JP2015004021A - Thermal decomposition gasification furnace, catalytic modification method, energy supply system and electric heat supply system - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a thermal decomposition gasification furnace for biomass and a catalytic modification method which improve the production yield of a modified gas serving as a raw material for gas fuels and ethanol fuels for diesel generator and the gasification conversion efficiency by reducing solid, e.g. char, and tar fractions produced in the thermal decomposition gasification furnace for forest biomass, wood debris and agricultural waste.SOLUTION: A thermal decomposition gasification furnace and a catalytic modification method are provided. In a catalytic modification reactor connected directly to the thermal decomposition gasification furnace for wood biomass, tar, etc. accompanying a gas produced in the body of the thermal decomposition gas furnace is brought into contact with a modification gasification catalyst to produce a raw material gas for gas fuels for power generation and ethanol synthesis having a hydrogen-rich gas composition of an H/CO mol ratio of 1 or higher with high gasification conversion efficiency and high efficiency with reduced production costs.

Description

  The present invention relates to a pyrolysis gasification furnace using a woody biomass, rubble material, agricultural waste, or the like as a raw material and a catalytic reforming method thereof, a biomass energy supply system, and an electric heat supply system.

Until now, woody biomass has been used as a combustion fuel for power generation or has been treated as waste. The pyrolysis gasification of biomass has many advantages from the viewpoint of environmental protection. That is, biomass gas (mixed gas containing CO, hydrogen, methane, etc.) obtained by pyrolysis gasification of biomass is used as a fuel gas for power generation. On the other hand, using an Rh composite catalyst from biomass gas obtained by gasification of biomass (H ₂ / CO molar ratio is 1 or more), ethanol fuel is highly efficient at pressures of 1MPa to 3MPa and temperatures of 260 ° C to 285 ° C. An ethanol direct synthesis catalyst technology to be synthesized has been developed (Patent Document 1). By combining these utilization methods, biomass gas can be used to supply tri-generation biomass energy that co-produces ethanol fuel using power generation, heat, and ethanol synthesis technology. Thus, to improve the utilization efficiency of biomass energy and it is possible to reduce CO ₂ emission is global warming factor (Non-Patent Document 1).

Therefore, the importance of technological development in this field is to develop a pyrolysis gasification technology with higher gasification conversion efficiency and more compact and economical in the development of biomass pyrolysis gasification furnace (non-patent literature). 2-4). On the other hand, the most serious problem in the conventional pyrolysis gasification technology is that a large amount of solid char, coke and tar is generated in addition to fuel gas components such as CO, hydrogen and methane (Non-patent Document 5). ).

  In order to reduce coke and tar emissions in biomass pyrolysis gasification, this pyrolysis gasification should be operated at a lower temperature. However, it is known that when the thermal decomposition reaction is performed at a low temperature, the gasification yield decreases and the generation of tar increases (Non-Patent Document 6). On the other hand, biomass pyrolysis gasification technology using a catalyst has been studied, but the efficiency of conversion to fuel gas is low and the catalytic activity deteriorates rapidly. There are technical challenges.

Japanese Patent No. 5052703

Supervised by Masaru Ichikawa "New Development of Biomass Refinery Catalyst Technology" CM Publishing 2011 I. Narvaez et al. Ind. Eng. Chem. Res. 35, 1996, 2110 D. Xianwen et al. Energy Fuels 14, 2000, 552 I. D. Barn et al. EnergyFuels 14, 2000, 889 M. A. Caballero et al. Ind. Eng. Chem. Res. 29, 2000, 1143 D. N. Bangala et al., Ind. Eng. Chem. Res. 36, 1997, 4184

In the conventional pyrolysis gas furnace for biomass, the production of solid components consisting of coke and char and tar is increased, and the gasification conversion efficiency of raw material gas for power generation and ethanol synthesis is 45% or less, which is economical. There are also problems in terms of cost.

This invention is made | formed in view of the said situation, and the objective of this invention is gas by making the gaseous component containing the tar etc. which arise in the process of thermally decomposing and biomassing a biomass with a reforming gasification catalyst. Pyrolysis gasification furnace and catalytic reforming for economical and low-cost production of gas raw materials for chemical synthesis such as ethanol synthesis with high gasification conversion efficiency and gas yield and gas composition with H ₂ / CO molar ratio of 1 or more Develop a method.

