upward with an inclination of 15 to 25 degrees from both sides of the biomass pyrolyzer and the pyrolysis gas reformer to the center. The biomass gasification method according to (31) above,
(37) Any one of the above (31) to (36), wherein an outer shape of a cross section perpendicular to the longitudinal direction (flow direction of the pyrolysis gas) of the pyrolysis gas introduction pipe is a substantially circular shape or a polygon Gasification method of biomass as described in
(38) The biomass according to any one of (31) to (36), wherein an outer shape of a cross section perpendicular to a longitudinal direction (flow direction of the pyrolysis gas) of the pyrolysis gas introduction pipe is substantially square. Gasification method,
(39) The biomass gasification method according to any one of (31) to (38), wherein 1 to 3 of the pyrolysis gas introduction pipes are provided,
(40) The biomass gasification method according to any one of (31) to (36), wherein one or two pyrolysis gas introduction pipes are provided,
(41) The biomass gasification according to any one of (31) to (40), wherein the pyrolysis gas introduction pipe has the plurality of granular materials and / or agglomerates therein. Method,
(42) The steam injection port is provided at one or more positions selected from the group consisting of a biomass pyrolyzer and its vicinity, a pyrolysis gas reformer and its vicinity, and a pyrolysis gas introduction pipe, (31) The method for gasifying biomass according to any one of (41),
(43) Any one of the above (31) to (41), wherein the steam inlet is provided in the biomass pyrolyzer or the vicinity thereof, the pyrolysis gas reformer or the vicinity thereof, and the pyrolysis gas introduction pipe. Gasification method of biomass as described in
(44) One to three steam inlets are provided in the biomass pyrolyzer or the vicinity thereof, the pyrolysis gas reformer or the vicinity thereof, and the pyrolysis gas introduction pipe, respectively. (41) The method for gasifying biomass according to any one of
(45) The above (31) to (41), wherein one steam inlet is provided in each of the biomass pyrolyzer or the vicinity thereof, the pyrolysis gas reformer or the vicinity thereof, and the pyrolysis gas introduction pipe. ) Biomass gasification method according to any one of
(46) Any of the above (31) to (45), wherein a preheater for preheating a plurality of granular materials and / or agglomerates is further provided in the upper part of the biomass pyrolyzer and pyrolysis gas reformer A biomass gasification method according to claim 1;
(47) In any one of the above (31) to (46), an inlet for the plurality of granular materials and / or agglomerates is provided above the biomass pyrolyzer and the pyrolysis gas reformer. The biomass gasification method described,
(48) In any one of the above (31) to (46), the introduction port for the plurality of granular materials and / or agglomerates is provided at the top of the biomass pyrolyzer and pyrolytic gas reformer. The biomass gasification method described,
(49) In any one of the above (31) to (48), the plurality of granular and / or lump discharge ports are provided below the biomass pyrolyzer and the pyrolysis gas reformer. The biomass gasification method described,
(50) In any one of the above (31) to (48), the plurality of granular and / or lump discharge ports are provided at the bottom of the biomass pyrolyzer and pyrolysis gas reformer. The biomass gasification method described,
(51) The biomass gasification method according to any one of (31) to (50), wherein the granular material and / or the lump are selected from the group consisting of metal balls and ceramic balls,
(52) The biomass gasification method according to (51), wherein the metal ball is made of stainless steel,
(53) The biomass gasification method according to (51), wherein the ceramic balls are made of one or more materials selected from the group consisting of alumina, silica, silicon carbide, tungsten carbide, zirconia, and silicon nitride.
(54) The biomass gasification method according to any one of (31) to (53) above, wherein the gas phase temperature of the biomass pyrolyzer is 400 to 700 ° C.
(55) The biomass gasification method according to any one of (31) to (53), wherein the gas phase temperature of the biomass pyrolyzer is 500 to 700 ° C.
(56) The biomass gasification method according to any one of (31) to (53), wherein the biomass pyrolyzer has a gas phase temperature of 550 to 650 ° C.
(57) The biomass gasification method according to any one of the above (31) to (56), wherein the pyrolysis gas reformer has a gas phase temperature of 700 to 1,000 ° C.
(58) The biomass gasification method according to any one of (31) to (56) above, wherein the pyrolysis gas reformer has a gas phase temperature of 850 to 950 ° C.
(59) The biomass gasification method according to any one of (31) to (56) above, wherein the pyrolysis gas reformer has a gas phase temperature of 880 to 930 ° C.
(60) The biomass as described in any one of (31) to (59) above, wherein the biomass is a biomass resource selected from the group consisting of plant biomass, biological biomass, household waste, and food waste Biomass gasification method,
Can be mentioned.

As in the first apparatus configuration, the present inventors have introduced a pyrolysis gas introduction pipe for introducing pyrolysis gas generated in the biomass pyrolysis apparatus into the pyrolysis gas reformer, that is, a pyrolysis gas introduction pipe. The gas inlet (gas inlet) is installed in the biomass pyrolyzer at the side of the biomass pyrolyzer below the upper surface of the heat carrier layer, that is, in the heat carrier layer. Then, only a biomass pyrolyzer introduces a plurality of granular materials and / or lumps [heat carrier medium (heat carrier)] to thermally decompose biomass, and the generated pyrolysis gas is converted into conventional heat. Even when introduced into an exchanger-type pyrolysis gas reformer and reforming the pyrolysis gas, the inventors have thought that the same effect as described above can be obtained. Therefore, the present inventors have conducted various studies on the device configuration, and as a result, the device configuration can solve the problems of the present invention without inferior to the first device configuration. I found it.

That is, the present invention
(61) Biomass pyrolyzer comprising a biomass feed port and a non-oxidizing gas feed port and / or a steam inlet, and a pyrolysis gas reformer comprising a steam inlet and a reformed gas outlet, A pyrolysis gas inlet pipe provided between the biomass pyrolyzer and the pyrolysis gas reformer, which introduces the pyrolysis gas generated in the biomass pyrolyzer into the pyrolysis gas reformer; And the biomass pyrolyzer further includes a plurality of preheated granule and / or lump inlets and discharge ports, and is heated by the heat of the plurality of granulates and / or lump. The pyrolysis of biomass is performed, while the pyrolysis gas reformer further includes a flow path of a gaseous or liquid heat medium that is preheated on the outside thereof, and the heat of the heat medium By pyrolysis of biomass In the biomass gasification apparatus that performs reforming of the generated pyrolysis gas, the pyrolysis gas introduction pipe is formed in the biomass pyrolysis device on the biomass pyrolysis device side. And / or a biomass gasifier characterized in that the biomass pyrolyzer is provided on a side surface of the biomass pyrolyzer below the upper surface of the massive layer.

As a preferred embodiment,
(62) The pyrolysis gas introduction pipe is provided substantially horizontally with respect to the direction of gravity on the biomass pyrolysis device side between the biomass pyrolysis device and the pyrolysis gas reformer, The biomass gasification apparatus according to (61), wherein the biomass gasification apparatus has a structure that rises upward toward the pyrolysis gas reformer side,
(63) The pyrolysis gas introduction tube is provided substantially horizontally with respect to the direction of gravity between the biomass pyrolysis device and the pyrolysis gas reformer, and the pyrolysis gas introduction tube The biomass gasification apparatus according to (61), wherein the inner bottom surface has a structure projecting upward,
(64) The pyrolysis gas introduction tube is provided substantially horizontally with respect to the direction of gravity between the biomass pyrolysis device and the pyrolysis gas reformer, and the pyrolysis gas introduction tube The biomass gasification apparatus according to (61), wherein the inner bottom surface has a structure protruding upward from both sides of the biomass pyrolyzer and the pyrolysis gas reformer with an inclination from both sides. ,
(65) The pyrolysis gas introduction tube is provided substantially horizontally with respect to the direction of gravity between the biomass pyrolysis device and the pyrolysis gas reformer, and the pyrolysis gas introduction tube The above (61), wherein the inner bottom surface has a structure projecting upward with an inclination of 5 to 45 degrees from both sides of the biomass pyrolyzer and the pyrolysis gas reformer to the center. Biomass gasification equipment,
(66) The pyrolysis gas introduction tube is provided substantially horizontally with respect to the direction of gravity between the biomass pyrolysis device and the pyrolysis gas reformer, and the pyrolysis gas introduction tube The above (61), wherein the inner bottom surface has a structure projecting upward with an inclination of 10 to 30 degrees from both sides of the biomass pyrolyzer and pyrolysis gas reformer to the center. Biomass gasification equipment,
(67) The pyrolysis gas introduction tube is provided substantially horizontally with respect to the direction of gravity between the biomass pyrolysis device and the pyrolysis gas reformer, and the pyrolysis gas introduction tube The above (61), wherein the inner bottom surface has a structure projecting upward with an inclination of 15 to 25 degrees from both sides of the biomass pyrolyzer and the pyrolysis gas reformer to the center. Biomass gasification equipment,
(68) Any one of the above (61) to (67), wherein an outer shape of a cross section perpendicular to the longitudinal direction of the pyrolysis gas introduction pipe (the pyrolysis gas flow direction) is a substantially circular shape or a substantially polygonal shape. A gasifier for biomass as described in
(69) The biomass according to any one of (61) to (67), wherein an outer shape of a cross section perpendicular to a longitudinal direction of the pyrolysis gas introduction pipe (flow direction of the pyrolysis gas) is a substantially square shape. Gasifier,
(70) The biomass gasification apparatus according to any one of (61) to (69), wherein one to three pyrolysis gas introduction pipes are provided,
(71) The biomass gasification apparatus according to any one of (61) to (69), wherein one or two pyrolysis gas introduction pipes are provided,
(72) The biomass gasification according to any one of (61) to (71), wherein the pyrolysis gas introduction pipe has the plurality of granular materials and / or agglomerates therein. apparatus,
(73) The steam inlet is provided at one or more positions selected from the group consisting of a biomass pyrolyzer and its vicinity, a pyrolysis gas reformer and its vicinity, and a pyrolysis gas introduction pipe, (61) The biomass gasification device according to any one of (72) to (72),
(74) Any one of the above (61) to (72), wherein the steam inlet is provided in the biomass pyrolyzer or the vicinity thereof, the pyrolysis gas reformer or the vicinity thereof, and the pyrolysis gas introduction pipe. Gasification apparatus for biomass as described in
(75) In the above (61) to (61), one to three steam inlets are respectively provided in the biomass pyrolyzer or the vicinity thereof, the pyrolysis gas reformer or the vicinity thereof, and the pyrolysis gas introduction pipe. (72) The biomass gasification apparatus according to any one of (72),
(76) The above (61) to (72), wherein one steam inlet is provided in each of the biomass pyrolyzer or the vicinity thereof, the pyrolysis gas reformer or the vicinity thereof, and the pyrolysis gas introduction pipe. ) The biomass gasification device according to any one of
(77) The biomass according to any one of the above (61) to (76), wherein a preheater for preheating a plurality of granular materials and / or agglomerates is further provided in an upper part of the biomass pyrolyzer. Gasifier,
(78) The biomass gasification apparatus according to any one of (61) to (77), wherein the plurality of granular and / or lump-like inlets are provided above the biomass pyrolyzer. ,
(79) The biomass gasification apparatus according to any one of (61) to (77), wherein the plurality of granular and / or lump-like inlets are provided at the top of the biomass pyrolyzer. ,
(80) The biomass gasification apparatus according to any one of (61) to (79), wherein the plurality of granular and / or lump discharge ports are provided below the biomass pyrolyzer. ,
(81) The biomass gasification apparatus according to any one of (61) to (79), wherein the plurality of granular and / or lump discharge ports are provided at the bottom of the biomass pyrolyzer. ,
(82) The biomass gasification apparatus according to any one of (61) to (81), wherein the granular material and / or the lump are selected from the group consisting of metal balls and ceramic balls,
(83) The biomass gasification apparatus according to (82), wherein the metal ball is made of stainless steel,
(84) The biomass gasifier according to (82), wherein the ceramic ball is made of one or more materials selected from the group consisting of alumina, silica, silicon carbide, tungsten carbide, zirconia, and silicon nitride.
(85) The biomass gasification apparatus according to any one of (61) to (84), wherein the preheated gaseous or liquid heat medium is high-temperature hot air,
(86) The biomass gasification apparatus according to any one of (61) to (85), wherein the biomass pyrolyzer has a gas phase temperature of 400 to 700 ° C.
(87) The biomass gasification apparatus according to any one of (61) to (85), wherein the biomass pyrolyzer has a gas phase temperature of 500 to 700 ° C.
(88) The biomass gasification apparatus according to any one of (61) to (85), wherein the biomass pyrolyzer has a gas phase temperature of 550 to 650 ° C.
(89) The biomass gasification apparatus according to any one of (61) to (88), wherein the pyrolysis gas reformer has a gas phase temperature of 700 to 1,000 ° C.
(90) The biomass gasification apparatus according to any one of (61) to (88), wherein the pyrolysis gas reformer has a gas phase temperature of 850 to 950 ° C.
(91) The biomass gasification apparatus according to any one of (61) to (88), wherein the pyrolysis gas reformer has a gas phase temperature of 880 to 930 ° C.
(92) The biomass as described in any one of (61) to (91), wherein the biomass is a biomass resource selected from the group consisting of plant biomass, biological biomass, daily waste, and food waste A biomass gasification apparatus can be mentioned.

The present invention is also a biomass gasification method using the biomass gasification apparatus described in (61) above. That is, the present invention
(93) A biomass pyrolyzer that heats biomass in a non-oxidizing gas atmosphere or a mixed gas atmosphere of non-oxidizing gas and steam, and a gas generated in the biomass pyrolyzer in the presence of steam. A plurality of preheated granulates and / or lumps are charged into the biomass pyrolyzer, and the plurality of granulates and / or lumps are heated. Biomass is thermally decomposed by the heat it has, while a preheated gaseous or liquid heat medium is passed through the flow path of the heat medium provided outside the pyrolysis gas reformer, In the biomass gasification method for reforming the pyrolysis gas generated by pyrolysis of biomass by the heat of the gaseous or liquid heat medium, the heat generated in the biomass pyrolyzer Through the pyrolysis gas introduction pipe provided on the side surface of the biomass pyrolyzer below the upper surface of the plurality of granular and / or bulk layers formed in the biomass pyrolyzer This is a method for gasifying biomass introduced into the pyrolysis gas reformer and reformed.

