WO2014069840A1

WO2014069840A1 - Dual biomass gasification reactor having nickel distribution plate and biomass gasifier having same

Info

Publication number: WO2014069840A1
Application number: PCT/KR2013/009559
Authority: WO
Inventors: 김주식
Original assignee: 서울시립대학교 산학협력단
Priority date: 2012-10-31
Filing date: 2013-10-25
Publication date: 2014-05-08
Also published as: KR20140055539A; KR101401472B1

Abstract

Disclosed is a dual biomass gasification reactor and a biomass gasifier having the dual biomass gasification reactor, and the reactor comprises: a first reactor which gasifies injected biomass using an external heat source and the oxidation heat source of the biomass, and in which sand or a tar pyrolysis catalyst is filled and moves along with the flow of the external heat source so as to gasify the biomass and to produce bio-char; a second reactor which is provided to communicate with the first reactor so as to use the heat sources of the first reactor and is filled with a carbon adsorbent so as to decrease the content of the tar in the gas produced in the first reactor and to increase hydrogen production for the supply of the gas to a subsequent process; and a distribution plate which is disposed in the communication portion between the first and second reactors so as to prevent the movement of the bio-char and the sand or the tar pyrolysis catalyst in the first reactor towards the second reactor and to prevent the leakage of the carbon adsorbent in the second reactor towards the first reactor, wherein the distribution plate is a nickel plate. When the dual biomass gasification reactor of the present invention and the biomass gasifier having the same are used, gas production from the biomass can be economically and effectively obtained with minimized amounts of tar and ammonia.

Description

Dual biomass gasification reactor with nickel distribution plate and biomass gasifier with the same

The present invention relates to a dual biomass gasification reactor having a nickel distribution plate and a biomass gasification apparatus having the same. More specifically, the present invention relates to a dual biomass gasification reactor having a nickel distribution plate which can minimize tar and ammonia generation and has excellent durability, and a biomass gasification apparatus having the same.

In general, fluidized bed gasifiers have been used in energy conversion and energy recovery processes associated with gasification of coal, sludge or waste polymers, waste wood and waste tires in many chemical processes such as alternative energy development and biomass treatment. There is extensive research on this. Fluidized bed gasifiers have better heat transfer characteristics than fixed bed gasifiers such as up-draft and down-draft gasifiers, and because of the uniform temperature distribution in the reactor, The yield and composition of the producer gas) is constant, and the residence time of the solid reactant in the reactor is long, and the solid has a fluid-like flow, and thus the solid treatment is easy.

The fluidized bed gasifier has been researched and developed in various ways, such as having an internal circulation structure or using a catalyst for high calorific value and yield increase of calorific gas. Among them, a gasifier using an inner circulating fluidized bed is known from South African Patent No. 857,717. The internal circulation fluidized bed gasifier known in this patent is configured to allow internal circulation in the fluidized bed by inserting a draft tube into the fluidized bed to divide the fluidized bed into two parts and injecting fluidized gas velocities at different rates.

Korean Patent Registration No. 208654 discloses an internal circulation fluidized bed gasification reactor having a bottom perforated draft tube, and Korean Patent Registration No. 340594 discloses a gasification method of coal using an internal circulation fluidized bed reactor.

1 is a conceptual diagram showing the configuration of a general fluidized bed gasifier disclosed in the above known art. Referring to FIG. 1, in the case of gasifying biomass using a general fluidized bed gasifier, oxidation, partial oxidation, pyrolysis, and drying occur almost simultaneously during gasification. As can be seen in Table 1 showing the gas characteristics and the tar content according to the type of gasification reactor, it has a smaller tar content in the generated gas than the ascending type gasifier. However, since this tar content is still high for power generation and the like, when tar is produced using gas turbines and gas engines using the generated gas obtained from the conventional fluidized bed gasifier, the gas turbine and gas due to tar are used. There is a problem that process failures such as plugging and fouling problems of the engine are likely to occur.