The present inventors use various woody biomass (wood, bark, bacus, rice straw, vegetation, etc.) and waste biomass (food waste, sludge, livestock manure, marine waste, industrial waste, etc.) In addition, the catalytic reforming effect of the metal-supported catalyst on the reforming gasification reaction of the gas component containing tar generated in the pyrolysis gasification furnace that gasifies the biomass will be studied, and the catalyst activity stabilization and catalyst regeneration method We have been studying these issues with extensive research and improvements.

As a result, tar associated with the gas generated in the main body of the pyrolysis gasifier in the catalytic reforming reactor directly connected to the gas discharge part of the pyrolysis gasifier of woody biomass, for example, the kiln type rotary gasifier Is brought into contact with the reforming gasification catalyst, so that high gasification conversion efficiency (<50%) at high pressure (0.1 MPa to 0.6 MPa) and a hydrogen-rich gas composition with a H ₂ / CO molar ratio of 1 or more. A novel pyrolysis gasification furnace and catalyst reforming method for supplying biomass gas for diesel power generation and ethanol synthesis having high efficiency with reduced production cost and CO ₂ emission amount have been found.

The biomass pyrolysis gasification furnace of the present invention is a catalyst reforming catalyst comprising a gas component containing tar, which is produced in the pyrolysis gasification process of biomass, in contact with a reformed gasification catalyst in a pyrolysis gas stream. Characterized by quality method.

The pyrolysis gasification furnace according to claim 1 is a pyrolysis gasification furnace that thermally decomposes biomass into at least a solid component and a gas component by gasification, wherein the pyrolysis gasification furnace main body and the pyrolysis gas gas A reforming catalyst reactor connected to the main body of the gasifier to gasify the tar in the gas component by a catalytic reforming reaction, and provided to surround the pyrolysis gasification furnace main body and the reforming catalyst reactor. Heating means for heating the pyrolysis gasification furnace main body and the inside of the reforming catalyst reactor, biomass supply means for supplying biomass into the pyrolysis gasification furnace main body, and in the pyrolysis gasification furnace main body A reforming gas comprising nickel, iron, platinum, cerium, and zirconium, and a porous oxide catalyst carrier. Catalyst Reformed gasification catalyst comprising ru, rhodium, molybdenum, titanium, cerium and neodymium and a porous oxide catalyst support, reformed gas comprising nickel, cobalt, cerium and lanthanum and a porous oxide catalyst support One of the reforming gasification catalysts is used.

  According to a second aspect of the present invention, there is provided the pyrolysis gasification furnace according to the first aspect, wherein the heating means burns char and bio-coke which are solid components generated in the pyrolysis gasification furnace. The combustion gas generated in the furnace is used to heat the pyrolysis gas furnace main body and the inside of the reforming catalyst reactor.

  The catalyst reforming method according to claim 3 is a reformed gasification catalyst comprising nickel, iron, platinum, cerium, and zirconium and a porous oxide catalyst support, nickel, rhodium, molybdenum, titanium, cerium, and A reformed gasification catalyst composed of neodymium and a porous oxide catalyst support, or a reformed gasification catalyst composed of nickel, cobalt, cerium, lanthanum, and a porous oxide catalyst support. Using a reforming catalytic reactor filled with a catalyst, tar in a gas component is gasified by catalytic reforming reaction.

The ethanol supply system according to claim 4 is an ethanol supply system including the pyrolysis gasification furnace according to claim 1 or 2, wherein the biomass gas generated in the pyrolysis gasification furnace is washed and It comprises a gas purification device for purification and an ethanol synthesis catalyst reactor for synthesizing ethanol using the purified gas.

An electric heat supply system according to claim 5 is an electric heat supply system including the ethanol supply system according to claim 4, wherein a liquid component such as ethanol is removed by a gas-liquid separator directly connected to the ethanol synthesis catalyst reactor. And a diesel generator for supplying electric power and heat using the separated exhaust gas as fuel.

In the embodiment of the biomass pyrolysis gasification furnace and the catalyst reforming method of the present invention, the gas component is a mixed gas such as CO, H ₂ , methane, water vapor, and CO ₂ and a gaseous tar. preferable.

In an embodiment of the biomass pyrolysis gasification furnace and catalyst reforming method of the present invention, the pyrolysis gasification is preferably performed at a temperature of 750 ° C. or lower.