As a preferred embodiment,
(94) The pyrolysis gas introduction pipe is provided substantially horizontally with respect to the direction of gravity on the biomass pyrolyzer side between the biomass pyrolyzer and the pyrolysis gas reformer, The biomass gasification method according to (93), wherein the biomass gasification method has a structure that rises upward toward the pyrolysis gas reformer,
(95) The pyrolysis gas introduction tube is provided substantially horizontally with respect to the direction of gravity between the biomass pyrolysis device and the pyrolysis gas reformer, and the pyrolysis gas introduction tube The method for gasifying biomass according to (93) above, wherein the inner bottom surface has a structure protruding upward.
(96) The pyrolysis gas introduction tube is provided substantially horizontally with respect to the direction of gravity between the biomass pyrolysis device and the pyrolysis gas reformer, and the pyrolysis gas introduction tube The biomass gasification method according to (93), wherein the inner bottom surface has a structure projecting upward from the both sides of the biomass pyrolyzer and the pyrolysis gas reformer with an inclination from both sides to the center. ,
(97) The pyrolysis gas introduction tube is provided substantially horizontally with respect to the direction of gravity between the biomass pyrolysis device and the pyrolysis gas reformer, and the pyrolysis gas introduction tube The above (93), wherein the inner bottom surface has a structure projecting upward with an inclination of 5 to 45 degrees from both sides of the biomass pyrolyzer and pyrolysis gas reformer to the center. Gasification method of biomass,
(98) The pyrolysis gas introduction tube is provided substantially horizontally with respect to the direction of gravity between the biomass pyrolysis device and the pyrolysis gas reformer, and the pyrolysis gas introduction tube The above (93), wherein the inner bottom surface has a structure projecting upward with an inclination of 10 to 30 degrees from both sides of the biomass pyrolyzer and the pyrolysis gas reformer to the center. Gasification method of biomass,
(99) The pyrolysis gas introduction tube is provided substantially horizontally with respect to the direction of gravity between the biomass pyrolysis device and the pyrolysis gas reformer, and the pyrolysis gas introduction tube The above (93), wherein the inner bottom surface has a structure projecting upward with an inclination of 15 to 25 degrees from both sides of the biomass pyrolyzer and the pyrolysis gas reformer to the center. Gasification method of biomass,
(100) Any one of the above (93) to (99), wherein the outer shape of the cross section perpendicular to the longitudinal direction (the direction of flow of the pyrolysis gas) of the pyrolysis gas introduction tube is substantially circular or polygonal Gasification method of biomass as described in
(101) The biomass according to any one of (93) to (99), wherein an outer shape of a cross section perpendicular to the longitudinal direction (flow direction of the pyrolysis gas) of the pyrolysis gas introduction pipe is substantially square Gasification method,
(102) The biomass gasification method according to any one of (93) to (101), wherein one to three pyrolysis gas introduction pipes are provided,
(103) The biomass gasification method according to any one of (93) to (101), wherein one or two pyrolysis gas introduction pipes are provided,
(104) The biomass gasification according to any one of (93) to (101), wherein the pyrolysis gas introduction pipe has the plurality of particulates and / or agglomerates therein. Method,
(105) The steam inlet is provided at one or more positions selected from the group consisting of a biomass pyrolyzer and its vicinity, a pyrolysis gas reformer and its vicinity, and a pyrolysis gas introduction pipe, (93) to (104) the biomass gasification method according to any one of
(106) Any one of the above (93) to (104), wherein the steam inlet is provided in the biomass pyrolyzer or the vicinity thereof, the pyrolysis gas reformer or the vicinity thereof, and the pyrolysis gas introduction pipe. Gasification method of biomass as described in
(107) The above (93) to (93), wherein one to three steam inlets are provided in the biomass pyrolyzer or its vicinity, the pyrolysis gas reformer or its vicinity, and the pyrolysis gas introduction pipe, respectively. (104) The biomass gasification method according to any one of (104),
(108) The above (93) to (104), wherein one steam inlet is provided in each of the biomass pyrolyzer or its vicinity, the pyrolysis gas reformer or its vicinity, and the pyrolysis gas introduction pipe. ) Biomass gasification method according to any one of
(109) The biomass according to any one of (93) to (108), wherein a preheater for preheating a plurality of granular materials and / or agglomerates is further provided in an upper part of the biomass pyrolyzer. Gasification method,
(110) The biomass gasification method according to any one of (93) to (109), wherein the plurality of granular and / or massive inlets are provided above the biomass pyrolyzer. ,
(111) The biomass gasification method according to any one of (93) to (109), wherein the plurality of granular and / or lump introduction ports are provided at the top of the biomass pyrolyzer. ,
(112) The biomass gasification method according to any one of (93) to (111), wherein the plurality of granular and / or lump discharge ports are provided below the biomass pyrolyzer. ,
(113) The biomass gasification method according to any one of (93) to (111), wherein the plurality of granular and / or lump discharge ports are provided at the bottom of the biomass pyrolyzer. ,
(114) The biomass gasification method according to any one of (93) to (113), wherein the granular material and / or the lump are selected from the group consisting of metal balls and ceramic balls,
(115) The biomass gasification method according to (114), wherein the metal ball is made of stainless steel,
(116) The biomass gasification method according to (114), wherein the ceramic balls are made of one or more materials selected from the group consisting of alumina, silica, silicon carbide, tungsten carbide, zirconia, and silicon nitride.
(117) The biomass gasification method according to any one of (93) to (116), wherein the preheated gaseous or liquid heat medium is high-temperature hot air,
(118) The biomass gasification method according to any one of (93) to (117), wherein the biomass pyrolyzer has a gas phase temperature of 400 to 700 ° C.
(119) The biomass gasification method according to any one of (93) to (117), wherein the biomass pyrolyzer has a gas phase temperature of 500 to 700 ° C.
(120) The biomass gasification method according to any one of (93) to (117), wherein the biomass pyrolyzer has a gas phase temperature of 550 to 650 ° C.
(121) The biomass gasification method according to any one of (93) to (120), wherein the pyrolysis gas reformer has a gas phase temperature of 700 to 1,000 ° C.
(122) The biomass gasification method according to any one of (93) to (120) above, wherein the pyrolysis gas reformer has a gas phase temperature of 850 to 950 ° C.
(123) The biomass gasification method according to any one of (93) to (120), wherein the pyrolysis gas reformer has a gas phase temperature of 880 to 930 ° C,
(124) The biomass according to any one of (93) to (123), wherein the biomass is a biomass resource selected from the group consisting of plant biomass, biological biomass, daily waste, and food waste. The biomass gasification method can be mentioned.

In the apparatus of the present invention, since the temperature of the biomass pyrolyzer and the pyrolysis gas reformer can be controlled separately, the biomass pyrolysis temperature and the reforming temperature of the generated pyrolysis gas are both controlled. It can be optimized easily and over a long period of time. As a result, the amount of pyrolysis gas generated can be increased and the production of the hydrogen-containing gas that is the final product can be increased, as well as tar and dust generated by the pyrolysis of biomass. The amount can be reduced as much as possible. In addition, the gas inlet (gas inlet) of the pyrolysis gas introduction pipe that introduces the pyrolysis gas generated in the biomass pyrolyzer into the pyrolysis gas reformer is in the heat carrier layer of the biomass pyrolyzer. Since the gas introduction port (gas outlet) of the pyrolysis gas introduction pipe is provided in the heat carrier layer of the pyrolysis gas reformer, heat is introduced into the pyrolysis gas introduction pipe. The carrier flows in and the heat carrier is held in the pyrolysis gas introduction pipe. Further, since the pyrolysis gas introduction pipe is provided substantially horizontally with respect to the direction of gravity, the heat carrier in the pyrolysis gas introduction pipe, the biomass pyrolysis device, and the pyrolysis gas reformer are disposed above. It is possible to avoid the heat carrier flowing from the biomass pyrolyzer into the pyrolysis gas introduction pipe from being mixed into the pyrolysis gas reformer as well as the heat carrier moving from the bottom to the bottom. On the other hand, it is possible to avoid the heat carrier flowing into the pyrolysis gas introduction pipe from the pyrolysis gas reformer from being mixed into the biomass pyrolysis device. Therefore, when the pyrolysis gas generated in the biomass pyrolyzer is introduced into the pyrolysis gas reformer through the pyrolysis gas introduction pipe, tar and dust contained in the pyrolysis gas are in the heat. Efficiently captured by the carrier, tar is effectively gasified, and the remaining tar and dust are withdrawn from the bottom of the biomass pyrolyzer and pyrolysis gas reformer while adhering to the heat carrier. And can be recovered. Accordingly, it is possible to remarkably reduce the trouble of the apparatus due to tar and dust, and to maximize the gasification rate of the generated tar, and to produce the hydrogen-containing gas from the biomass with high thermal efficiency and low cost.

FIG. 1 shows a biomass gas according to the present invention having a first apparatus configuration in which a plurality of pre-heated granules and / or agglomerates are introduced into both a biomass pyrolyzer and a pyrolysis gas reformer. It is the schematic which showed one embodiment of the formation apparatus. FIG. 2 shows a biomass gas according to the present invention having a first apparatus configuration in which a plurality of preheated particulates and / or agglomerates are introduced into both a biomass pyrolyzer and a pyrolysis gas reformer. It is the schematic which showed another one embodiment of the formation apparatus. FIG. 3 shows an embodiment of the biomass gasification apparatus of the present invention, which includes a second apparatus configuration in which a plurality of pre-heated granular materials and / or agglomerates are charged only into the biomass pyrolyzer. FIG. FIG. 4 is a schematic view showing several different embodiments of the pyrolysis gas introduction pipe provided between the biomass pyrolyzer and the pyrolysis gas reformer. FIG. 5 is a schematic view of a conventional biomass gasification apparatus used in a comparative example.

The gasifier of the present invention (first apparatus configuration) includes a biomass supply port, a biomass pyrolyzer having a non-oxidizing gas supply port and / or a steam injection port, a steam injection port, and a reformed gas. A pyrolysis gas reformer having an outlet; and the biomass pyrolysis device and the pyrolysis gas reformer for introducing pyrolysis gas generated in the biomass pyrolysis device into the pyrolysis gas reformer; And the biomass pyrolyzer and the pyrolytic gas reformer are each further provided with a plurality of preheated granules and / or agglomerates, that is, And a heat carrier medium (heat carrier) inlet and outlet. Then, a plurality of pre-heated granules and / or lump is introduced into the biomass pyrolyzer and pyrolysis gas reformer, and the heat of the plurality of granules and / or lump is used to generate biomass. Reforming of pyrolysis gas generated by pyrolysis and pyrolysis of biomass is performed. Here, in the gasification apparatus of the present invention, the biomass pyrolyzer and the pyrolysis gas reformer are provided in parallel to the flow of the plurality of granular materials and / or bulk materials. Thus, like a conventional biomass gasification apparatus, a biomass pyrolyzer and a pyrolysis gas reformer are provided in series in the vertical direction with respect to a plurality of granular and / or lump flows. Rather than being provided in parallel, a plurality of particulates and / or agglomerates can be separately introduced into the biomass pyrolyzer and pyrolysis gas reformer, The temperature can be controlled separately.

In the gasification apparatus of the present invention, the pyrolysis gas introduction pipe is formed in the biomass pyrolysis device and the pyrolysis gas reformer on both sides of the biomass pyrolysis device and the pyrolysis gas reformer, respectively. The particulate and / or bulk layer, that is, the side surface of the biomass pyrolyzer and pyrolyzed gas reformer below the upper surface of the heat carrier layer. That is, on the biomass pyrolyzer side, a gas inlet (gas inlet) of the pyrolysis gas introduction pipe is provided in a layer formed of a plurality of granular materials and / or lumps formed in the biomass pyrolyzer, In addition, on the pyrolysis gas reformer side, a gas inlet (gas outlet) of the pyrolysis gas introduction pipe is formed in a layer composed of a plurality of granular materials and / or agglomerates formed in the pyrolysis gas reformer. ) Is provided. Then, the pyrolysis gas generated in the biomass pyrolyzer through the pyrolysis gas introduction pipe is introduced into the pyrolysis gas reformer. As described above, since the pyrolysis gas intake port of the pyrolysis gas introduction pipe is provided in the layer composed of a plurality of particles and / or a lump, a plurality of particles present in the biomass pyrolyzer. A part of the product and / or the lump can enter the inside of the pyrolysis gas introduction pipe, and a plurality of gas introduction ports to the pyrolysis gas reformer of the pyrolysis gas introduction pipe are provided. Since it is provided in the layer composed of the granular material and / or the lump, a part of the plurality of the granular material and / or lump existing in the pyrolysis gas reformer is provided in the pyrolysis gas introduction pipe. It can penetrate into the interior, and the pyrolysis gas introduction tube can hold a plurality of particulates and / or agglomerates therein. In addition, since the pyrolysis gas introduction pipe is provided substantially horizontally with respect to the direction of gravity, a plurality of particulates and / or lumps can easily enter the pyrolysis gas introduction pipe, and The plurality of granular materials and / or bulks held in the pyrolysis gas introduction pipe are moved through the biomass pyrolysis device and the pyrolysis gas reformer by gravity from the top to the bottom, and / or Or with the flow of a lump, it can be gradually and gradually replaced with a plurality of particles and / or lump that are moving from top to bottom. And thereby, the some granular material and / or lump which were hold | maintained inside the pyrolysis gas introduction pipe | tube can keep a new state. Furthermore, a plurality of particulates and / or lumps that have flowed into the pyrolysis gas inlet pipe from the biomass pyrolyzer are mixed into the pyrolysis gas reformer, while thermal decomposition from the pyrolysis gas reformer. It can be avoided that a plurality of particulates and / or lumps flowing into the gas introduction pipe are mixed into the biomass pyrolyzer. As described above, since a plurality of granular materials and / or lumps are held inside the pyrolysis gas introduction pipe, they are included in the pyrolysis gas that passes through them and is introduced into the pyrolysis gas reformer. The tar, dust, and the like that are collected are brought into contact with the plurality of granular materials and / or lumps. Then, a part or most of the trapped tar is pyrolyzed and gasified by the heat of the plurality of particulates and / or lumps, and is preferably further modified. Further, tar and dust remaining without being gasified are discharged from the bottom portion of the biomass pyrolyzer and the bottom portion of the pyrolysis gas reformer while adhering to a plurality of granular materials and / or bulk materials. Thereby, tar and dust can be effectively removed from the pyrolysis gas.