Table 1

Type of gasifier	Gas component (VOL.% Dry)					High calorific value (MJ / m3)	Gas properties
Type of gasifier	H ₂	CO	CO ₂	CH ₄	N ₂	High calorific value (MJ / m3)	tar	dust
Rising Airflow Type (Air Supply)	11	24	9	3	53	5.5	High (~ 50 g / m3)	that
Downdraft type (air supply)	17	21	13	One	48	5.7	Low (~ 1g / m3)	medium
Fluid type (air supply)	9	14	20	7	50	5.4	Medium (~ 10 g / m3)	Go

In addition to tar, it is important to biomass gasification to minimize the generation of ammonia in the product gas. In particular, minimizing the generation of ammonia should be considered particularly important in the gasification of sewage sludge containing a lot of nitrogen.

Accordingly, one object of the present invention is to provide a dual biomass gasification reactor in which tar and ammonia generation can be minimized in order to solve the problems of the prior art.

Another object of the present invention is to provide a gasification apparatus for producing a high calorific value gas having a low tar and ammonia content by using the dual biomass gasification reactor stably used for power generation.

One aspect of the present invention to achieve the above object

A first reactor for gasifying the injected biomass using an external heat source and an oxidizing heat source of the biomass itself, wherein the biomass is filled with sand or tar decomposition catalyst and flows along the air stream of the external heat source. A first reactor for gasifying and generating bio-char;

It is installed to communicate with the first reactor and uses the heat source of the first reactor and the carbon adsorbent is filled therein to reduce the content of tar in the generated gas produced in the first reactor and increase hydrogen production to a subsequent process A second reactor for supplying; And

A distribution plate provided at a communication site between the first and second reactors, the distribution plate prevents flow of the biochar and the sand or tar decomposition catalyst toward the second reactor in the first reactor, and the carbon in the second reactor. A distribution plate for preventing the outflow of the adsorbent to the first reactor,

The distribution plate provides a dual biomass gasification reactor, characterized in that the nickel plate.

In one embodiment of the invention, the second reactor is fixed to the inner top of the first reactor so as to be located in the upper side in the interior of the first reactor, with a gap from the inner circumference of the first reactor It may be fixed spaced apart.

In another embodiment of the present invention, the second reactor may be installed on the top of the first reactor to form a two-stage configuration.

In one embodiment of the present invention, the distribution plate is preferably a nickel plate plated on an iron-based metal plate.

In one embodiment of the present invention, the distribution plate may have a shape of a porous plate having a plurality of holes.

In another embodiment of the present invention, a hook-shaped pipe may protrude toward the second reactor 220a at the upper end of each hole of the distribution plate.

The distribution plate may be attached to the hook (hook) bent a plurality of top.

In one embodiment of the present invention, the carbon adsorbent may be activated carbon or biochar.

In one embodiment of the present invention, the first reactor comprises: a first pipe installed in communication with the interior of the first reactor for discharging excess biochar to the outside such that the biochar inside maintains a constant amount; And

The storage unit may further include an accommodation unit configured to store the surplus biochar discharged by gravity along the first pipe.

In one embodiment of the present invention, the second reactor may be further provided with a cyclone to discharge the generated gas of reduced tar content in a subsequent process and prevent the outflow of the carbon adsorbent charged therein. .

In one embodiment of the present invention, further comprising a second pipe for communicating the first and second reactors with each other to flow surplus carbon adsorbent toward the first reactor so that the carbon adsorbent in the second reactor maintains a certain amount. It can be provided.

Another aspect of the present invention to achieve the above another object,

Biomass injection means for injecting biomass;

Dual biomass gasification reactor according to an aspect of the present invention for gasifying the biomass injected through the biomass injection means using an external heat source and the heat source of the biomass itself;

Heat source supply means for supplying preheated air to the gasification reactor; And

It provides a biomass gasification apparatus comprising a purifying means for purifying the exhaust gas discharged from the gasification reactor.

By using the dual biomass gasification reactor of the present invention and a biomass gasification apparatus including the same, it is possible to economically and efficiently obtain a product gas with minimal tar and ammonia content from the biomass.