In the aspect of the method for converting biomass into biomass according to the present invention, the plant is preferably at least one selected from the group consisting of wood, bark, bacus, rice straw, waste paper, and sludge.

CO pressurization generated in the gasifier in the biomass of the present invention _{(0.1MPa~0.6MPa),} H 2, methane, a mixed gas and gaseous data gaseous component consisting of one le of water vapor and CO ₂ The reforming gasification catalyst is contacted and reacted at the gasification furnace temperature.

The pyrolysis gasification furnace of the present invention has a function of generating a solid component composed of char, bio-coke and ash and a gas component from the biomass in accordance with the type of biomass at a desired temperature. The solid component is separated from the gas component, and char and ash content connected to the outlet are collected in a collection container.

  According to the present invention, gasification conversion efficiency and gas yield are increased by reacting a gas component containing tar and the like produced by pyrolyzing and gasifying biomass such as wood and agricultural waste with a reformed gasification catalyst. A pyrolysis gasification furnace and a catalyst reforming method for producing pyrolysis gas economically and at low cost are provided. At the same time, the biomass gas produced in the reforming gasification reactor connected to the pyrolysis gasification furnace is used to generate power, heat, and ethanol synthesis reactors using diesel generators for local society and industry such as alcohol synthesis fuel. Providing energy fuel can contribute to local energy independence.

The figure which shows the pyrolysis dregging furnace and catalyst reforming method of biomass by one Example of this invention

First, the outline of the present invention will be described.
In the catalytic reforming gasification reactor directly connected to the pyrolysis gasification furnace main body of the present invention, a mixed gas such as pressurized CO, H ₂ , methane, water vapor and CO ₂ generated in the pyrolysis gas furnace of biomass Is a catalytic reforming reaction of a pyrolysis gas comprising The tar and pyrolysis gas come into contact with the reforming catalyst and form a reformed gas mainly composed of CO and H ₂ by a reforming gasification reaction. The catalytic reforming gasification reaction of tar can be performed in a catalytic reforming reactor directly connected to the outlet of the pyrolysis gasification furnace in which pyrolysis gasification of biomass occurs. A fixed bed catalyst reactor and a fluidized bed reforming catalyst reactor are used depending on the mode of catalyst filling.

Further, in the present invention, “biomass gas” means a mixed gas containing carbon monoxide and hydrogen, and the pyrolysis gas generated in the pyrolysis gasification furnace of biomass includes CO ₂ , CH ₄ , Lower hydrocarbons such as C ₂ H ₆ may be included. Biomass gas is used as a raw material for chemical industry such as gas fuel such as diesel power generation, ethanol synthesis, methanol synthesis and FT oil synthesis, for example.

In the pyrolysis gasification process of biomass, biomass is pyrolyzed into solid components such as char, charcoal, and ash, and gas components including tar. The catalytic reforming reaction conditions of the gas component (pyrolysis gas) containing the tar are generally 400 ° C. to 750 ° C., and the contact time is generally 0.1 seconds to 10 seconds. Although the catalyst reforming temperature can be appropriately changed depending on the type of biomass and the pyrolysis gasification temperature, it is preferably 500 ° C. to 650 ° C. under the optimization conditions of the gasification yield and the gasification conversion efficiency. 2 hours to 2 hours.

On the other hand, as described above, the pyrolysis gas component can be converted into reformed gas by reacting with tar in the presence of CO, hydrogen, methane, ethane and water vapor by contacting with the reformed gasification catalyst. The reformed gasification reaction of the tar can be performed under an appropriate catalyst.

In addition, the catalyst includes one or more metal elements selected from nickel, iron, cobalt, platinum, rhodium, molybdenum, zirconia, titanium, cerium, lanthanum, and neodymium and a porous oxide catalyst support. A reforming catalyst can be used. The catalyst can be prepared according to a conventional impregnation method using an acetone solution of the above metal acetylacetonate complex or an aqueous solution of various salts (such as nitrates and hydrochlorides).

Moreover, in reaction with a gaseous component, reaction temperature is 400 to 750 degreeC, From a viewpoint of reactivity and thermal efficiency, Preferably it is 500 to 700 degreeC, More preferably, it is 550 to 650 degreeC.