In the gasifier of the present invention, it is preferable that the inner bottom surface of the pyrolysis gas introduction pipe has a structure protruding upward. As described above, since the inner bottom surface of the pyrolysis gas introduction pipe protrudes upward, a plurality of granular materials and / or lumps that have entered the pyrolysis gas introduction pipe from the biomass pyrolyzer. Mixed with a plurality of particulates and / or lumps that have entered the pyrolysis gas inlet pipe from the pyrolysis gas reformer, that is, a plurality of particles that have flowed into the pyrolysis gas inlet pipe from the biomass pyrolyzer The particulates and / or lumps are mixed into the pyrolysis gas reformer, while the plurality of granules and / or lumps that have flowed into the pyrolysis gas introduction pipe from the pyrolysis gas reformer, It can prevent more effectively mixing into a biomass pyrolyzer. More preferably, the inner bottom surface of the pyrolysis gas introduction pipe has a structure projecting upward with an inclination from both sides of the biomass pyrolyzer and pyrolysis gas reformer toward the center. The inclination angle (θ) is preferably 5 to 45 degrees, more preferably 10 to 30 degrees, and still more preferably 15 to 25 degrees. The inclination angle (θ) may be the same on both sides of the biomass pyrolyzer and the pyrolysis gas reformer, or may be different from each other. By providing such an inclination, a plurality of particulates and / or lumps that have entered the pyrolysis gas introduction pipe from both the biomass pyrolyzer and pyrolysis gas reformer are stagnant at the point where they merge. In this case, the replacement of a plurality of granular materials and / or lumps in the pyrolysis gas introduction pipe is promoted. In the pyrolysis gas introduction pipe, the outer shape of the cross section perpendicular to the longitudinal direction thereof, 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 square. It is. The inner diameter of the pyrolysis gas introduction pipe is not particularly limited as long as a plurality of granular materials and / or lumps can easily flow into and out of the pyrolysis gas introduction pipe. The pyrolysis gas introduction pipe is preferably provided between 1 and 3 and more preferably 1 or 2 between the biomass pyrolyzer and the pyrolysis gas reformer.

In the gasifier of the present invention, the steam inlet is preferably one selected from the group consisting of a biomass pyrolyzer and its vicinity, a pyrolysis gas reformer and its vicinity, and a pyrolysis gas introduction pipe. It is provided in the above position. More preferably, the steam inlet is provided in all of the biomass pyrolyzer or the vicinity thereof, the pyrolysis gas reformer or the vicinity thereof, and the pyrolysis gas introduction pipe. Thereby, pyrolysis of biomass and reforming of pyrolysis gas can be achieved more satisfactorily. The number of steam inlets is not particularly limited, but preferably 1 to 3, respectively, in the biomass pyrolyzer or the vicinity thereof, the pyrolysis gas reformer or the vicinity thereof, and the pyrolysis gas introduction pipe. More preferably, one is provided for each.

In the gasification apparatus of the present invention, a preheater for preheating a plurality of granular materials and / or agglomerates is provided above the biomass pyrolyzer and the pyrolytic gas reformer. Thereby, this some granular material and / or lump are heated to predetermined temperature. The preheater is provided at the upper part of the biomass pyrolyzer and pyrolysis gas reformer, where all the granular materials and / or lumps are heated to a predetermined temperature and heated to the same temperature. The granular and / or lump can be separately introduced into the biomass pyrolyzer and the pyrolysis gas reformer. Also, one preheater is provided above each of the biomass pyrolyzer and pyrolytic gas reformer, that is, a total of two preheaters are provided, and the biomass pyrolyzer and pyrolytic gas reformer are provided in each preheater. It can also be introduced separately into the biomass pyrolyzer and pyrolysis gas reformer, heated to separate temperatures to match the respective temperatures of the reactor. In any of the above configurations, the effect can be sufficiently achieved. If the former configuration is adopted, the apparatus cost can be reduced, and when the biomass pyrolysis temperature is controlled by the amount of steam introduced into the biomass pyrolyzer, the steam introduced more effectively with the introduced steam. And reforming can be performed. On the other hand, if the latter form is adopted, temperature control can be easily performed and energy required for heating the granular material and / or the massive material can be reduced.

Also, a plurality of granular and / or lump inlets are provided above (upper), preferably at the top of the biomass pyrolyzer and pyrolytic gas reformer, while the biomass pyrolyzer and pyrolytic gas. Below the reformer (lower part), preferably at the bottom, a plurality of particulate and / or lump outlets are provided. For example, a so-called two-stage valve system in which a plurality of granular materials and / or massive inlets and outlets are provided with a total of two valves, one above and one below the pipe, is used. However, the introduction and extraction method is an example, and the present invention is not limited to this method.

The plurality of granular materials and / or agglomerates, that is, the heat carrier medium (heat carrier) is preferably made of 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. The ceramic is selected from the group consisting of alumina, silica, silicon carbide, tungsten carbide, zirconia, and silicon nitride, and more preferably alumina. The shape of the plurality of granular materials and / or lumps is preferably spherical (ball), but is not necessarily a true sphere, and may be a spherical material having an elliptical or oval cross-sectional shape. The diameter (maximum diameter) of the spherical object is preferably 3 to 25 mm, more preferably 8 to 15 mm. If the above upper limit is exceeded, fluidity inside the biomass pyrolyzer and pyrolysis gas reformer, i.e., free fall, may be impaired. May become stationary inside the organ and cause blockage. On the other hand, below the lower limit, in particular, in the biomass pyrolyzer, the spherical substance itself may be fixed due to tar and dust adhering to the spherical substance, which may cause clogging. For example, if the diameter of the spherical material is less than 3 mm, the spherical material grows by adhering to the inner wall of the biomass pyrolyzer due to the influence of tar and soot adhering to the spherical material. There is a concern that the pyrolyzer will be blocked. In addition, when the spherical object with tar attached is pulled out from the bottom valve of the biomass pyrolyzer and pyrolysis gas reformer, the spherical object of less than 3 mm is light, and since tar is attached, it falls naturally. Without being fixed, it may stick to the inside of the valve and promote blockage.

The biomass of the present invention refers to so-called biomass resources. Here, the biomass resources are plant biomass, for example, agricultural products such as thinned wood, sawn wood waste, pruned branches, forest land residue, unused trees, etc. , Rice straw, wheat straw, rice husks, etc., other marine plants, construction waste wood, etc .; biological biomass, for example, biological waste such as livestock waste and sewage sludge; and household waste such as dust and food waste Say etc. The apparatus of the present invention is preferably suitable for gasification of plant biomass and biological biomass.

Hereinafter, the biomass gasification apparatus of the present invention will be described with reference to the accompanying drawings. FIG. 1 shows that both the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) have a plurality of pre-heated granules and / or agglomerates (7), ie a heat carrier medium (heat It is the schematic which showed one embodiment of the gasification apparatus of the biomass of this invention provided with the 1st apparatus structure which throws in (carrier). In the biomass gasification apparatus, the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) are provided with a plurality of granular and / or lump (7), that is, with respect to the flow of the heat carrier. Are provided in parallel. And the preheater (1) for heating a some granular material and / or a lump (7) previously is equipped with 1 unit | set, the biomass pyrolyzer (3), and the pyrolysis gas reformer (2) upper part. It has been. Moreover, the pyrolysis gas introduction pipe (9) is provided in one between the biomass pyrolysis device (3) and the pyrolysis gas reformer (2), and thereby the biomass pyrolysis device (3). The pyrolysis gas generated in is introduced into the pyrolysis gas reformer (2). Here, the pyrolysis gas introduction pipe (9) is connected to the biomass pyrolysis device (3) and the pyrolysis gas reformer (2) on both sides of the biomass pyrolysis device (3) and the pyrolysis gas reformer (2). ) Are formed on the side surfaces of the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) below the upper surface (13) of the plurality of granular and / or lump (7) layers, respectively. It has been. Specifically, the biomass pyrolyzer (3) side gas inlet (gas inlet) (9-3) and the pyrolyzed gas reformer (2) side gas inlet (gas outlet) of the pyrolysis gas inlet pipe (9) ( All of 9-2) are provided in a plurality of granular and / or massive (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 internal bottom face of the pyrolysis gas introduction pipe (9) has a structure protruding upward. However, the inner bottom surface may be a flat structure.

Prior to being introduced into the biomass pyrolyzer (3) and the pyrolysis gas reformer (2), a plurality of granulates and / or agglomerates (7), i.e. the heat carrier, are pre-heated in the preheater (1). Heated. The heat carrier (7) is preferably heated to 1,000 to 1,100 ° C., more preferably 1,050 to 1,100 ° C. If it is less than the said lower limit, the gas generated by the pyrolysis of biomass may not be fully reformed in the pyrolysis gas reformer (2). On the other hand, if the above upper limit is exceeded, it is not possible to expect a significant increase in the effect just by applying extra heat. Moreover, it becomes a cause of the thermal efficiency fall of an installation.

The heat carrier (7) heated to the predetermined temperature in the preheater (1) is then subjected to a biomass pyrolyzer (3) and a pyrolysis gas reformer arranged in parallel with the flow of the heat carrier (7). Each is introduced separately into the vessel (2). In the biomass pyrolyzer (3), the heat carrier (7) is brought into contact with the biomass separately supplied from the biomass supply port (4) to the biomass pyrolyzer (3). Here, although the biomass supply port (4) may be provided in the biomass pyrolyzer (3) itself, as shown in FIG. 1, the biomass pyrolyzer (3) vicinity, for example, a heat carrier (7 ) Can also be provided in the distribution piping to the biomass pyrolyzer (3). In addition, the biomass pyrolyzer (3) contains non-oxidizing gas, for example, nitrogen, and optionally steam, from the non-oxidizing gas supply port (12) and the steam blow-in port (11 ₁ ), respectively. Supplied and kept in a non-oxidizing gas atmosphere or a mixed gas atmosphere of non-oxidizing gas and steam. And by contact with a heat carrier (7) and biomass, biomass is heated and thermally decomposed and pyrolysis gas produces | generates. By setting the biomass pyrolyzer (3) to a non-oxidizing gas atmosphere, it is possible to prevent the combustion of the biomass and efficiently thermally decompose the biomass. The generated pyrolysis gas passes through the pyrolysis gas introduction pipe (9) and is introduced into the pyrolysis gas reformer (2). At this time, tar, dust and the like contained in the generated pyrolysis gas are captured by the heat carrier (7) held in the pyrolysis gas introduction pipe (9), and a part or most of the tar is heat carrier ( 7) Heated and gasified by 7), remaining tar, dust, etc. are discharged from the bottom of the biomass pyrolyzer (3) or pyrolytic gas reformer (2) while adhering to the heat carrier (7). . 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 even more preferably 550 ° C. If it is less than the said lower limit, biomass thermal decomposition may not advance. If the above upper limit is exceeded, heavy tar is generated. Such heavy tar cannot be sufficiently reformed by steam, and may cause equipment troubles due to tar. Here, the gas phase temperature of the biomass pyrolyzer (3) refers to the preheated heat carrier (7), the raw material biomass and the non-oxidizing gas, which are put into the biomass pyrolyzer (3). The temperature generated by mixing with steam that is optionally blown, and the gas phase temperature inside the biomass pyrolyzer (3) generated comprehensively from the radiation heat of the heat carrier (7) layer and the like. The gas phase temperature of the biomass pyrolyzer (3) includes the supply rate and extraction rate of the heat carrier (7), the volume and occupation rate of the heat carrier layer in the biomass pyrolyzer (3), the supply amount of biomass, It can be appropriately controlled by the supply amount of non-oxidizing gas and / or steam. Usually, the supply rate and extraction rate of the heat carrier (7) are determined from the biomass supply amount, and then the volume of the heat carrier layer and its occupancy in the biomass pyrolyzer (3) are gradually changed, By appropriately changing the supply amount of the oxidizing gas and / or steam, the gas phase temperature of the biomass pyrolyzer (3) can be controlled to a predetermined temperature.

