KR101401472B1 - Two-stage biomass gasifier having nickel distributor plate and biomass gasifier apparatus having the same - Google Patents

Abstract

A first reactor for gasifying the injected biomass using an external heat source and an oxidizing heat source of the biomass itself, wherein a sand or tar decomposition catalyst is filled therein and flows along the air stream of the external heat source, A first reactor for gasifying and producing a bio-char; The first reactor is connected to the first reactor and uses the heat source of the first reactor. The carbon adsorbent is filled in the first reactor, thereby reducing the content of tar in the product gas generated in the first reactor and increasing the production of hydrogen. A second reactor for supplying the reactants; And a distribution plate disposed in a communicating portion between the first and second reactors, wherein the distribution plate shields the flow of the bichar and the sand or tar decomposition catalyst in the first reactor toward the second reactor, A dual biomass gasification reactor and a biomass gasification apparatus comprising the gasification reactor are disclosed, wherein the dual biomass gasification reactor comprises a distribution plate for preventing the carbon adsorbent from flowing out toward the first reactor, and the distribution plate is a nickel plate. Using the dual biomass gasification reactor of the present invention and the biomass gasification apparatus having the dual biomass gasification reactor, it is possible to economically and efficiently produce the product gas from which the tar and ammonia contents are minimized from the biomass.

Description

TECHNICAL FIELD The present invention relates to a dual-biomass gasification reactor having a nickel distribution plate and a biomass gasifier having the nickel distribution plate,

The present invention relates to a dual biomass gasification reactor having a nickel distribution plate and a biomass gasification apparatus having the biomass gasification reactor. More particularly, the present invention relates to a dual biomass gasification reactor having a nickel distribution plate that can minimize the generation of tar and ammonia and is excellent in durability, and a biomass gasification apparatus having the dual biomass gasification reactor.

Generally, fluidized bed gasification apparatuses have been used in energy conversion processes and energy recovery processes related to gasification of coal, sludge or waste polymers, waste wood and waste tires in various chemical processing fields such as alternative energy development and biomass treatment, Extensive research is underway. The fluidized bed gasifier has superior heat transfer characteristics compared to the fixed bed gasifier such as an up-draft gasifier and a down-draft gasifier, and because of the uniform temperature distribution in the reactor, producer gas has a constant yield and composition, has a long residence time in the reactor of the solid reactant, and has a flow such as a solid, which facilitates solid processing.

Since the fluidized bed gasifier has a primary purpose of obtaining the calorific gas generated by treating the solid, it has been developed in various ways such as having an internal circulation structure or using a catalyst for increasing the calorific value of the calorific gas and increasing the yield. Among them, a gasification apparatus using an internal circulating fluidized bed is known from South Africa Patent No. 857,717. The internal circulating fluidized bed gasification apparatus disclosed in this patent is configured to allow internal circulation in the fluidized bed by inserting a draft tube into the fluidized bed, dividing the fluidized bed into two parts, and injecting them at different fluidizing gas velocities.

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

FIG. 1 is a conceptual diagram showing the construction of a general fluidized bed gasification apparatus disclosed in the above-mentioned prior art. 1, oxidation, partial oxidation, pyrolysis, and drying of the biomass and the like occur almost simultaneously during the gasification of the biomass using a general fluidized bed gasification apparatus, As can be seen from Table 1, which shows the gas characteristics and the tar content according to the types of the gasification reactors, it has a smaller content of tar in the product gas than in the upflow gasification type gasifier. However, since this amount of tar is still a high value for use in electric power generation and the like, when producing gas using the gas turbine and the gas engine using the gas obtained from the conventional fluidized bed gasification apparatus, the gas turbine and gas There is a problem that process failures such as plugging and fouling of the engine are likely to occur.

Types of Gasification Apparatus
Gas composition (VOL.% Drying) eminence
Calorific value
(MJ / m3) Gas characteristic H ₂ CO CO ₂ CH ₄ N ₂ tar dust Upflow type (air supply) 11 24 9 3 53 5.5 High (~ 50g / m3) that Downflow type (air supply) 17 21 13 One 48 5.7 Low (~ 1g / m3) medium Flow type (air supply) 9 14 20 7 50 5.4 (~ 10g / m3) The

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

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

It is another object of the present invention to provide a gasification apparatus which can stably utilize the dual biomass gasification reactor and produce gas with a high heating amount with low tar and ammonia content.

According to an aspect of the present invention,

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

The first reactor is connected to the first reactor and uses the heat source of the first reactor. The carbon adsorbent is filled in the first reactor, thereby reducing the content of tar in the product gas generated in the first reactor and increasing the production of hydrogen. A second reactor for supplying the reactants; And

A distribution plate disposed in a communicating portion between the first and second reactors to prevent the flow of the bichar and the sand or tar decomposition catalyst in the first reactor toward the second reactor, A distribution plate for preventing the adsorbent from flowing out toward the first reactor,

Wherein the distribution plate is a nickel plate. The present invention also provides a dual biomass gasification reactor.