The reaction vessel for carrying out the present invention is preferably a fixed bed reactor filled with a honeycomb structure catalyst or a pellet structure catalyst, but is not limited thereto. Since the fluidized bed reactor provides a high heat transfer rate and can maintain an isothermal operation, it is very effective in gas production by a combination of a pyrolysis reaction and a reformed gasification reaction.

One embodiment of the biomass pyrolysis gasification furnace of the present invention will be described with reference to FIG.

FIG. 1 is a diagram showing a biomass pyrolysis cassification furnace and a catalyst reforming method according to an embodiment of the present invention. In FIG. 1, reference numeral 20 denotes a pyrolysis gasification furnace main body, which supplies woody biomass from an inlet through a biomass hopper 10, a screw feeder 11 and a conveyor elevator 12. Necessary water is introduced into the holder of the pyrolysis gasification furnace main body 20 from the pipe 13, and the pyrolysis gasification reaction proceeds while being stirred and moved uniformly in an atmosphere of biomass and high-temperature steam by a kiln type rotary system. . During this time, char and bio-coke, which are solids produced, are discharged from the discharge unit 22, while the gas component consisting of pyrolysis gas and tar generated in the pyrolysis gasification reaction is placed in the rear part of the pyrolysis gasification furnace holder. A catalytic reforming gasification reaction of tar or the like is performed using the reforming gasification catalyst 41 filled in the catalyst reforming gasification reactor 40 to be connected.

The catalytic reforming gasification reactor 40 may have a gas inlet 42 in some cases. Thereby, by introducing a gas such as water vapor, the hydrogen / CO molar ratio of the reformed gas generated by selecting the reformed gasification catalyst or controlling the temperature and pressure is 1 or more, usually 2 to 2.5. Can be generated. When the catalytic activity is deteriorated, the reforming catalyst can be regenerated using steam and hydrogen, or steam and air. Thereby, the continuous operation | movement of a pyrolysis gasification furnace can be performed by advancing reforming gasification reaction, such as highly efficient tar, stably.

Next, the process until production from biomass will be described. First, raw material biomass is supplied from the inlet of the pyrolysis gas furnace body 20. The supplied biomass is supplied as it is or once into a highly airtight biomass storage chamber, and then supplied to the pyrolysis gasifier folder by opening or closing a damper or a hatch. In the pyrolysis furnace folder, the biomass is pyrolyzed and gasified by pressurization (0.1 MPa to 0.6 MPa) with a residence time of 0.1 seconds to 10 seconds in a temperature range of 400 ° C. to 850 ° C. In addition, it is more preferable that it is the residence time of 0.2 second-2 second in the temperature range of 500 degreeC-750 degreeC. As a result, biomass generates a solid component composed of char, ash, and the like, and a pressurized gas component composed of gaseous tar and the like. Here, it is important to adjust the temperature so that tar becomes a gas component, but it is usually achieved sufficiently at the internal temperature of the pyrolysis gasifier. Solid components such as char, charcoal and ash are discharged from the discharge unit 22 and stored in the recovery container 23. Char and char are burned in the high temperature combustion furnace 30 and combustion gas of 800 ° C. or higher is supplied to the pyrolysis gasification furnace main body 20 and the external heating holder 21 of the catalytic reforming gasification reactor 40 via a heat exchanger. Thus, the inside of the furnace can be heated to 600 ° C. to 750 ° C.

The gaseous component containing gaseous tar is introduced into the catalytic reforming gasification reactor 40 together with, for example, water vapor in accordance with the flow of gas from the gas inlet 42 or the like.

In the catalytic reforming gasification reactor 40 for tar, a gas component containing tar reacts with water vapor in the presence of the catalyst 41, and in particular, a reforming gasification reaction of a gas component composed of hydrocarbon such as tar proceeds. Generate biomass gas. As described above, it is possible to generate a pressurized reformed gas having a gas composition with an H ₂ / CO ratio of 1 or more with a high gasification yield (50% or more) without reducing the catalytic activity. . The produced biomass gas is purified by the desulfurization / PSA gas regulator 44 and then stored in the gas holder 46. If necessary, biomass gas is input to the generator 50 to generate electric power and heat, and is input to the ethanol synthesis reactor 60 via the booster pump 61, and the gas and liquid separator 62 separates the gas and ethanol. Can be taken out respectively. The separated and extracted gas is supplied as fuel from the pipe 63 to the diesel generator. In addition, ethanol that has been separated and taken out can be purified and used as a fuel. This will supply tri-generation biomass energy consisting of electricity, heat and ethanol fuel.