The pyrolysis gas generated by pyrolyzing the biomass in the biomass pyrolyzer (3) is introduced into the pyrolysis gas reformer (2) through the pyrolysis gas introduction pipe (9). The pyrolysis gas introduced is brought into contact with the heat carrier (7) in the presence of steam and heated. As a result, the pyrolysis gas and steam react to reform the pyrolysis gas into a gas rich in hydrogen. Here, steam used for gas reforming is biomass pyrolyzer (3) and its vicinity, pyrolysis gas reformer (2) and its vicinity, and biomass pyrolyzer (3) and pyrolysis gas. It introduce | transduces from the steam inlet (11 ₁ , 11 ₂ , 11 ₃ ) provided at one or more positions selected from the group consisting of the pyrolysis gas introduction pipe (9) between the reformer (2). . Preferably, the biomass pyrolyzer (3) or its vicinity, the pyrolysis gas reformer (2) or its vicinity, and the steam inlets (11 ₁ , 11 ₂ ) provided in the pyrolysis gas introduction pipe (9) 11 ₃ ). The upper limit of the gas phase temperature in the pyrolysis 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. It is 850 degreeC, More preferably, it is 880 degreeC. If it is less than the lower limit, the reforming reaction may not proceed. On the other hand, even if the upper limit is exceeded, a significant increase in the effect cannot be expected, and the amount of heat required for heating the heat carrier increases, resulting in high costs. When the gas phase temperature in the pyrolysis gas reformer (2) is 850 ° C. or more, which is the more preferable lower limit value, the reforming of carbon monoxide by steam becomes remarkable, and further, at 880 ° C. or more, which is a more preferable lower limit value. The reforming of methane by steam becomes remarkable. Therefore, in order to efficiently reform both carbon monoxide and methane, the gas phase temperature in the pyrolysis gas reformer (2) is more preferably 880 ° C. or higher. A more preferable upper limit of the gas phase temperature in the pyrolysis gas reformer (2) is 950 ° C., and the pyrolysis gas can be sufficiently reformed below the temperature, but in order to reduce the amount of fuel used, 930 More preferably, it is not higher than ° C. Here, the gas phase temperature of the pyrolysis gas reformer (2) refers to the preheated heat carrier (7), pyrolysis gas and steam introduced into the pyrolysis gas reformer (2). The temperature generated by mixing and the gas phase temperature inside the pyrolysis gas reformer (2) generated comprehensively from the radiant heat of the heat carrier (7) layer and the like. The gas phase temperature of the pyrolysis gas reformer (2) includes the supply temperature of the heat carrier (7), the supply rate and extraction speed of the heat carrier (7), and the heat carrier layer in the pyrolysis gas reformer (2). And the occupation ratio thereof, the amount of pyrolysis gas supplied from the biomass pyrolyzer (3), the supply amount of steam, and the like can be appropriately controlled. Usually, the supply temperature and the extraction speed of the heat carrier (7), the volume of the heat carrier layer in the pyrolysis gas reformer (2) and the occupation ratio thereof are kept constant, and the supply temperature of the heat carrier (7) is desired. The gas phase temperature of the biomass pyrolyzer (3) is set to a predetermined temperature by supplying the steam at a temperature preferably 100 to 400 ° C., more preferably 150 to 200 ° C. Can be controlled.

Most of the heat necessary for the pyrolysis of biomass in the biomass pyrolyzer (3) and the reforming of the pyrolysis gas in the pyrolysis gas reformer (2) is preheated to the above temperature. The granular and / or lump (7), that is, supplied by the heat of the heat carrier medium (heat carrier). Introduction of heat carrier (7) into biomass pyrolyzer (3) and pyrolysis gas reformer (2), and biomass pyrolyzer (3) and pyrolysis gas reformer (7) of heat carrier (7) The extraction from 2) is performed using, for example, a so-called two-stage valve system (not shown) provided with a total of two valves, one above and one below the pipe. Briefly explaining the operation of the two-stage valve system, the upper and lower two valves are closed, first, the upper valve is opened, the heat carrier (7) is dropped into the pipe, the lower valve and the upper valve are opened. A heat carrier (7) is filled between the bulbs. Next, by closing the upper valve and opening the lower valve, the heat carrier (7) filled between the two valves is transferred to the biomass pyrolyzer (3) and pyrolytic gas reformer (2). Introduced or extracted from the biomass pyrolyzer (3) and pyrolytic gas reformer (2). By repeating such valve operation, the heat carrier (7) is introduced almost continuously into the biomass pyrolyzer (3) and the pyrolysis gas reformer (2), and the biomass pyrolyzer (3). And is continuously withdrawn from the pyrolysis gas reformer (2). The introduction and extraction method is an example, and the present invention is not limited to this method. By controlling the introduction rate of the heat carrier (7) into the biomass pyrolyzer (3) and the extraction rate of the heat carrier (7) from the biomass pyrolyzer (3), the heat carrier in the biomass pyrolyzer (3) A layer can be formed, the thickness of the layer can be controlled to an appropriate value, and the temperature of the biomass pyrolyzer (3) can be controlled to the predetermined temperature. The same applies to the pyrolysis gas reformer (2). Thus, by arranging the pyrolysis gas reformer (2) and the biomass pyrolyzer (3) in parallel, the internal temperature of the pyrolysis gas reformer (2) and the biomass pyrolyzer (3) Can be controlled individually. As a result, the reforming reaction in the pyrolysis gas reformer (2) can be allowed to proceed at an appropriate temperature, and the pyrolysis of biomass in the biomass pyrolyzer (3) can be performed at an appropriate temperature. It becomes. Furthermore, it becomes possible to improve thermal efficiency. Further, the pyrolysis gas reformer (2) and the biomass pyrolyzer (3) are arranged in parallel to the flow of the heat carrier, and each container (2, 3) is preferably in a bowl shape. By arranging and allowing the heat carrier to naturally drop by gravity, it is possible to provide an energy saving efficient gasifier without requiring power for moving the heat carrier.

Here, if the extraction speed of the heat carrier (7) from the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) is too fast, the biomass pyrolyzer (3) and the pyrolysis gas reformer ( On the other hand, if the temperature of 2) becomes high and the extraction speed is too slow, the heat carrier dissipates heat, and the temperatures of the biomass pyrolyzer (3) and pyrolytic gas reformer (2) become low. The supply rate and extraction rate of the heat carrier (7) to the biomass pyrolyzer (3) depend on the supply amount and type of biomass as a raw material, and the moisture and ash content of the biomass. Determined with respect to the amount of supply. Usually, it is set to 5 to 60 mass times the feed rate of the dry raw material, that is, dry biomass to the biomass pyrolyzer (3). Preferably, it is set to 5 to 30 times by mass, more preferably 10 to 20 times by mass, the supply rate of dry biomass to the biomass pyrolyzer (3). If it is less than the said minimum, the calorie | heat amount required in order to thermally decompose biomass cannot be supplied. On the other hand, if the above upper limit is exceeded, the supply amount of the heat carrier (7) becomes excessive, and therefore the biomass pyrolyzer (3) must be made larger than necessary, and the heat carrier (7) ) Requires an extra amount of heat. Further, the supply rate and extraction rate of the heat carrier (7) to the pyrolysis gas reformer (2) depend on the amount of pyrolysis gas supplied and its temperature, the temperature of steam, its supply amount, and the like. Controlled. However, it is preferable that the biomass supply amount is determined in advance and is controlled based on fluctuations in the above factors at any time in the operation stage. Usually, it is set to 5 to 30 mass times the feed rate of the dry raw material, that is, dry biomass to the biomass pyrolyzer (3). Preferably, it is set to 5 to 15 times by mass, more preferably 10 to 15 times by mass, the supply rate of dry biomass to the biomass pyrolyzer (3). If it is less than the lower limit, the amount of heat necessary for reforming the pyrolysis gas cannot be supplied. On the other hand, if the above upper limit is exceeded, the amount of heat carrier (7) supplied becomes excessive, and therefore the pyrolysis gas reformer (2) must be made larger than necessary, and the heat carrier An extra amount of heat is required for heating in (7).

The upper limit of the pressure in the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) is preferably 104.33 kPa, more preferably 102.33 kPa, and the lower limit is preferably 100.33 kPa, more preferably Is 101.23 kPa. If the above upper limit is exceeded, the generated pyrolysis gas may flow backward from the biomass supply port (4) and leak to the outside of the biomass pyrolyzer (3). On the other hand, if it is less than the above lower limit, the generated pyrolysis gas is contained in the layer of the heat carrier (7) in the biomass pyrolyzer (3), pyrolysis gas reformer (2), and pyrolysis gas introduction pipe (9). The pyrolysis gas and accompanying tar may not be sufficiently gasified and reformed without being uniformly dispersed.

As described above, the steam inlets (11 ₁ , 11 ₂ , 11 ₃ ) are preferably configured to have a biomass pyrolyzer (3), a pyrolysis gas reformer (2) bottom, and a biomass pyrolyzer (3 ) And the pyrolysis gas reformer (2). When installing in the biomass pyrolyzer (3), it is particularly preferable to install it in the upper part of the biomass pyrolyzer (3). Thereby, the contact between the steam introduced into the biomass pyrolyzer (3) and the heat carrier (7) can be carried out more effectively, and the gas generated by pyrolysis of the steam and biomass. Not only can be made longer, but also the contact time with the heat carrier (7) can be made longer. As a result, gasification and reforming of pyrolysis gas and tar attached to the heat carrier can be efficiently performed. In FIG. 1, the steam inlet includes a lower part (11 ₂ ) of the pyrolysis gas reformer (2), an upper part (11 ₁ ) of the biomass pyrolyzer (3), and a pyrolysis gas introduction pipe (9 ) (11 ₃ ), one each, a total of three are installed, but this is not a limitation. A plurality of steam inlets can be installed at each location. The temperature of the supplied steam is not particularly limited, but is preferably 130 to 200 ° C, more preferably about 160 ° C. In addition, superheated steam of preferably 500 to 600 ° C. can also be used. For example, when a more preferable steam at about 160 ° C. is supplied, it is preferable that the supply amount of steam is substantially equal to the supply amount of biomass as a raw material. However, the amount of steam varies depending on the moisture content of the raw material, and is not limited to the above.

The biomass supply port (4) should just be installed in the position which can supply biomass to a biomass pyrolyzer (3) effectively. Preferably, it is installed above the biomass pyrolyzer (3), that is, in a pipe for dropping the heat carrier (7) from the preheater (1) to the biomass pyrolyzer (3). Thereby, mixing with biomass and a heat carrier (7) can be performed efficiently, the contact time inside a biomass pyrolyzer (3) can be ensured appropriately, and biomass is fully pyrolyzed. be able to. In FIG. 1, although one biomass supply port (4) is described, it is not limited to this. One or more biomass supply ports (4) are preferably installed, more preferably 1 to 5, more preferably 1 to 3, and even more preferably 1 or 2. By installing a plurality of biomass supply ports (4), biomass having different properties can be simultaneously supplied from the respective supply ports.

The residence time of the biomass in the biomass pyrolyzer (3) is preferably 5 to 60 minutes, more preferably 10 to 40 minutes, and further preferably 15 to 35 minutes. If the amount is less than the lower limit, heat is not uniformly transmitted to the biomass, and uniform pyrolysis is not performed, so that the amount of pyrolysis gas generated is reduced. On the other hand, even if the above upper limit is exceeded, a significant increase in the effect is not recognized, 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 from the moving speed of the heat carrier (7) and the biomass supply amount. The residence time of the gas in the pyrolysis gas reformer (2) is preferably 1 to 10 seconds, more preferably 2 to 5 seconds. The residence time of the gas in the pyrolysis gas reformer (2) can be set from the moving speed and filling amount of the heat carrier (7), the steam supply amount, and the scheduled pyrolysis gas amount. When the pyrolysis gas reformer and the biomass pyrolyzer are connected in series, as in the past, the residence time in each vessel, that is, the residence time and pyrolysis for biomass pyrolysis in the biomass pyrolyzer It was impossible to individually control the residence time for the decomposition of tar in the gas and the residence time required for the reforming reaction between the pyrolysis gas and steam in the pyrolysis gas reformer. . However, the residence time in each container can be controlled independently by arranging the pyrolysis gas reformer (2) and the biomass pyrolyzer (3) in parallel as in the present invention. As a result, the temperature inside each container (2, 3) can be independently controlled without consuming new energy.

As described above, the heat carrier (7) that has passed through the biomass pyrolyzer (3) is composed of the pyrolysis residue (char) of biomass and the trace amount remaining without being thermally decomposed attached to the heat carrier (7). It is discharged from the bottom of the biomass pyrolyzer (3) together with tar and dust. The treatment of the discharged matter including the discharged heat carrier (7) is performed by a conventionally known method such as separation of char in the discharged matter processing apparatus (5) as shown in FIG. For example, the method and apparatus described in

Patent Documents

4 and 5 above can be employed. On the other hand, the heat carrier (7) that has passed through the pyrolysis gas reformer (2), together with a small amount of tar and soot adhering to the heat carrier (7), the bottom of the pyrolysis gas reformer (2). Discharged from. The treatment of the discharged matter including the discharged heat carrier (7) is performed by a conventionally known method with or without being mixed with the heat carrier (7) discharged from the bottom of the biomass pyrolyzer (3). Is done. For example, the method and apparatus described in

Patent Documents

4 and 5 can be employed in the same manner as described above. The heat carrier (7) thus treated is returned again to the preheater (1) and supplied to the biomass pyrolyzer (3) and the pyrolysis gas reformer (2).

FIG. 2 shows that both the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) have a plurality of pre-heated granules and / or agglomerates (7), ie a heat carrier medium (heat It is the schematic which showed another one embodiment of the biomass gasification apparatus of this invention provided with the 1st apparatus structure which throws in a carrier. In the biomass gasification apparatus, a preheater (1 ₁ , 1 ₂ ) for preheating a plurality of granular materials and / or agglomerates (7) is used as a biomass pyrolyzer (3) and a pyrolysis gas reformer. One device is provided on the top of each of the quality devices (2). The other apparatus configuration is the same as the biomass gasification apparatus shown in FIG.

A plurality of granulates and / or agglomerates (7), i.e. a heat carrier, is introduced into the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) before the biomass pyrolyzer (3). And in the preheaters (1 ₂ ) and (1 ₁ ) provided on the respective upper portions of the pyrolysis gas reformer (2), they are separately heated in advance. In the preheater (1 ₂ ) provided at the top of the biomass pyrolyzer (3), the heat carrier (7) is preferably heated to 700 to 800 ° C, more preferably 750 to 800 ° C. If it is less than the said minimum, biomass may not fully be thermally decomposed in a biomass pyrolyzer (3). Even if the upper limit is exceeded, as already described in the description of FIG. 1 above, the amount of steam blown into the biomass pyrolyzer (3) is changed, and the temperature is controlled to an appropriate temperature so that the thermal decomposition of the biomass is efficient. Can be implemented. However, when two preheaters (1) are used, it is preferable to further increase the thermal efficiency by setting the temperature of the heat carrier (7) to the upper limit or less. On the other hand, in the preheater (1 ₁ ) provided in the upper part of the pyrolysis gas reformer (2), the heat carrier (7) is preferably 1,000 to 1,100 ° C., more preferably 1,050. Heated to ˜1,100 ° C. If it is less than the said lower limit, the gas generated by the pyrolysis of biomass may not be fully reformed in the pyrolysis gas reformer (2). In addition, if the above upper limit is exceeded, it is not possible to expect a significant increase in the effect just by applying extra heat, but it only increases the cost. Moreover, it becomes a cause of the thermal efficiency fall of an installation.