1 is a conceptual diagram of a general fluidized bed gasifier.

2 is a conceptual diagram of a gasifier having a dual biomass gasification reactor according to a first embodiment of the present invention.

3 is a detailed view of the dual biomass gasification reactor shown in FIG. 2.

4 is a conceptual diagram of a gasifier having a dual biomass gasification reactor according to a second embodiment of the present invention.

5 is a conceptual diagram of a gasifier applied to the experimental example of the present invention.

Hereinafter, with reference to the accompanying drawings will be described in detail with respect to specific embodiments of a dual biomass gasification reactor having a nickel distribution plate and a gasification apparatus having the same according to the present invention. The following description is provided for illustrative purposes so that the present invention may be readily reproduced, and needless to say, it does not limit the scope of the present invention.

First embodiment

FIG. 2 is a conceptual diagram of a gasification apparatus having a dual biomass gasification reactor according to a first embodiment of the present invention, and FIG. 3 is a detailed view of the dual biomass gasification reactor shown in FIG.

Referring to FIG. 2, the gasification apparatus of the present embodiment includes a biomass injection means 10 for injecting biomass such as sewage sludge and waste wood, and a biomass injected through the biomass injection means 10. A dual biomass gasification reactor 20 to gasify using a heat source and a heat source of the biomass itself, and to reduce the content of tar and ammonia by adsorption or cracking of tar and ammonia in the generated product gas, and a gasification reactor A heat source supply means 30 for supplying preheated air as an oxidant to the 20 and also supplying steam as needed, and refining means for purifying the exhaust gas discharged from the gasification reactor 20 to be used for power production or the like. It consists of

The biomass injection means 10 is a pulverized biomass such as sewage sludge or waste wood to be injected into a predetermined size and is composed of a general configuration relationship used in the gasifier.

2 and 3, the gasification reactor 20 includes a first reactor 210 having a volume of a predetermined size, and a second reactor 220 installed inside the first reactor 210.

The first reactor 210 serves to generate a gas by gasifying the biomass using the preliminary heat source, air and water vapor supplied from the heat source supply means 30, and the heat content of the biomass itself. The first reactor 210 is filled with a predetermined amount of sand or tar decomposition catalyst therein, and is configured to receive the preheated air and steam from the heat source supply means 30 to one side. Here, the sand or tar decomposition catalyst serves to facilitate the gasification of the biomass while flowing along the air stream of the air and water vapor supplied from the heat source supply means (30). That is, the first reactor 210 undergoes typical biomass gasification as a fluidized bed reactor and produces bio-char as a gasification byproduct during the process.

The first reactor 210 is configured such that the surplus biochar flows along the first pipe 211 and is stored in the accommodating part 212 so that the biochar generated during the process maintains a constant amount at all times so as not to burden the process. That is, one end of the first pipe 211 is configured to communicate with the inside at a predetermined height of the first reactor 210. At this time, the first pipe 211 has a bent shape so as not to be disturbed by upflow. Therefore, the surplus biochar is stored in the accommodating portion 212 by gravity along the first pipe 211 and not the mechanical device, so that it does not burden the process.

The second reactor 220 is fixed to the inner top of the first reactor 210 to be installed on the upper side of the inside of the first reactor 210. Therefore, the second reactor 220 uses the heat source of the first reactor 210 as it is. The second reactor 220 is installed at a predetermined distance from the inner circumference of the first reactor 210, except for the lower portion has a structure that is closed with the first reactor 210. That is, the second reactor 220 has a distribution plate 221 communicating with the first reactor 210 at the bottom thereof.