Next, examples of the present invention will be described below. However, the following examples are merely illustrative of the invention, and the content of the present invention is not limited by the following examples.

  Using a fixed bed reformed gasification reactor filled with a pellet-type reformed gasification catalyst or a honeycomb-type reformed gasification catalyst, cedar pellets in Example 1, bark material in Example 2 and Example 3 as biomass Sugarcane pomace bagasse (25% to 30% moisture content) was introduced into a kiln type rotary gasifier at a feed rate of 100 kg / h to conduct a pyrolysis gasification reaction using high-temperature (650 ° C) steam. . Pressurized biomass gas was obtained by bringing a gas component containing tar into contact with a reformed gasification catalyst charged in a reformed gasification reactor directly connected to a pyrolysis gasification furnace. The test results conducted in Examples 1 to 3 in which performance comparison was made with respect to the gasification conversion efficiency and reformed gas composition of the biomass in the pyrolysis gas furnace in the case of catalytic reforming gasification and in the case of no catalyst are as follows: Show.

Example 1
Pellet-type reforming catalyst A (4% Ni, 0.2% Pt, 2% Fe, 25% CeO ₂ , 3% ZrO ₂ / Al ₂ O ₃ where the metal component is weight% with respect to the support alumina) ring alumina pellets catalyst (19X16mm 10holes, surface area 325 m ² / g) 50L reformed gasification reactor (internal diameter 25 cm, height 150 cm) was packed into a kiln-type rotary gasifier temperature at 650 ° C. The reformed gasification reactor was operated and the reformed gasification reactor internal temperature was controlled at 650 ° C. to perform tar reforming gasification, and a pressurized biomass gas of 0.3 atm was obtained. The concentrations of CO, hydrogen, CO ₂ , CH _4, and hydrocarbons in the outlet biomass gas were measured using a micro gas chromatograph and a Shimadzu FID gas chromatograph filled with gas cropack and molecular sieve 13X. The flow rate of the exhaust gas was measured with a wet gas flow meter. The production rate of the product gas was calculated from the GC analysis of the effluent gas. The gasification conversion rate (% C-conv) was calculated from (CO + CO ₂ + CH ₄ + hydrocarbon production rate) / (total C supply amount of biomass) × 100. C-conv and production rate are average values from 2 hours to 10 hours. The amount of char was determined by measuring the collected weight after stopping the biomass supply. The outlet gas was 148 Nm ³ of reformed gas per hour (50% H ₂ , 23% CO, 6% methane, 1% ethane, 15% CO ₂ ; nitrogen balance). When the reformed gasification catalyst was not used, a reformed gas of 75 Nm ³ per hour was obtained as the outlet gas of the pyrolysis gasifier. Table 1 shows the composition of components such as product gas, tar, and char, and the gasification conversion rate when the reformed gasification catalyst A is used in comparison with the results of pyrolysis gasification without a catalyst. From this result, in the pyrolysis gasification furnace equipped with the catalytic reforming gasification reactor filled with the pellet type reforming catalyst A, by-product methane and tar were reduced and the amount of hydrogen generation was greatly increased. In addition, the H ₂ / CO molar ratio increased from 0.9 without catalyst to 2.2. In addition, the biomass gasification conversion efficiency increases from 47.2% when no catalyst is used to 82.4% when a reforming gasification reactor is provided, and the amount of tar produced is 25% when no catalyst is used. To 2%.