FIG. 4 shows several different embodiments of the pyrolysis gas inlet pipe (9) provided between the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) (I, II, III, IV, V, VI, VII, VIII, IX, X). FIG. 4 shows a longitudinal section (a section along the flow direction of the pyrolysis gas) of the pyrolysis gas introduction pipe (9). In FIG. 4, (g) schematically shows the flow direction of the pyrolysis gas. 4, the right side is a biomass pyrolyzer (3) (in FIG. 4, 3 to be displayed.), The left side is an pyrolysis gas reformer (2) (in FIG. 4, 2 Is displayed.) In addition, only the heat carrier (7) in the pyrolysis gas introduction pipe (9) is colored and schematically shown, and the heat carrier in the biomass pyrolysis device (3) and the pyrolysis gas reformer (2) is shown. (7) is not displayed. Although not shown in FIG. 4, the pyrolysis gas introduction pipe (9) may have a flat surface whose inner bottom surface does not protrude upward. All the pyrolysis gas introduction pipes (9) shown in FIG. 4 can be used for the biomass pyrolysis apparatus of the present invention, for example, the biomass pyrolysis apparatus shown in FIGS. That is, on both sides of the biomass pyrolyzer (3) and the pyrolysis gas reformer (2), heat carriers (3) formed in the biomass pyrolyzer (3) and pyrolysis gas reformer (2), respectively. 7) Provided on the side surfaces of the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) below the upper surface (13) of the layer, and the pyrolysis gas introduction pipe (9) It is provided substantially horizontally with respect to the direction and has a structure in which the inner bottom surface of the pyrolysis gas introduction pipe (9) protrudes upward. The pyrolysis gas introduction pipe (9) shown in (I) and (VI) of FIG. 4 has an inner bottom surface protruding upward, and the height (h) of the protruding portion is the heat It is lower than the vertical width (height) (h ₁ , h ₂ ) of the gas inlet (gas inlet) and the gas inlet (gas outlet) of the cracked gas inlet pipe (9). Therefore, the heat carrier (7) that has entered from both the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) will merge above the protruding portion. However, since the heat carrier (7) is a granular material and / or a lump, it is not easily mixed unlike liquids such as water and oil. Therefore, the heat carrier (7) that has entered the pyrolysis gas introduction pipe (9) from the biomass pyrolyzer (3) does not enter the pyrolysis gas reformer (2). Conversely, the heat carrier (7) that has entered the pyrolysis gas introduction pipe (9) from the pyrolysis gas reformer (2) does not enter the biomass pyrolysis device (3). However, if the operation of the biomass pyrolysis apparatus is continued for a considerably long period of time, it is expected to be mixed in rarely. In order to avoid this without fail, the pyrolysis gas introduction pipe (9) has a structure shown in (II), (III) and (IV) and (VII), (VIII) and (IX) of FIG. It is preferable to make it. That is, the height (h) of the protruding portion of the inner bottom surface of the pyrolysis gas introduction pipe (9) is the vertical width (height) (h) of the gas intake port and the introduction port of the pyrolysis gas introduction pipe (9). ₁ , h ₂ ) is the same structure (II, VII) or higher (III, IV, VIII, IX). More preferably, the height (h) of the protruding portion is higher than the vertical width (height) (h ₁ , h ₂ ) of the gas inlet and the inlet of the pyrolysis gas inlet pipe (9). (III, IV, VIII, IX). If such a structure is employ | adopted, mixing of a heat carrier (7) can be prevented more reliably. Moreover, when the projecting portion extends vertically from the bottom surface of the pyrolysis gas introduction pipe (9) as in (I) and (II) of FIG. 4, the biomass pyrolyzer (3) and Heat carrier (7) that invades from each of the places where the heat carriers (7) that have entered from both of the pyrolysis gas reformers (2) merge or where the heat carrier (7) contacts the protruding portion. May stagnate. Therefore, in order to avoid this stagnation, the protruding portion has an inclination angle (θ) like (III), (IV), (VI), (VII), (VIII) and (IX) in FIG. A structure is preferable. More preferred is the structure of (VII), (VIII) and (IX) in FIG. For example, a structure having an inclination angle (θ) in two stages as shown in (III) of FIG. 4 is less susceptible to the stagnation as compared with the structure of (VIII) of FIG. 4 having the same inclination angle (θ). May be less effective to avoid. Therefore, it is more preferable to increase the number of steps in the protruding portion that protrudes stepwise as shown in the left column of FIG. The inclination angle (θ) is preferably 5 to 45 degrees, more preferably 10 to 30 degrees, and still more preferably 15 to 25 degrees. Moreover, the structure of the pyrolysis gas introduction pipe (9) shown in (IV) and (IX) of FIG. 4 is basically a horizontal pipe, but on the inner upper surface of the pipe as shown in (IV). It is also possible to provide a structure in which a concave portion is provided, or a concave portion in which an inclination is provided on the inner upper surface of the pipe as in (IX). Moreover, the vertical width (height) (h ₁ , h ₂ ) of the gas inlet and the gas inlet of the pyrolysis gas inlet pipe (9) may be the same as or different from each other. The inclination angle (θ) may be the same as or different from each other on both sides of the biomass pyrolyzer and the pyrolysis gas reformer. Moreover, as shown to (V) and (X) of FIG. 4, it is also possible to set it as the structure which does not provide a space part (gas reservoir) in the upper part of a pyrolysis gas introduction pipe | tube (9). In this case, the gas generated in the biomass pyrolyzer (3) passes through the voids of the heat carrier (7) layer present in the pyrolyzed gas introduction pipe (9), and then the pyrolyzed gas reformer. (2) will be introduced. Also in the pyrolysis gas introduction pipe (9) having this structure, the continuous operation of the biomass gasification apparatus of the present invention can be sufficiently achieved. However, in order to perform continuous operation for a considerably long time, from the viewpoint of safety, a pyrolysis gas introduction pipe (9) provided with a space (gas reservoir) in the upper part, for example, (I), ( It is preferred to use II), (III), (IV), (VI), (VII), (VIII) and (IX). The pyrolysis gas introduction pipe (9) shown in FIG. 4 is an example, and the present invention is not limited to this. The outer shape of the cross section perpendicular to the longitudinal direction of the pyrolysis gas introduction pipe (9) (the cross section perpendicular to the flow direction of the pyrolysis gas) is as described above, and is preferably substantially circular or substantially polygonal. Yes, more preferably a substantially square shape. Further, the inner diameter of the pyrolysis gas introduction pipe, that is, the vertical width (height) (h ₁ ) of the gas inlet and the vertical width (height) (h ₂ ) of the gas inlet are defined as the heat carrier. There is no particular limitation as long as (7) can easily flow into and out of the pyrolysis gas introduction pipe, preferably 8 to 50 times the size (maximum diameter) of the heat carrier (7), more preferably It is 10 to 40 times, more preferably 10 to 30 times.

The gasifier of the present invention (second apparatus configuration) includes a biomass supply port, a biomass pyrolyzer having a non-oxidizing gas supply port and / or a steam injection port, a steam injection port and a reformer. The pyrolysis gas reformer having a gas outlet and the pyrolysis gas generated in the biomass pyrolysis device is introduced into the pyrolysis gas reformer, and the biomass pyrolysis device and the pyrolysis gas reforming are introduced. The biomass pyrolyzer is further provided with a plurality of preheated granules and / or agglomerates, that is, a heat carrier medium (heat carrier). ), And the pyrolysis gas reformer further includes a preheated gas or liquid heat medium flow path on the outside thereof. Then, a plurality of granular materials and / or chunks heated in advance are introduced into the biomass pyrolyzer, and the pyrolysis of biomass is executed by the heat of the plurality of particulates and / or chunks, The preheated gaseous or liquid heat medium is introduced into the flow path of the gaseous or liquid heat medium provided outside the pyrolysis gas reformer, and the heat of the heat medium causes the biomass. The reforming of the pyrolysis gas generated by the pyrolysis of is performed. As described above, in the gasification apparatus of the present invention, the pyrolysis of biomass in the biomass pyrolyzer and the reforming of the pyrolysis gas in the pyrolysis gas reformer are performed in advance. Since it is separately performed by a granular material and / or a lump, and a gaseous or liquid heating medium preheated separately, each temperature can be controlled separately.

In the gasification apparatus of the present invention, the pyrolysis gas introduction pipe is formed on the biomass pyrolyzer side with a plurality of granular and / or massive layers, ie, heat carrier layers, formed in the biomass pyrolyzer. It is provided on the side of the biomass pyrolyzer below the upper surface. That is, on the biomass pyrolyzer side, a gas inlet (gas inlet) of the pyrolysis gas introduction pipe is provided in a layer formed of a plurality of granular materials and / or lumps formed in the biomass pyrolyzer. Then, the pyrolysis gas generated in the biomass pyrolyzer through the pyrolysis gas introduction pipe is introduced into the pyrolysis gas reformer. As described above, since the pyrolysis gas intake port of the pyrolysis gas introduction pipe is provided in the layer composed of a plurality of particles and / or a lump, a plurality of particles present in the biomass pyrolyzer. A part of the material and / or the lump can enter the inside of the pyrolysis gas introduction pipe, and the pyrolysis gas introduction pipe holds a plurality of particles and / or lump in the inside. You can do it.

In addition, the pyrolysis gas introduction pipe is preferably provided substantially horizontally with respect to the direction of gravity on the biomass pyrolyzer side between the biomass pyrolyzer and the pyrolysis gas reformer, It has a structure that rises upward toward the pyrolysis gas reformer side. As described above, since the pyrolysis gas introduction pipe is provided substantially horizontally with respect to the direction of gravity on the biomass pyrolysis device side, a plurality of granular materials and / or lumps are formed inside the pyrolysis gas introduction pipe. The plurality of granular materials and / or agglomerates retained in the pyrolysis gas introduction pipe are easily moved into the biomass pyrolysis device from the top to the bottom by gravity. Along with the flow of the lump, it can be gradually and gradually replaced with a plurality of particles and / or lump that are moving from top to bottom. And thereby, the some granular material and / or lump which were hold | maintained inside the pyrolysis gas introduction pipe | tube can keep a new state. On the other hand, the pyrolysis gas introduction pipe has a structure that rises upward toward the pyrolysis gas reformer side downstream of the horizontal pipe, that is, on the pyrolysis gas reformer side. In addition, it is possible to avoid mixing a plurality of particulates and / or lumps that have flowed into the pyrolysis gas introduction pipe from the biomass pyrolyzer into the pyrolysis gas reformer. As described above, since a plurality of granular materials and / or lumps are held inside the pyrolysis gas introduction pipe, they are included in the pyrolysis gas that passes through them and is introduced into the pyrolysis gas reformer. The tar, dust, and the like that are collected are brought into contact with the plurality of granular materials and / or lumps. Then, a part or most of the trapped tar is pyrolyzed and gasified by the heat of the plurality of particulates and / or lumps, and is preferably further modified. Further, tar and dust remaining without being gasified are discharged from the bottom portion of the biomass pyrolyzer while adhering to a plurality of granular materials and / or bulk materials. Thereby, tar and dust can be effectively removed from the pyrolysis gas.

In the pyrolysis gas introduction pipe, a horizontal pipe extending from the biomass pyrolysis device side is connected to the pyrolysis gas reformer on the pyrolysis gas reformer side between the biomass pyrolysis device and the pyrolysis gas reformer. What is necessary is just to have the structure which stood up upwards. The rising angle is not particularly limited and is more than 0 degree (horizontal) and 90 degrees or less. For example, it may be configured to rise upward at a substantially right angle and connect to the bottom of the pyrolysis gas reformer, or to rise slightly from the horizontal and connected to the side or bottom of the pyrolysis gas reformer. Also good. The rising angle is preferably 5 degrees or more from the horizontal, more preferably 10 degrees or more from the horizontal, and further preferably 15 degrees or more from the horizontal. Here, when the rising angle is large, for example, when it exceeds 45 degrees from the horizontal, it is preferably 5 toward the bottom of the horizontal piping at the rising portion from the biomass pyrolyzer side toward the pyrolysis gas reformer side. It is preferable to provide a protrusion having an inclination angle (θ) of ˜45 degrees, more preferably 10 to 30 degrees, and still more preferably 15 to 25 degrees. This facilitates replacement of a plurality of particulates and / or lumps entering the pyrolysis gas introduction pipe and avoids stagnation of the plurality of particulates and / or lumps at the rising portion. Can do. In the pyrolysis gas introduction pipe, the outer shape of 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. It is. The pyrolysis gas introduction pipe is preferably provided between 1 and 3 and more preferably 1 or 2 between the biomass pyrolyzer and the pyrolysis gas reformer. Also in the gasifier of the present invention (second apparatus configuration), the pyrolysis gas introduction pipe used in the first apparatus configuration described above, that is, provided substantially horizontally in the direction of gravity. It is also possible to use a pyrolysis gas introduction pipe whose inner bottom surface protrudes upward. For example, the pyrolysis gas introduction pipe (II, III, IV, VII, VIII, IX) shown in FIG. 4 can be used. Preferably, the pyrolysis gas introduction pipe (III, IV, VIII, IX) shown in FIG. 4 can be used. Since the pyrolysis gas introduction pipe is horizontal and the inner bottom surface protrudes upward, a plurality of particulates and / or lumps that have entered from the biomass pyrolyzer enter the pyrolysis gas reformer. Can be effectively avoided. However, in a long-term operation, a plurality of granular materials and / or agglomerates may enter the pyrolysis gas reformer, so that the pyrolysis gas reformer side of the pyrolysis gas reformer side protrudes. A plurality of granular and / or lump pools (collecting sections) are provided at the bottom of the introduction pipe or inside the pyrolysis gas reformer, and if necessary, the granular and / or lump collected regularly. Is preferably extracted.