Here, the distribution plate 221 flows smoothly through the product gas generated in the first reactor 210 flows in the upward air flow, but a plurality of micrometer-sized holes, for example, a plurality of holes so that biochar does not pass through. It has the shape of a perforated plate having a hole of. In addition, the hole of the distribution plate 221 has a size that the carbon adsorbent filled in the second reactor 220 does not flow out to the lower first reactor 210. This distribution plate 221 is a nickel plate having a plurality of holes. In terms of economy, the distribution plate 221 is a nickel plate plated on an iron metal plate. For example, the distribution plate 221 is a nickel plate plated on a stainless steel plate. The nickel distribution plate partitioning the first reactor and the second reactor can simultaneously undergo tar reduction and ammonia decomposition. That is, the nickel distribution plate decomposes the tar generated in the first reactor 210 by reducing the tar content in the product gas by decomposing the tar generated in the first reactor 210 and the ammonia generated in the first reactor 210 according to the reaction scheme shown below. Thereby exhibiting an ammonia decomposition catalytic action that reduces the ammonia content in the product gas, thereby reducing the content of tar and ammonia in the gas obtained from the biomass.

i) Tar cracking catalysis: C _n H _x (tar) → C _m H _y (small molecule tar or light hydrocarbon) + H ₂

ii) Catalytic decomposition of ammonia: 2NH ₃ → N ₂ + 3H ₂ .

Reaction ii) is a reverse reaction of ammonia synthesis from hydrogen gas and nitrogen gas. Nickel distribution plates are important in the gasification of sewage sludge containing a lot of nitrogen, especially since they can dramatically reduce the content of ammonia. As described above, the use of the nickel distribution plate disclosed in the present invention can reduce nickel loss and nickel deactivation phenomena as compared to a configuration using a nickel catalyst particle layer inside a fluidized bed reactor or a configuration using a separate fixed bed nickel catalyst tower outside the reactor. There are advantages to it. That is, the nickel distribution plate 221 can prevent the loss of the nickel catalyst accompanying the swept away by the fluid (fluid medium) flow in the fluidized bed when adopting a configuration using a nickel catalyst particle layer in the fluidized bed reactor. For this reason, in this case, a second fixed bed nickel catalyst tower may be additionally installed to solve the energy problem of operating. When using the nickel distribution plate according to the present invention is because the energy required for tar decomposition by nickel can utilize the energy generated by oxidation in the fluidized bed reactor. In addition, when using the nickel distribution plate according to the present invention has the advantage that the deactivation (deactivation) of the nickel generated by the coke is deposited on the nickel distribution plate is reduced. In general, the nickel catalyst is rapidly deactivated by sulfur, tar, etc., and when the biomass such as wood with low sulfur content and polyolefin waste plastics are gasified, the main deactivation route is generation of coke due to tar deposition. In the gasifier according to the present invention, deactivation may be drastically reduced since continuous collision with the nickel distribution plate occurs due to active movement of fluidized bed materials such as sand and / or tar decomposition catalysts, and the coke is separated. It is also possible to continuously oxidize the carbon deposits formed in the nickel distribution plate by air which is often supplied to the first reactor, so that coke deposition can be further reduced. In addition, CO ₂ and H ₂ O generated from the first gasification reactor may react with coke (C) deposited on the nickel distribution plate to cause coke decomposition.

i) Reaction of coke with CO ₂ : C (coke) + CO ₂ → 2CO

ii) Reaction of coke with H ₂ O: C (coke) + H ₂ O → CO + H ₂

Therefore, by using the dual biomass gasification reactor of the present invention and a biomass gasification apparatus having the same, it is possible to obtain a product gas with minimal tar and ammonia content from the biomass economically and efficiently.

The second reactor 220 serves to reduce the content of tar by adsorbing or cracking tar in the generated gas generated in the first reactor 210, and a predetermined amount of carbon adsorbent (activated carbon) is contained therein. And / or biochar). Here, the carbon adsorbent serves to catalyze the tar in the product gas to reduce the content of tar or promote the decomposition of tar, thereby reducing the content and promoting the reaction with moisture in the product gas, thereby helping to produce hydrogen. do.