(Example 2)
Pellet type reforming gasification catalyst B (3% Ni, 2% Rh, 30% CeO ₂ , 3% MoO ₃ , 5% TiO ₂ , 1.5% Nd ₂ O ₃ / Al ₂ O ₃ Using a ring-shaped alumina pellet catalyst (19X16mm10holes, surface area 365m ² / g) 50L carrying the weight concentration of alumina), the reformed gasification reaction is performed using the gas components generated in the pyrolysis gasification furnace for bark. went. Reaction conditions and test embodiments are the same as in Example 1. The outlet gas was 135 Nm ³ of reformed gas per hour (48% H ₂ , 20% CO, 6% methane, 1% ethane, 19% CO ₂ ). Table 2 shows the gas component composition and gasification conversion rate of the product gas when the reformed gasification catalyst B is used in comparison with the results of pyrolysis gasification without a catalyst. From this result, in the pyrolysis gasification furnace equipped with the catalytic reforming gasification reactor filled with the pellet type reforming catalyst B, by-product methane and tar were reduced and the amount of hydrogen generation was greatly increased. In addition, the H ₂ / CO molar ratio increased from 0.9 without catalyst to 2.4. In addition, the gasification conversion efficiency of biomass is increased from 45.8% when no catalyst is used to 78.2% when a reforming gasification reactor is provided, and the amount of tar generated is 24% when no catalyst is used. Reduced to 3%.

Example 3
Honeycomb reformed gas catalyst C (8% Ni, 25% CeO 2, 2% Co, 5% La 2 O 3 / Al 2 O 3: wherein a weight% relative to the carrier alumina a metal component) carrying A reformed gasification reaction was carried out using 50 L of honeycomb structure catalyst (20 cm inner diameter X100 cm height cylinder, surface area 125 m ² / g) and using gas components generated by pyrolysis gasification of bagasse, which is the residue of sugarcane. . Reaction conditions and test embodiments are the same as in Example 1. As the outlet gas, 143 Nm ³ of reformed gas (50% H ₂ , 23% CO, 8% methane, 1% ethane, 20% CO ₂ ) was obtained per hour. Table 3 shows the gas component composition and gasification conversion rate of the product gas when the reformed gasification catalyst C is used, compared with the results of pyrolysis gasification without catalyst. From this result, in the pyrolysis gasification furnace equipped with the catalytic reforming gasification reactor filled with the honeycomb-type reforming catalyst C, by-product methane and tar were reduced and the amount of hydrogen generation was greatly increased. Also, the H ₂ / CO molar ratio increased from 0.4 without catalyst to 2.2. In addition, the gasification conversion efficiency of biomass is increased from 53.5% when no catalyst is used to 75.8% when a reforming gasification reactor is provided, and the amount of tar produced is 26% when no catalyst is used. To 2%.

  Hereinafter, the present invention will be described in more detail with reference to the process for producing reformed gasification catalysts A, B and C.

For the production of the reformed gasification catalyst A of Example 1, cerium nitrate (Ce (NO ₃ ) ₃ XH ₂ O), zirconium chloride (ZrCl ₄ ), iron chloride (FeCl ₃ ) and ammonium molybdate ((NH ₄ ) Using an aqueous ethanol solution in which ₂ Mo ₂ O ₇ ) was mixed and dissolved, 1 kg of alumina support (16 × 19 mm Al ₂ O ₃ ) was impregnated and dried at 120 ° C. for 6 hours. Thereafter, a baking treatment was performed at 450 ° C. for 5 hours under an air stream. Further, after impregnating sequentially with an aqueous ethanol solution in which nickel chloride (NiCl ₂ ) and chloroplatinate (H ₂ PtCl ₆ 6H ₂ O) are dissolved, the molded product is 650 ° C at a maximum flow rate of 1 L / min of dry air. For 5 hours. A reformed gasification catalyst with high density and high strength was prepared.

For the production of the reformed gasification catalyst B of Example 2, cerium nitrate (Ce (NO ₃ ) ₃ XH ₂ O), cobalt chloride (CoCl ₂ ), lanthanum chloride (LaCl ₅ XH ₂ O) and nickel chloride (NiCl ₂ ) Using a mixed and dissolved ethanol aqueous solution, a drying treatment was performed at 120 ° C. for 6 hours while impregnating. Thereafter, a baking treatment was performed at 450 ° C. for 5 hours under an air stream. Further, after impregnating successively with an aqueous ethanol solution in which nickel chloride (NiCl ₂ ) and rhodium chloride (RhCl ₃ XH ₂ O) are dissolved, the molded product is fired at a maximum flow of 650 ° C. for 5 hours under a flow rate of 1 L / min of dry air. did. A reformed gasification catalyst pellet having a dense particle aggregate and high strength was prepared.