In the gasifier of the present invention, a preheater for preheating a plurality of granular materials and / or agglomerates is provided on the upper part of the biomass pyrolyzer. Thereby, this some granular material and / or lump are heated to predetermined temperature. Also, a plurality of granular and / or lump inlets are provided above (upper), preferably at the top of the biomass pyrolyzer, while below (lower), preferably at the bottom, of the biomass pyrolyzer. A plurality of granular and / or massive outlets are provided. For example, a so-called two-stage valve system in which a plurality of granular materials and / or massive inlets and outlets are provided with a total of two valves, one above and one below the pipe, is used. However, the introduction and extraction method is an example, and the present invention is not limited to this method. Further, the above-mentioned pool part (collecting part) can be extracted by the same method. On the other hand, the pyrolysis gas reformer is provided with a flow path of a gaseous or liquid heat medium heated in advance on the outside thereof. The pyrolysis gas reformer may be a normal heat exchanger type pyrolysis gas reformer, and may be either a multi-tube type or a double-pipe type.

FIG. 3 shows an embodiment of the biomass gasification apparatus of the present invention, which includes a second apparatus configuration in which a plurality of pre-heated granular materials and / or agglomerates are charged only into the biomass pyrolyzer. FIG. In the biomass gasification apparatus, a plurality of pre-heated particulates and / or agglomerates (7), that is, a biomass pyrolyzer (3) that performs thermal decomposition of biomass by heat of a heat carrier, And a heat exchanger type pyrolysis gas reformer (2) for reforming the pyrolysis gas generated by the pyrolysis of biomass by the heat of the preheated gaseous or liquid heat medium. ing. And the preheater (1) for heating a some granular material and / or lump (7) previously is provided in the upper part of the biomass pyrolyzer (3). Moreover, the pyrolysis gas introduction pipe (9) is provided in one between the biomass pyrolysis device (3) and the pyrolysis gas reformer (2), and thereby the biomass pyrolysis device (3). The pyrolysis gas generated in is introduced into the pyrolysis gas reformer (2). Here, the pyrolysis gas introduction pipe (9) has a plurality of granular and / or lump (7) layers formed in the biomass pyrolyzer (3) on the biomass pyrolyzer (3) side. It is provided on the side surface of the biomass pyrolyzer (3) below the upper surface (13). That is, the biomass pyrolyzer (3) side gas intake (gas inlet) (9-3) of the pyrolysis gas introduction pipe (9) is provided in the plurality of granular and / or massive (7) layers. ing. On the other hand, on the pyrolysis gas reformer (2) side, the pyrolysis gas introduction pipe (9) is connected to the bottom of the pyrolysis gas reformer (2). In addition, the pyrolysis gas introduction pipe (9) is provided substantially horizontally with respect to the direction of gravity on the biomass pyrolyzer (3) side, and toward the pyrolysis gas reformer (2) on the downstream side thereof. Standing up almost vertically. 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 from the biomass pyrolyzer (3) side to the pyrolysis gas reformer (2) side. A protrusion having

A plurality of granulates and / or agglomerates (7), i.e. a heat carrier, is introduced into the biomass pyrolyzer (3) before it is introduced into the biomass pyrolyzer (3) with a preheater (1 ) In advance. In the preheater (1) provided at the top of the biomass pyrolyzer (3), the heat carrier (7) is preferably heated to 700 to 800 ° C, more preferably 750 to 800 ° C. If it is less than the said minimum, biomass may not fully be thermally decomposed in a biomass pyrolyzer (3). Even if the upper limit is exceeded, as already described in the description of FIG. 1 above, the amount of steam blown into the biomass pyrolyzer (3) is changed, and the temperature is controlled to an appropriate temperature so that the thermal decomposition of the biomass is efficient. Can be implemented. However, it is preferable to further increase the thermal efficiency by setting the temperature of the heat carrier (7) to the upper limit or less.

In FIG. 3, the pyrolysis gas reformer (2) is a so-called heat exchanger type pyrolysis gas reformer. The pyrolysis gas introduced from the pyrolysis gas introduction pipe (9) is mixed with the steam further introduced from the steam inlet (11 ₂ ) to form a heat exchanger type pyrolysis gas reformer (2). It is reformed by heat exchange with a heat medium that passes through the outer jacket, for example, hot hot air. Conditions such as gas phase temperature and pressure in the heat exchanger type pyrolysis gas reformer (2) are the same as those in the apparatus shown in FIG. Here, the gas phase temperature of the heat exchanger type pyrolysis gas reformer (2) is the gas phase temperature near the reformed gas outlet (8) in the upper part of the pyrolysis gas reformer (2). To tell. The gas phase temperature includes the amount of steam supplied from the steam inlet (11 ₂ , 11 ₃ ) and the amount of pyrolysis gas with respect to the amount of pyrolysis gas supplied from the biomass pyrolyzer (3). It can be controlled by appropriately changing the temperature and flow rate of the heat medium passing through the jacket of the reformer (2).

EXAMPLES Hereinafter, although an Example demonstrates this invention still in detail, this invention is not limited by these Examples.

Example 1
The biomass material used in Example 1 and the gasifier used for thermal decomposition and gas reforming of the biomass material are as follows.

As the biomass material, construction waste wood was used. The waste wood was crushed and used. The size of the waste wood after pulverization was about the size of sawdust, and the maximum size was about 2 to 6 mm. Table 1 shows the properties of the waste wood.

For each value in Table 1,
Moisture conforms to JIS Z 7302-3: 2009,
Ash content conforms to JIS Z 7302-4: 2009,
Volatile content conforms to JIS M 8812-7: 2006, and
The higher heating value is measured in accordance with JIS Z 7302-2: 1999.
In addition, among the elemental compositions, carbon (C), hydrogen (H), and nitrogen (N) all comply with JIS Z 7302-8: 2002,
Sulfur (S) conforms to JIS Z 7302-7: 2002, and
Chlorine (Cl) is measured in accordance with JIS Z 7302-6: 1999.
Further, oxygen (O) is obtained by subtracting each mass% of C, H, N, S, Cl and ash from 100 mass%.
Here, the ash, volatile matter, fixed carbon, and elemental composition are all calculated on a dry basis. In addition, the moisture is from when the biomass raw material is received.

As the gasifier used for the thermal decomposition of the biomass material and the reforming of the generated pyrolysis gas, the one shown in FIG. 1 was used. The gasifier had an apparatus configuration in which a biomass pyrolyzer (3) and a pyrolytic gas reformer (2) were arranged in parallel with the flow of the heat carrier (7). The biomass pyrolyzer (3) and the pyrolysis gas reformer (2) are provided with one preheater (1), and in the preheater (1), the biomass pyrolyzer (3) and the pyrolysis are provided. The heat carrier (7) to be supplied to both of the gas reformers (2) was preliminarily heated in advance. The biomass pyrolyzer (3) had an inner diameter of about 180 mm, a height of about 1,000 mm, and an internal volume of about 25 liters. The pyrolysis gas reformer (2) had an inner diameter of about 180 mm, a height of about 2,350 mm, and an internal volume of about 60 liters. As the pyrolysis gas introduction pipe (9), the one having the structure shown in FIG. 4 (VIII) was used. Here, the inclination angle (θ) of the protrusion was 25 degrees on both sides. The pyrolysis gas introduction pipe (9) is disposed in the biomass pyrolysis device (3) and the pyrolysis gas reformer (2) on both sides of the biomass pyrolysis device (3) and the pyrolysis gas reformer (2). They were provided on the side surfaces of the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) below the upper surface (13) of the heat carrier (7) layer formed respectively. Further, the pyrolysis gas introduction pipe (9) was provided substantially horizontally with respect to the direction of gravity. The length of the pyrolysis gas introduction pipe (9) is about 500 mm, and the outer shape of the cross section perpendicular to the longitudinal direction, that is, the cross section perpendicular to the flow direction of the pyrolysis gas is a substantially square having a side of 180 mm. , the vertical width of the gas inlet of the pyrolysis gas inlet pipe (height) (h ₁₎ and the gas inlet of the vertical width (height) (h ₂₎ were both 150 mm. As the heat carrier (7), a substantially spherical alumina ball having a diameter (maximum diameter) of 10 to 12 mm was used.

The biomass pyrolyzer (3) and pyrolytic gas reformer (2), and the preheater (1) are pre-filled with a heat carrier (7) to a height of about 70% of each container, and then The heat carrier (7) was heated to a temperature of about 500 ° C. in the preheater (1). The heat carrier (7) is then separately introduced from the top of the biomass pyrolyzer (3) and pyrolysis gas reformer (2) in an amount of 30 kilograms / hour respectively, and the biomass pyrolyzer ( 3) and an appropriate amount were separately extracted from the bottom of the pyrolysis gas reformer (2), and circulation of the heat carrier (7) was started. By the circulation of the heat carrier (7), the gas phase temperature inside the biomass pyrolyzer (3) and pyrolytic gas reformer (2) and the temperature of the container itself gradually increased. 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 to gradually increase the gas phase temperature inside the biomass pyrolyzer (3) and the pyrolysis gas reformer (2), From the time when the gas phase temperature of the pyrolyzer (3) exceeds 600 ° C., the biomass pyrolyzer (3) from the biomass supply port (4), the non-oxidizing gas supply port (12) and the steam inlet (11 ₁ ). ), Biomass raw material, nitrogen gas and steam were introduced, respectively, and the temperature of the biomass pyrolyzer (3) was controlled to 600 ° C. On the other hand, steam was further introduced and controlled from the steam inlet (11 ₂ ) so that the gas phase temperature of the pyrolysis gas reformer (2) was 950 ° C. At this time, the heat carrier (7) is deposited in layers in the biomass pyrolyzer (3) and the pyrolysis gas reformer (2), and the amount of deposition is the biomass pyrolyzer (3). And about 60% by volume of the internal volume of the pyrolysis gas reformer (2). The extraction amount of the heat carrier (7) from the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) is the same as the supply amount, and the biomass pyrolyzer (3) and pyrolysis gas reformer are the same. It was 30 kilograms / hour in the quality organ (2). Moreover, the temperature of the heat carrier (7) at the time of extraction was 400 ° C. for all. However. The extraction amount of the heat carrier (7) from the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) can be individually controlled according to the respective temperature conditions.

In the above operation, the construction waste wood as a biomass raw material is gradually increased from the biomass supply port (4) to the biomass pyrolyzer (3) using a quantitative feeder, and finally about It was continuously introduced at 4 kg / hour (dry basis). The temperature of the biomass pyrolyzer (3) gradually decreased with the introduction of the biomass raw material, but at the same time, nitrogen gas and superheated steam were introduced into the biomass pyrolyzer (3) while adjusting the supply amount. As a result, the temperature of the biomass pyrolyzer (3) was kept at 600 ° C. Moreover, the pressure in a biomass pyrolyzer (3) was hold | maintained at 101.3 kPa. Here, nitrogen gas was finally introduced at a fixed amount of 60 liters / hour from the non-oxidizing gas supply port (12) provided in the upper part of the biomass pyrolyzer (3). As the steam, superheated steam (160 ° C., 0.6 MPa) is used, and finally 2 kg / hour from the steam inlet (11 ₁ ) provided at the top of the biomass pyrolyzer (3). Was introduced in a certain amount. The residence time of the biomass raw material in the biomass pyrolyzer (3) was about 1 hour. As a result, gas generated by pyrolysis in the biomass pyrolyzer (3) was obtained at 5.2 kg / hour. Char was discharged from the pyrolysis residue (char) discharge port (6) at 0.8 kg / hour.

The pyrolysis gas obtained in the biomass pyrolyzer (3) subsequently passes through the pyrolysis gas introduction pipe (9) from the lower part of the biomass pyrolyzer (3) and is maintained at the above temperature. It was introduced into the reformer (2). At the beginning of the introduction of the pyrolysis gas, the temperature in the biomass pyrolyzer (3) becomes unstable, but from the steam inlet (11 ₂ ) provided at the bottom of the pyrolysis gas reformer (2), The temperature was adjusted to 950 ° C. by introducing superheated steam (160 ° C., 0.6 MPa) while adjusting the amount thereof. At this time, the pyrolysis gas reformer (2) was maintained at a pressure of 101.3 kPa. The superheated steam from the steam inlet (11 ₂ ) provided at the lower part of the pyrolysis gas reformer (2) was finally introduced at a constant amount of 2 kilograms / hour.

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. As a result, a reformed gas having a temperature of 950 ° C. was obtained from the reformed gas outlet (8) in an amount of 7.2 kilograms / hour.

The resulting reformed gas was collected in a rubber bag, and the gas composition was measured by gas chromatography [GC-14A (trademark) manufactured by Shimadzu Corporation]. Table 2 shows the composition of the obtained reformed gas. In addition, the operation could be carried out continuously for 3 days. During the operation period, it was possible to maintain a good continuous operation without any trouble, in particular, trouble caused by tar. Further, during the operation period, there is no trouble that the heat carrier (7) is clogged by tar or the like in the pyrolysis gas introduction pipe (9), and the pyrolysis gas reformer ( The smooth introduction of pyrolysis gas into 2) was maintained. The amount of tar in the reformed gas taken out from the pyrolysis gas reformer (2) outlet (8) was about 0.5 g / m ³ -normal.

(Example 2)
The biomass raw material used in Example 2 and the gasifier used for thermal decomposition and gas reforming of the biomass raw material are as follows.

Palm biomass waste was used as a biomass raw material. The waste material was used after being roughly pulverized. Palm palm waste has a form in which many pieces of soft string-like pieces of wood with a thickness of about 1 to 2 mm and a length of about 3 to 30 mm overlap each other. In other words, it is like a form in which cotton yarn is frayed. It was. When coarsely pulverized, it was shaped like a yarn ball (fiber ball), and its maximum dimension was about 0 to 30 mm. Table 3 shows the properties of the waste material.