In addition, a cyclone 222 is installed inside the second reactor 220 to prevent the outflow of the carbon adsorbent charged therein and to supply the product gas having a reduced tar content to the purifying means 40. The cyclone 222 preferably has a structure in which its lower end is bent so as not to be disturbed by upflow. In addition, in the second reactor 220, the excess carbon adsorbent flows along the second pipe 223 toward the first reactor 210 so as not to impede the process by maintaining a constant amount of the carbon adsorbent charged therein at all times. It is configured to be stored in the receiving portion (212). That is, one end of the second pipe 211 is in communication with the inside at a certain height of the second reactor 220, the other end is configured to communicate with the inside at a certain height of the first reactor (210). In this case, the second pipe 223 has a bent shape so as not to be disturbed by upflow.

The dual biomass gasification reactor 20 having the above configuration has a predetermined amount of carbon adsorbent inside the second reactor 220 to adsorb tar in the product gas to reduce the content of tar or promote tar decomposition. It acts as a catalyst to reduce the content and promotes the reaction with moisture in the generated gas to help the production of hydrogen to produce a high calorific value gas.

In addition, the dual biomass gasification reactor 20 can reduce the amount of particles contained in the product gas through the following components. That is, the surplus biochar in the first reactor 210 is discharged to the receiving portion 212 through the first first pipe 211, and the first reactor (through the distribution plate 221 of the second reactor 220). The biochar in the product gas generated in 210 to be flowed into the second reactor 220 along the rising air flow is filtered, and the third cyclone 222 prevents the outflow of the carbon adsorbent inside the second reactor 220. For example, the amount of particles included in the generated gas may be reduced by discharging the excess carbon adsorbent in the second reactor 210 through the second pipe 223 to the accommodation portion 212 through the first reactor 210.

The heat source supply means 30 serves to supply a preliminary heat source and air to the first reactor 210 and also to supply water vapor as necessary, and is configured in a general configuration relationship used in a fluidized bed gasifier.

The purifying means 40 serves to purify the exhaust gas discharged from the second reactor 220 to be used for electric power production, etc., and is configured in a general configuration relationship used in the fluidized bed gasifier.

2nd Embodiment

The gasifier according to the second embodiment of the present invention has the same concept as the gasifier of the first embodiment except for the partial structure of the reactor. Therefore, the same or similar components as those in the first embodiment will be denoted by the same reference numerals and the description thereof will be omitted.

4 is a conceptual diagram of a gasifier having a dual biomass gasification reactor containing a carbon adsorbent according to a second embodiment of the present invention. Referring to FIG. 4, the dual biomass gasification reactor 20a according to the present embodiment includes a biomass injected through the biomass injection means 10a and an external heat source supplied from the heat source supply means 30a and the biomass itself. It comprises a first reactor (210a) for gasification using a heat source, and a second reactor (220a) to reduce the content of tar by adsorption or decomposition of the tar in the product gas generated in the first reactor (210a). Here, the second reactor 220a has a wider size and volume than the first reactor 210a and is installed directly above the first reactor 210a. Therefore, the first and

second reactors

210a and 220a form two stages up and down, and the connection portion has a tapered shape.

The first reactor 210a is filled with a certain amount of sand therein, and the surplus biochar generated during the process is stored in the receiving portion 212a along the first pipe 211a. 1 is configured to serve the same function as the reactor (210).

In addition, the second reactor 220a is filled with a predetermined amount of carbon adsorbent (activated carbon and / or biochar) therein, and a nickel distribution plate 221a communicating with the first reactor 210a at the lower portion thereof, and carbon Cyclone 222a for supplying the generated gas having reduced tar content to the refining means 40a as well as preventing the outflow of the adsorbent, and a second pipe 223a connecting the first and

second reactors

210a and 220a. It is configured to serve the same function as the second reactor 220 of the first embodiment, and the like. Here, the nickel distribution plate 221a may be configured in a form in which a hook-shaped pipe protrudes toward the second reactor 220a at the upper end of each hole, unlike the nickel distribution plate 221 of the first embodiment. have.

Part of the tar in the product gas generated in the first reactor 210a and flowing to the second reactor 220a by supplying air from the heat source supply means 30a to the connection portions of the first and

second reactors

210a and 220a. By removing the air supply line 310a to reduce the tar content in the product gas is installed in communication with the heat source supply means (30a). Thus, by supplying air to oxidize the tar in the product gas can be reduced its content.