For the production of the reformed gasification catalyst C of Example 3, cerium nitrate (Ce (NO ₃ ) ₃ XH ₂ O), cobalt chloride (CoCl ₂ ), lanthanum chloride (LaCl ₅ XH ₂ O) and nickel chloride (NiCl ₂₎ ) Was mixed and dissolved in a honeycomb structure catalyst (20 cm inner diameter × 25 cm height cylinder, surface area 125 m ² / g) and simultaneously subjected to a drying treatment at 120 ° C. for 6 hours. Thereafter, a baking treatment was performed at 450 ° C. for 5 hours under an air stream. The molding was fired at a maximum of 650 ° C. for 5 hours under a flow rate of 1 L / min of dry air. The reformed gasification catalyst C (surface area 125 m ² / g) was produced.

  As a result, as in the present invention, by providing a reformed gasification reactor in a biomass pyrolysis gasification furnace, a gas component containing tar generated by pyrolyzing biomass reacts with the reformed gasification catalyst. By suppressing the generation of tar and hydrocarbon components, the gasification conversion efficiency of biomass is improved, and a pyrolysis gasification furnace and catalytic reforming that produce high-energy pyrolysis gas economically and at low cost Clarified that the method.

10 Hopper 11 Screw feeder 12 Biomass supply port (conveyor elevator)
13 Water Supply Pipe 20 Pyrolysis Gasification Furnace Body 21 External Heating Holder 22 Discharge Port 23 Recovery Unit 30 High Temperature Combustion Furnace 31 External Heating Holder 32 Air Supply 33 Heat Exchanger 40 Tar Reforming Gasification Reactor 41 Reforming Gasification catalyst 42 Gas inlet 43 Gas scrubber 44 Desulfurization / PSA gas regulator 45 Fluid pump 46 Biomass gas holder 50 Diesel generator 60 Ethanol synthesis reactor 61 Booster pump 62 Gas-liquid separator 63 Pipe 64 Bioethanol

Claims (5)

A pyrolysis gasification furnace that thermally decomposes biomass into at least a solid component and a gas component by gasification,
A pyrolysis gasification furnace body;
A reforming catalyst reactor connected to the pyrolysis gas gasification furnace main body and gasifying tar in a gas component by a catalytic reforming reaction;
Heating means provided so as to surround the pyrolysis gasification furnace main body and the reforming catalyst reactor, and heating the pyrolysis gasification furnace main body and the interior of the reforming catalyst reactor;
Biomass supply means for supplying biomass into the pyrolysis gasifier body;
Water vapor and oxidant supply means for supplying water vapor and oxidant into the pyrolysis gasifier main body,
The reforming catalyst reactor includes a reformed gasification catalyst comprising nickel, iron, platinum, cerium, and zirconium and a porous oxide catalyst support, nickel, rhodium, molybdenum, titanium, cerium, neodymium, and porous. Reformed gasification catalyst consisting of a porous oxide catalyst support, nickel, cobalt, cerium and lanthanum, and a reformed gasification catalyst consisting of a porous oxide catalyst support filled with any reformed gasification catalyst A pyrolysis gasification furnace characterized by the above.   The heating means uses the combustion gas generated in a high-temperature combustion furnace that burns char and bio-coke, which are solid components generated in the pyrolysis gasification furnace, and the inside of the pyrolysis gas furnace main body and the reforming catalyst reactor. The pyrolysis gasification furnace according to claim 1, wherein:   Reformed gasification catalyst consisting of nickel, iron, platinum, cerium and zirconium and porous oxide catalyst support, consisting of nickel, rhodium, molybdenum, titanium, cerium, neodymium and porous oxide catalyst support A reforming catalyst reactor filled with any reforming gasification catalyst out of a reforming gasification catalyst consisting of a reforming gasification catalyst, nickel, cobalt, cerium and lanthanum and a porous oxide catalyst carrier A catalytic reforming method characterized in that the tar in a gas component is gasified by a catalytic reforming reaction. An ethanol supply system comprising the pyrolysis gasification furnace according to claim 1 or 2,
A gas purification device for cleaning and purifying biomass gas produced in the pyrolysis gasification furnace;
An ethanol supply system comprising an ethanol synthesis catalyst reactor for synthesizing ethanol using purified gas. An electric heat supply system comprising the ethanol supply system according to claim 4,
An electric heat supply system comprising a diesel generator for supplying electric power and heat using a gas obtained by separating a liquid component such as ethanol as a fuel in a gas-liquid separator directly connected to the ethanol synthesis catalyst reactor.