For each value in Table 3,
Moisture conforms to JIS Z 7302-3: 2009,
Ash content conforms to JIS Z 7302-4: 2009,
Volatile content conforms to JIS M 8812-7: 2006, and
The higher heating value is measured in accordance with JIS Z 7302-2: 1999.
In addition, among the elemental compositions, carbon (C), hydrogen (H), and nitrogen (N) all comply with JIS Z 7302-8: 2002,
Sulfur (S) conforms to JIS Z 7302-7: 2002, and
Chlorine (Cl) is measured in accordance with JIS Z 7302-6: 1999.
Further, oxygen (O) is obtained by subtracting each mass% of C, H, N, S, Cl and ash from 100 mass%.
Here, the ash, volatile matter, fixed carbon, and elemental composition are all calculated on a dry basis. In addition, the moisture is from when the biomass raw material is received.

The gasifier used for pyrolysis and gas reforming of the biomass raw material was the same as that used in Example 1, and the one shown in FIG. 1 was used.

Under the same conditions and operation method as in Example 1, the temperatures of the pyrolysis gas reformer (2) and the biomass pyrolyzer (3) were 950 ° C. and 600 ° C., respectively. Moreover, the temperature of the heat carrier (7) at the time of extraction was 400 ° C. for all.

In the operation of controlling the temperatures of the pyrolysis gas reformer (2) and the biomass pyrolyzer (3) to the above-mentioned predetermined values, the palm palm waste material as the biomass raw material is supplied to the biomass supply port (4 ) To the biomass pyrolyzer (3), while gradually increasing the supply amount, it was continuously introduced to finally reach about 5 kilograms / hour (dry basis). The temperature of the biomass pyrolyzer (3) gradually decreased with the introduction of the biomass raw material, but at the same time, nitrogen gas and superheated steam were introduced into the biomass pyrolyzer (3) while adjusting the supply amount. As a result, the temperature of the biomass pyrolyzer (3) was kept at 600 ° C. Moreover, the pressure in a biomass pyrolyzer (3) was hold | maintained at 101.3 kPa. Here, nitrogen gas was finally introduced at a fixed amount of 6 liters / hour from the non-oxidizing gas supply port (12) provided in the upper part of the biomass pyrolyzer (3). As the steam, superheated steam (160 ° C., 0.6 MPa) is used, and finally 2 kg / hour from the steam inlet (11 ₁ ) provided at the top of the biomass pyrolyzer (3). Was introduced in a certain amount. The residence time of the biomass raw material in the biomass pyrolyzer (3) was about 1 hour. Thereby, the gas produced | generated by the pyrolysis in the biomass pyrolyzer (3) was obtained at 6.1 kilogram / hour. Further, char was discharged from the pyrolysis residue (char) discharge port (6) at 0.9 kg / hour.

The pyrolysis gas obtained in the biomass pyrolyzer (3) is subsequently passed through the pyrolysis gas introduction pipe (9) from the bottom of the biomass pyrolyzer (3) to a temperature of 950 ° C. and a pressure of 101.3 kPa. It was introduced into the retained pyrolysis gas reformer (2). At the beginning of the introduction of the pyrolysis gas, the temperature in the biomass pyrolyzer (3) becomes unstable, but from the steam inlet (11 ₂ ) provided at the bottom of the pyrolysis gas reformer (2), The temperature was adjusted to 950 ° C. by introducing superheated steam (160 ° C., 0.6 MPa) while adjusting the amount thereof. At this time, the pyrolysis gas reformer (2) was maintained at a pressure of 101.3 kPa. The superheated steam from the steam inlet (11 ₂ ) provided at the lower part of the pyrolysis gas reformer (2) was finally introduced at a fixed amount of 3 kilograms / hour.

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. As a result, a reformed gas having a temperature of 950 ° C. was obtained from the reformed gas outlet (8) in an amount of 9.1 kilograms / hour.

The resulting reformed gas was collected in a rubber bag, and the gas composition was measured by gas chromatography [GC-14A (trademark) manufactured by Shimadzu Corporation]. Table 4 shows the composition of the reformed gas obtained. In addition, the operation could be carried out continuously for 3 days. During the operation period, it was possible to maintain a good continuous operation without any trouble, in particular, trouble caused by tar. Further, during the operation period, there is no trouble that the heat carrier (7) is clogged by tar or the like in the pyrolysis gas introduction pipe (9), and the pyrolysis gas reformer ( The smooth introduction of pyrolysis gas into 2) was maintained. The amount of tar in the reformed gas taken out from the pyrolysis gas reformer (2) outlet (8) was about 0.5 g / m ³ -normal.

(Example 3)
The biomass raw material used is the same as that used in Example 1. Moreover, what was shown in FIG. 2 was used for the gasification apparatus used for the thermal decomposition and gas reforming of biomass raw material. The used apparatus was the apparatus structure which has arrange | positioned the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) in parallel with respect to the flow of the heat carrier (7). The biomass pyrolyzer (3) and the pyrolysis gas reformer (2) are each provided with one preheater (1 ₂ , 1 ₁ ), and in the preheater (1 ₂ , 1 ₁ ), The heat carrier (7) supplied to the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) is separately heated in advance. In addition, the dimensions and capacity of the biomass pyrolyzer (3) and pyrolysis gas reformer (2), the shape and dimensions of the pyrolysis gas introduction pipe (9), and the pyrolysis gas introduction pipe (9) are in the direction of gravity. And the material and dimensions of the heat carrier (7) were the same as those of Example 1.

The biomass carrier (3), pyrolysis gas reformer (2), and preheater (1 ₂ , 1 ₁ ) are pre-filled with a heat carrier (7) to a height of about 70% of each container. Then, the heat carrier (7) was preheated to a temperature of about 500 ° C. in the preheater (1 ₂ , 1 ₁ ), respectively. Each heat carrier (7) is then introduced separately from the top of the biomass pyrolyzer (3) and pyrolytic gas reformer (2) in an amount of 30 kilograms / hour, respectively, and the biomass pyrolyzer Appropriate amounts were separately extracted from the bottom of (3) and the pyrolysis gas reformer (2), respectively, and circulation of the heat carrier (7) was started. By the circulation of the heat carrier (7), the gas phase temperature inside the biomass pyrolyzer (3) and pyrolytic gas reformer (2) and the temperature of the container itself gradually increased. While continuing the circulation of the heat carrier (7), the temperature of the heat carrier (7) inside the preheater (1 ₂ ) is gradually raised to 800 ° C., while the inside of the preheater (1 ₁ ) The temperature of the heat carrier (7) was gradually raised to 1,050 ° C. After each heat carrier (7) reaches the above temperature, the circulation is further continued to gradually increase the gas phase temperature inside the biomass pyrolyzer (3) and pyrolysis gas reformer (2). From the time when the gas phase temperature of the biomass pyrolyzer (3) exceeds 600 ° C, the biomass pyrolyzer is introduced from the biomass supply port (4), the non-oxidizing gas supply port (12), and the steam inlet (11 ₁ ). In (3), biomass raw material, nitrogen gas and steam were introduced, respectively, and the temperature of the biomass pyrolyzer (3) was controlled to 600 ° C. On the other hand, steam was further introduced and controlled from the steam inlet (11 ₂ ) so that the gas phase temperature of the pyrolysis gas reformer (2) was 950 ° C. At this time, the heat carrier (7) is deposited in layers in the biomass pyrolyzer (3) and the pyrolysis gas reformer (2), and the amount of deposition is the biomass pyrolyzer (3). And about 60% by volume of the internal volume of the pyrolysis gas reformer (2). The extraction amount of the heat carrier (7) from the biomass pyrolyzer (3) and the pyrolysis gas reformer (2) is the same as the supply amount, and the biomass pyrolyzer (3) and pyrolysis gas reformer are the same. It was 30 kilograms / hour in the quality organ (2). Moreover, the temperature of the heat carrier (7) at the time of extraction was 400 ° C. for all.

The pyrolysis gas obtained in the biomass pyrolyzer (3) subsequently passes through the pyrolysis gas introduction pipe (9) from the lower part of the biomass pyrolyzer (3) and is maintained at the above temperature. It was introduced into the reformer (2). At the beginning of introduction of the pyrolysis gas, the temperature in the pyrolysis gas reformer (2) becomes unstable, but from the steam inlet (11 ₂ ) provided at the lower part of the pyrolysis gas reformer (2). Furthermore, the temperature was adjusted to 950 ° C. by introducing superheated steam (160 ° C., 0.6 MPa) while adjusting the amount thereof. At this time, the pyrolysis gas reformer (2) was maintained at a pressure of 101.3 kPa. The superheated steam from the steam inlet (11 ₂ ) provided at the lower part of the pyrolysis gas reformer (2) was finally introduced at a constant amount of 2 kilograms / hour.

The resulting reformed gas was collected in a rubber bag, and the gas composition was measured by gas chromatography [GC-14A (trademark) manufactured by Shimadzu Corporation]. Table 5 shows the composition of the reformed gas obtained. In addition, the operation could be carried out continuously for 3 days. During the operation period, it was possible to maintain a good continuous operation without any trouble, in particular, trouble caused by tar. Further, during the operation period, there is no trouble that the heat carrier (7) is clogged by tar or the like in the pyrolysis gas introduction pipe (9), and the pyrolysis gas reformer ( The smooth introduction of pyrolysis gas into 2) was maintained. The amount of tar in the reformed gas taken out from the pyrolysis gas reformer (2) outlet (8) was about 0.5 g / m ³ -normal.

Example 4
The biomass raw material used is the same as that used in Example 1. The gasifier used for pyrolysis and gas reforming of the biomass material was the one shown in FIG. The used apparatus is that the biomass pyrolyzer (3) pyrolyzes the biomass with the heat of the heat carrier (7), and the heat exchanger type pyrolytic gas reformer (2) heats the biomass. The gas generated by the decomposition was modified by a gaseous heat medium, that is, high-temperature hot air. The dimensions and capacity of the biomass pyrolyzer (3) and pyrolytic gas reformer (2), and the material and dimensions of the heat carrier (7) are the same as those in Example 1. The pyrolysis gas introduction pipe (9) is located on the biomass pyrolyzer (3) side and is below the upper surface (13) of the heat carrier (7) layer formed in the biomass pyrolyzer (3). It was provided on the side of (3). On the other hand, on the pyrolysis gas reformer (2) side, the pyrolysis gas introduction pipe (9) was connected to the bottom of the pyrolysis gas reformer (2). The pyrolysis gas introduction pipe (9) is provided substantially horizontally with respect to the direction of gravity on the biomass pyrolyzer (3) side, and toward the bottom of the pyrolysis gas reformer (2) on the downstream side. It stood up almost vertically. 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 from the biomass pyrolyzer (3) side to the pyrolysis gas reformer (2) side. Protrusions having The pyrolysis gas introduction pipe (9) has a length of about 1,000 mm (horizontal portion: about 500 mm, rising portion: about 500 mm), and is perpendicular to the longitudinal direction, that is, with respect to the flow direction of the pyrolysis gas. The outer shape of the vertical cross section was a substantially square with a side of 180 mm.

The biomass pyrolyzer (3) and the preheater (1) are preliminarily filled with a heat carrier (7) to a height of about 70% of each container, and then the heat carrier (7) is added to the preheater (1). ) To a temperature of 500 ° C. Next, the heat carrier (7) is introduced in an amount of 30 kg / hour from the top of the biomass pyrolyzer (3), and an appropriate amount is withdrawn from the bottom of the biomass pyrolyzer (3). ) Circulation started. By circulation of the heat carrier (7), the gas phase temperature inside the biomass pyrolyzer (3) and the temperature of the container itself gradually increased. 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, the circulation is further continued to gradually increase the gas phase temperature inside the biomass pyrolyzer (3), and the gas phase temperature of the biomass pyrolyzer (3). When the temperature exceeds 600 ° C., the biomass feed port (4), the non-oxidizing gas supply port (12), and the steam blow-in port (11 ₁ ) are fed into the biomass pyrolyzer (3), respectively. And steam were introduced, and the temperature of the biomass pyrolyzer (3) was controlled to 600 ° C. On the other hand, while the high-temperature hot air of 1,200 ° C. is blown into the pyrolysis gas reformer (2) at an amount of about 2 m ³ / hour from the heating medium inlet (10 ₁ ), the pyrolysis gas reformer (2 Further, steam was introduced from the steam inlet (11 ₂ ) and controlled so that the gas phase temperature of) was 950 ° C. At this time, the heat carrier (7) was deposited in layers in the biomass pyrolyzer (3), and the amount deposited was approximately 60% by volume of the internal volume of the biomass pyrolyzer (3). The extraction amount of the heat carrier (7) from the biomass pyrolyzer (3) was the same as the supply amount, and was 30 kg / hour in the biomass pyrolyzer (3). Moreover, the temperature of the heat carrier (7) at the time of extraction was 400 degreeC.

In the above operation, the construction waste wood as a biomass raw material is gradually increased from the biomass supply port (4) to the biomass pyrolyzer (3) using a quantitative feeder, and finally about It was continuously introduced at 4 kg / hour (dry basis). The temperature of the biomass pyrolyzer (3) gradually decreased with the introduction of the biomass raw material, but at the same time, nitrogen gas and superheated steam were introduced into the biomass pyrolyzer (3) while adjusting the supply amount. As a result, the temperature of the biomass pyrolyzer (3) was kept at 600 ° C. Moreover, the pressure in a biomass pyrolyzer (3) was hold | maintained at 101.3 kPa. Here, nitrogen gas was finally introduced at a fixed amount of 60 liters / hour from the non-oxidizing gas supply port (12) provided in the upper part of the biomass pyrolyzer (3). As the steam, superheated steam (160 ° C., 0.6 MPa) is used, and finally 2 kg / hour from the steam inlet (11 ₁ ) provided at the top of the biomass pyrolyzer (3). Was introduced in a certain amount. The residence time of the biomass raw material in the biomass pyrolyzer (3) was about 1 hour. As a result, gas generated by pyrolysis in the biomass pyrolyzer (3) was obtained at 5.1 kilogram / hour. Further, char was discharged from the pyrolysis residue (char) discharge port (6) at 0.9 kg / hour.