As described above, the dual biomass gasification reactor of the present invention and the biomass gasification apparatus including the same can produce a product gas that minimizes the tar and ammonia content from the biomass by economically and efficiently adopting a nickel distribution plate.

In addition, the dual biomass gasification reactor of the present invention and the biomass gasification apparatus having the same has a separate internal reactor or two stages of the reactor inside, but by containing a carbon adsorbent in the upper reactor content of tar in the generated gas It can reduce and generate high calorific value gas and can be designed to have a medium-sized power generation capacity. This overcomes the limitation that existing fixed bed gasifiers can only be used in small power generation systems.

The dual biomass gasification reactor of the present invention and the biomass gasification apparatus including the same can also produce a high calorific value gas having a low content of tar and ammonia that can be stably used for electric power production and the like by providing a dual biomass gasification reactor.

The dual biomass gasification reactor of the present invention and the biomass gasification apparatus including the same also have a small installation space because the reactor can be dually configured so that the heat source of the lower reactor (first reactor) can be used as it is in the upper reactor (second reactor). The efficiency of the process can be increased.

Experimental Example

Hereinafter, an experimental example of the biomass gasifier according to the present invention configured as described above will be described.

The feedstock used in this experiment was 1kg of dry sewage sludge of 250 ~ 425㎛ size as biomass and 500g of activated carbon as carbon adsorbent.

And, the gasifier is configured as shown in Figure 5, using a two-stage gasification reactor made of STS-316. Here, the lower reactor had a size of 100 mm in diameter and 360 mm in height, and was filled with silica sand therein. In addition, three thermocouples were installed in the bottom reactor for flow stability testing. The upper reactor was 160 mm in diameter and 340 mm in height and filled with activated carbon therein. In addition, two thermocouples were installed in the upper reactor for flow stability testing.

Cyclone filtered the particle | grains of 10 micrometers or more, the hot filter used the product of the specification which filters the particle | grains of 1 micrometer or more, and the condenser cooled the condensate liquid to 0 degreeC. The generated gases were analyzed using GCs and GC-MS systems.

TABLE 2

	Comparative Example 1	Comparative Example 2	Example 1
Experimental conditions
Upper reactor temperature (℃)	807	800	793
Bottom reactor temperature (° C)	812	779	794
Driving time (min)	91	93	93
Equivalence ratio *	0.20	0.21	0.20
Bed material (g)	Natural Olivine 2500g	Natural Olivine 2500g	Natural Olivine 2500g
G of activated carbon in the upper reactor (g)	Do not use	2,000 g	2,000 g
Distribution plate material	Stainless steel distribution plate	Stainless Steel Distribution Plate	Nickel plated plate on stainless steel plate
Product gas characteristics
N ₂ (vol.%)	46.81	44.22	38.85
CO ₂ (vol.%)	16.73	7.65	13.26
H ₂ (vol.%)	9.97	29.19	26.46
CO (vol.%)	14.26	14.94	17.23
CH ₄ (vol.%)	8.04	4.00	4.19
C ₂ H ₂ (vol.%)	0.20	0.0000	0.0053
C ₂ H ₄ (vol.%)	3.16	0.0020	0.0010
C ₂ H ₆ (vol.%)	0.19	0.0008	0.0009
C ₃ + C ₄ + C ₅ (vol.%)	0.10	0.0034	<0.0001
Benzene (vol.%)	0.49	0.0051	0.0002
Aromatic compounds heavier than benzene (vol.%)	0.06	0.0015	0.0003
Tar (g / Nm ³ )	2.41	0.06	0.0098
Low calorific value (MJ / Nm ³ )	8.36	6.18	6.28
Ammonia Content (mg / L)	Not measured	700	11.7

* Equivalence ratio represents the amount of air that is chemically equivalent to the actual amount of air supplied during gasification / complete oxidation.

Referring to Table 2, Example 1 using the nickel-plated stainless distribution plate produced gas compared to Comparative Example 2 (0.06 g / Nm ³ ) tested under the same conditions except that a stainless distribution plate instead of a nickel distribution plate It can be seen that the tar content (about 0.01 g / Nm ³ ) is reduced by about 6 times or more. The ammonia content (about 12 mg / L) of the product gas obtained in Example 1 was confirmed to be reduced by about 58.3 times compared to Comparative Example 2 (700 mg / L). In addition, the deactivation of the nickel distribution plate of Example 1 was not observed when the change of the product gas component was observed under the above experimental conditions.

Therefore, in the case of Comparative Example 1 using a stainless distribution plate as in Comparative Example 2 but not filled with activated carbon in the upper reactor (second reactor) it was confirmed that the tar content is more. Ammonia content of Comparative Example 1 was not measured, but considering the properties of activated carbon with ammonia adsorption, it is determined that it is 700 mg / L or more.

Those skilled in the art will recognize that various modifications and variations can be made within the scope of the appended claims without departing from the scope of the spirit of the invention.

10: biomass injection means

20: gasification reactor

30: heat source supply means

40: refining means

210: first reactor

211: first pipe

212: accommodation

220: second reactor

221: Distribution Plate

222: cyclone

223: second pipe.

Claims

A first reactor for gasifying the injected biomass using an external heat source and an oxidizing heat source of the biomass itself, wherein the biomass is filled with sand or tar decomposition catalyst and flows along the air stream of the external heat source. Reactor to gasify and generate bio-char

It is installed to communicate with the first reactor and uses the heat source of the first reactor and the carbon adsorbent is filled therein to reduce the content of tar in the generated gas produced in the first reactor and increase hydrogen production to a subsequent process A second reactor for supplying; And

A distribution plate provided at a communication site between the first and second reactors, the distribution plate prevents flow of the biochar and the sand or tar decomposition catalyst toward the second reactor in the first reactor, and the carbon in the second reactor. A distribution plate for preventing the outflow of the adsorbent to the first reactor,

The distribution plate is a dual biomass gasification reactor, characterized in that the nickel plate.
The method of claim 1, wherein the second reactor is fixed to the inner top of the first reactor so as to be located in the upper side in the interior of the first reactor, spaced apart from the inner circumference of the first reactor Dual biomass gasification reactor, characterized in that fixed to.
The dual biomass gasification reactor of claim 1, wherein the second reactor is installed on the top of the first reactor to form a two-stage configuration.
The dual biomass gasification reactor according to claim 1, wherein the distribution plate is a nickel plate plated on an iron-based metal plate.
The dual biomass gasification reactor according to claim 1, wherein the distribution plate has a shape of a porous plate having a plurality of holes.
6. The dual biomass gasification reactor according to claim 5, wherein a hook-shaped pipe protrudes toward the second reactor (220a) at the upper end of each hole of the distribution plate.
The dual biomass gasification reactor of claim 1, wherein the carbon adsorbent is activated carbon or biochar.
According to claim 1, wherein the first reactor has a first pipe installed in communication with the interior of the first reactor for discharging the surplus biochar to the outside to maintain a certain amount of the biochar therein; And

And a receptacle for storing the surplus biochar discharged by gravity along the first pipe.
The method of claim 1, wherein the second reactor is further provided with a cyclone for discharging the product gas of reduced tar content in a subsequent process and preventing the outflow of the carbon adsorbent charged therein. Biomass gasification reactor.
The method of claim 1, further comprising a second pipe communicating the first and second reactors with each other to flow a surplus carbon adsorbent toward the first reactor to maintain a constant amount of the carbon adsorbent in the second reactor. Dual biomass gasification reactor characterized in that.
Biomass injection means for injecting biomass;

The dual biomass gasification reactor according to any one of claims 1 to 10, wherein the biomass injected through the biomass injection means is gasified using an external heat source and a heat source of the biomass itself;

Heat source supply means for supplying preheated air to the gasification reactor; And

Biomass gasification apparatus comprising a purifying means for purifying the exhaust gas discharged from the gasification reactor.