The pyrolysis gas obtained in the biomass pyrolyzer (3) is then passed from the bottom of the biomass pyrolyzer (3) through the pyrolysis gas introduction pipe (9) to improve the heat exchanger type pyrolysis gas. Introduced into the mass device (2). In the pyrolysis gas reformer (2), high-temperature hot air previously heated to about 1,200 ° C. is provided outside the pyrolysis gas reformer (2) from the high-temperature hot air inlet (10 ₁ ). After being introduced into the heat medium flow path and exchanging heat with the pyrolysis gas flowing inside the pyrolysis gas reformer (2), it was discharged from the high temperature hot air outlet (10 ₂ ) at about 700 ° C. At the beginning of the introduction of the pyrolysis gas, the temperature in the pyrolysis gas reformer (2) becomes unstable, but gradually increases while adjusting the amount of hot hot air, and the lower part of the pyrolysis gas reformer (2) Further, superheated steam (160 ° C., 0.6 MPa) is introduced from the steam inlet (11 ₂ ) provided in the tank while adjusting the amount thereof, thereby allowing the inside of the pyrolysis gas reformer (2). 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 inlet (11 ₂ ) provided at the lower part of the pyrolysis gas reformer (2) was finally introduced at a constant amount of 2 kilograms / hour.

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. As a result, a reformed gas having a temperature of 900 ° C. was obtained from the reformed gas outlet (8) in an amount of 7.1 kilogram / hour.

The resulting reformed gas was collected in a rubber bag, and the gas composition was measured by gas chromatography [GC-14A (trademark) manufactured by Shimadzu Corporation]. Table 6 shows the composition of the reformed gas obtained. In addition, the operation could be carried out continuously for 3 days. During the operation period, it was possible to maintain a good continuous operation without any trouble, in particular, trouble caused by tar. Further, during the operation period, there is no trouble that the heat carrier (7) is clogged by tar or the like in the pyrolysis gas introduction pipe (9), and the pyrolysis gas reformer ( The smooth introduction of pyrolysis gas into 2) was maintained. In addition, the amount of tar in the reformed gas taken out from the pyrolysis gas reformer (2) outlet (8) was about 0.8 g / m ³ -normal.

(Comparative Example 1)
As the gasifier used for the pyrolysis of the biomass raw material and the reforming of the generated pyrolysis gas, the one described in FIG. That is, it is an apparatus in which a reforming region (300) is provided in series above and below the pyrolysis region (200). In other words, it is an apparatus in which a biomass pyrolyzer and a pyrolysis gas reformer are connected in series up and down. In the comparative example, about one-tenth of a small experimental device was used. The gasifier used was as shown in FIG. The material of the gasifier (A) main body is Inconel. The gasification furnace (A) has a cylindrical shape with an inner diameter of 100 mm and a height of 650 mm, 300 mm from the bottom of the gasification furnace (A) is the thermal decomposition region (200), and 300 mm from the top is the reforming region (300). . In the pyrolysis region (200), an alumina ball (D) (diameter: 5 to 15 mm) was used as a heat medium. The upper part of the reforming region (300) is filled with a nickel catalyst (E). A steam inlet (400) is provided between the thermal decomposition region (200) and the reforming region (300). In addition, electric heaters (B) and (C) capable of temperature control are installed on the outer walls of the gasification furnace in the pyrolysis region (200) and the reforming region (300), respectively.

As the raw material, the same construction waste wood as in Example 1 was used. The raw material was intermittently introduced from the raw material supply pipe (100) into the thermal decomposition region (200) of the gasification furnace (A) at intervals of 30 to 40 seconds every 30 minutes by airflow conveyance. The pyrolysis region (200) of the gasification furnace (A) was controlled to a temperature of 550 ° C. by heating an alumina ball as a heating medium using an electric heater (B). The pyrolysis region (200) was maintained at a pressure of 0.103 MPa by introducing helium gas at 0.50 liter / min from the bottom (600) thereof. The waste wood was pyrolyzed, and the generated gas was introduced into the reforming region (300) of the gasification furnace (A) maintained at the same pressure, and mixed with steam.

The temperature of the reforming region (300) of the gasification furnace (A) was 1,000 ° C., and the gas temperature at the outlet (500) of the reforming region (300) was 947 ° C. The temperature of the reforming zone (300) was controlled to be constant by the electric heater (C). The composition of the obtained reformed gas is as shown in Table 7. Further, the amount of tar in the reformed gas on the outlet side of the reforming region (300) was about 5 g / m ³ -normal. In the apparatus, the operation could be carried out continuously for 3 days, but the pressure in the pyrolysis region (200) began to increase slightly after the second day. After completion of the operation, the alumina ball (D) layer was inspected, and tar deposition was observed. Therefore, it is assumed that there is a problem with long-term continuous operation.

In Examples 1 and 2, biomass raw materials are changed. Any biomass raw material can be continuously operated without any trouble caused by tar during the operation period, and the heat carrier (7) is caused by tar or the like in the pyrolysis gas introduction pipe (9). The smooth introduction of pyrolysis gas from the biomass pyrolyzer (3) to the pyrolysis gas reformer (2) was maintained without causing the trouble of blocking. In addition, the amount of tar in the resulting reformed gas was extremely small. In Example 3, a preheater (1 ₂ , 1 ₁ ) is separately installed on the upper part of the biomass pyrolyzer (3) and the pyrolysis gas reformer (2), and the heat carrier (7) is respectively installed. A gasifier is used which is heated to different temperatures and supplied to the biomass pyrolyzer (3) and the pyrolysis gas reformer (2). As in Examples 1 and 2, good operation could be ensured, and the amount of tar in the resulting reformed gas was extremely small. In Example 4, a heat exchanger type reformer that is heated with high-temperature hot air is used as the pyrolysis gas reformer (2). As in Examples 1 to 3, good operation could be secured. Further, although the amount of tar in the obtained reformed gas slightly increased, it did not hinder the smooth operation of the apparatus. Comparative Example 1 uses a conventional apparatus. Tar deposition on the alumina ball (D) layer was observed, and it was found that there was a problem with long-term continuous operation. In addition, from the results of Examples 1 to 4 and Comparative Example 1, in any case, the reformed gas composition is almost equal, and if the gasifier of the present invention is used, a conventional vertical series two-stage gasifier is used. It was found that gasification treatment can be performed to the same extent. Further, the amount of tar in the reformed gas is significantly reduced in the apparatus of the present invention, indicating that it is useful as a biomass gasification apparatus.

According to the biomass gasification apparatus of the present invention, the amount of pyrolysis gas generated is increased by optimizing the pyrolysis temperature of biomass and the reforming temperature of the generated pyrolysis gas, and is the final product. Not only can the production amount of hydrogen-containing gas be increased, but also the generation amount of tar and dust can be reduced. In addition, the generated tar can be effectively gasified, and the tar and dust remaining without being gasified can be efficiently recovered, thereby significantly reducing the trouble of the equipment due to tar and dust. Therefore, it is expected that the gasification apparatus of the present invention will be greatly utilized for biomass gasification in the future. In addition, it is expected to be used for hydrogen production business and power generation business.

1, 1 ₁ , 1 ₂ Preheater 2 Pyrolysis gas reformer 3 Biomass pyrolyzer 4 Biomass supply port 5 Waste treatment device 6 Pyrolysis residue (char) discharge port 7 Multiple granular and / or lump [ Thermal support medium (heat carrier)]
8 Reformed gas outlet 9 Pyrolysis gas introduction pipe 9-2 Pyrolysis gas reformer side gas introduction port (gas outlet) of pyrolysis gas introduction pipe
9-3 Biomass pyrolyzer side gas inlet of the pyrolysis gas inlet pipe (gas inlet)
10 ₁ , 10 ₂ Heat medium inlet,

outlet

11 ₁ , 11 ₂ , 11 ₃ Steam inlet 12 Non-oxidizing gas supply port 13 A plurality of formed in the biomass pyrolyzer and pyrolytic gas reformer, respectively The upper surface g of the granular material and / or the lump material layer The flow direction h of the pyrolysis gas h The height h of the protruding portion of the inner bottom surface of the pyrolysis gas introduction tube ₁ The vertical width (height of the gas inlet of the pyrolysis gas introduction tube )
h ₂ Vertical width (height) of the gas inlet of the pyrolysis gas inlet pipe
θ Inclination angle A of the inner bottom protrusion of the pyrolysis gas inlet tube A Gasification furnace B Electric heater C Electric heater D Alumina ball (heat medium)
E Nickel catalyst 100 Raw material supply pipe 200 Pyrolysis region 300 Reforming region 400 Steam inlet 500 Reformed gas outlet 600 Helium inlet

Claims

Biomass pyrolyzer having a biomass supply port, a non-oxidizing gas supply port and / or a steam blow-in port, a pyrolysis gas reformer having a steam blow-in port and a reformed gas discharge port, and the biomass heat A pyrolysis gas introduction pipe provided between the biomass pyrolysis device and the pyrolysis gas reformer for introducing the pyrolysis gas generated in the cracker into the pyrolysis gas reformer; In addition, the biomass pyrolyzer and the pyrolysis gas reformer each further include a plurality of preheated granular and / or lump inlets and outlets, and the plurality of granular and / or The biomass pyrolyzer and the pyrolysis gas in the biomass gasification apparatus for performing the pyrolysis of the biomass and reforming of the pyrolysis gas generated by the pyrolysis of the biomass by the heat of the lump. And a pyrolyzed gas introduction pipe, the biomass pyrolyzer and the pyrolytic gas reformer are provided in parallel with the flow of the plurality of particulates and / or agglomerates. The biomass pyrolyzer and the pyrolysis gas below the upper surfaces of the plurality of granular and / or lump layers formed in the biomass pyrolyzer and the pyrolysis gas reformer, respectively, on both sides of A biomass gasification apparatus which is provided on a side surface of a reformer and wherein the pyrolysis gas introduction pipe is provided substantially horizontally with respect to a direction of gravity.
The biomass gasification apparatus according to claim 1, wherein an inner bottom surface of the pyrolysis gas introduction pipe has a structure protruding upward.
The inner bottom surface of the pyrolysis gas introduction pipe has a structure projecting upward with an inclination from both sides of the biomass pyrolyzer and the pyrolysis gas reformer to the center. Biomass gasifier.
The biomass gasification apparatus according to any one of claims 1 to 3, wherein an outer shape of a cross section perpendicular to the longitudinal direction of the pyrolysis gas introduction pipe is substantially rectangular.
The biomass gasification apparatus according to any one of claims 1 to 4, wherein one or two of the pyrolysis gas introduction pipes are provided.
The biomass gasification apparatus according to any one of claims 1 to 5, wherein the pyrolysis gas introduction pipe has the plurality of particulates and / or agglomerates therein.
Biomass pyrolyzer having a biomass supply port, a non-oxidizing gas supply port and / or a steam blow-in port, a pyrolysis gas reformer having a steam blow-in port and a reformed gas discharge port, and the biomass heat A pyrolysis gas introduction pipe provided between the biomass pyrolysis device and the pyrolysis gas reformer for introducing the pyrolysis gas generated in the cracker into the pyrolysis gas reformer; The biomass pyrolyzer further includes a plurality of pre-heated granular and / or lump inlets and outlets, and the heat of the plurality of granular and / or lump-like materials causes the biomass to decompose. On the other hand, the pyrolysis gas reformer is further provided with a flow path of a gaseous or liquid heating medium preheated outside thereof, and heat of the biomass is generated by the heat of the heating medium. Caused by decomposition In the biomass gasification apparatus for performing reforming of pyrolysis gas, the pyrolysis gas introduction pipe is formed in the biomass pyrolysis device on the biomass pyrolysis device side, and the plurality of granular materials and / or Alternatively, the biomass gasification apparatus is provided on a side surface of the biomass pyrolyzer below the upper surface of the massive layer.
The pyrolysis gas introduction pipe is provided substantially horizontally with respect to the direction of gravity on the biomass pyrolyzer side between the biomass pyrolyzer and the pyrolysis gas reformer. The biomass gasification apparatus according to claim 7, wherein the biomass gasification apparatus has a structure that rises upward toward the cracked gas reformer.
The biomass gasification apparatus according to claim 7 or 8, wherein the pyrolysis gas introduction pipe has the plurality of granular materials and / or agglomerates therein.
A biomass pyrolyzer that heats biomass in a non-oxidizing gas atmosphere or a mixed gas atmosphere of non-oxidizing gas and steam, and heat that heats the gas generated in the biomass pyrolyzer in the presence of steam A plurality of granules and / or lump that have been heated in advance and are put into the biomass pyrolyzer and the pyrolysis gas reformer, and the plurality of granules and In the method for biomass gasification in which the pyrolysis of biomass and the reforming of pyrolysis gas generated by the pyrolysis of biomass are performed by the heat of the lump, the plurality of granules and / or lump is the above The biomass pyrolyzer and the pyrolysis gas reformer provided in parallel to the flow of a plurality of particulates and / or agglomerates are separately charged, The pyrolysis gas generated in the pyrolyzer is formed in the biomass pyrolyzer and the pyrolysis gas reformer on both sides of the biomass pyrolyzer and the pyrolysis gas reformer, respectively. Pyrolysis gas provided on the side surfaces of the biomass pyrolyzer and pyrolysis gas reformer below the upper surface of the plurality of granular and / or lump layers and provided substantially horizontally with respect to the direction of gravity A method for gasifying biomass that is introduced into the pyrolysis gas reformer and reformed through an introduction pipe.
The biomass gasification method according to claim 10, wherein an inner bottom surface of the pyrolysis gas introduction pipe has a structure protruding upward.
The biomass gasification method according to claim 10 or 11, wherein the pyrolysis gas introduction pipe has the plurality of granular materials and / or agglomerates therein.