In one embodiment of the present invention, the second reactor is fixed to the upper side of the inner side of the first reactor so as to be located on the upper side inside the first reactor, and is spaced apart from the inner periphery of the first reactor And may be fixed and spaced apart.

In another embodiment of the present invention, the second reactor may be installed at the upper end of the first reactor to form a two-stage reactor.

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

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

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

The distribution plate may be provided with a plurality of hooks bent at the upper end thereof.

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 includes a first pipe communicating with the interior of the first reactor to discharge surplus biochar to the outside so that the biochar in the bioreactor is maintained at a predetermined amount; And

And a receiver for storing the surplus biochar discharged by gravity along the first pipe.

In an embodiment of the present invention, a cyclone may be further provided in the second reactor to discharge the generated gas in which the content of tar is reduced in a subsequent process, and to prevent the carbon adsorbent charged therein from flowing out .

In an embodiment of the present invention, a second pipe communicating the first and second reactors to flow the excess carbon adsorbent toward the first reactor so that the carbon adsorbent inside the second reactor maintains a predetermined amount .

According to another aspect of the present invention,

Biomass injection means for injecting biomass;

A dual biomass gasification reactor according to one aspect of the present invention for gasifying biomass injected through the biomass injecting means using an external heat source and a heat source of the biomass itself;

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

And a purification means for purifying the exhaust gas discharged from the gasification reactor.

Using the dual biomass gasification reactor of the present invention and the biomass gasification apparatus having the dual biomass gasification reactor, it is possible to economically and efficiently produce the product gas from which the tar and ammonia contents are minimized from the biomass.

1 is a conceptual diagram of a general fluidized bed gasification apparatus.
2 is a conceptual diagram of a gasification apparatus having a dual biomass gasification reactor according to a first embodiment of the present invention.
FIG. 3 is a detailed view of the dual biomass gasification reactor shown in FIG. 2. FIG.
4 is a conceptual diagram of a gasification apparatus having a dual biomass gasification reactor according to a second embodiment of the present invention.
5 is a conceptual diagram of a gasification apparatus applied to an experimental example of the present invention.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, a dual biomass gasification reactor having a nickel distribution plate according to the present invention and a gasification apparatus having the same will be described in detail with reference to the accompanying drawings. It is needless to say that the following description is provided for the illustrative purpose of easily reproducing the present invention and does not limit the scope of the present invention in any way.

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.

2, the gasification apparatus of the present embodiment includes a biomass injection means 10 for injecting biomass such as sewage sludge and waste wood, a biomass injection means 10 for supplying the biomass injected through the biomass injection means 10 to the outside A dual biomass gasification reactor 20 for gasifying using a heat source and a heat source of the biomass itself and adsorbing or cracking tar and ammonia in the produced gas to reduce the content of tar and ammonia, (30) for supplying air preheated as an oxidizing agent to the gasification reactor (20) and supplying steam as necessary, and purification means (40) for purifying the exhaust gas discharged from the gasification reactor (20) ).

The biomass injecting means 10 is formed by pulverizing and injecting biomass such as sewage sludge and waste wood into a predetermined size and has a general constitutional relationship used in a gasification apparatus.

Referring to FIGS. 2 and 3, the gasification reactor 20 includes a first reactor 210 having a predetermined volume and a second reactor 220 installed in the first reactor 210.

The first reactor 210 serves to generate the gas by gasifying the biomass using the heat source, the air, and the steam, which are 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, and is supplied with the preheated air and steam from the heat source supply means 30 to one side. Here, the sand or tar decomposition catalyst functions to smoothly gasify the biomass while flowing along the air stream of steam and steam supplied from the heat source supply means 30. That is, the first reactor 210 is a fluidized bed reactor, which typically produces biomass gasification and produces bio-char as a by-product of gasification during the process.

The first reactor 210 is configured so that the surplus biocharging flows along the first pipe 211 and is stored in the accommodating portion 212 so that the biochar produced during the process is always maintained at a constant amount, That is, one end of the first pipe 211 is configured to communicate with the inside of the first reactor 210 at a predetermined height. At this time, the first pipe 211 is curved so as not to be disturbed by the upward flow. Therefore, the surplus biochar is stored in the accommodating portion 212 by the gravity along the first pipe 211, not the mechanical device, so that the process is not troublesome.

The second reactor 220 is fixed to the inner upper end of the first reactor 210 so as to be installed on the upper side of the interior of the first reactor 210. Accordingly, 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 interval from the inner circumference of the first reactor 210 and has a structure closed with the first reactor 210 except for the lower portion thereof. That is, the second reactor 220 has a distribution plate 221 communicating with the first reactor 210 at a lower portion thereof.

In this case, the distribution plate 221 is formed such that the product gas generated in the first reactor 210 flows along the ascending airflow to smoothly pass therethrough, but a plurality of micrometer-sized holes, for example, a plurality of And has a shape of a perforated plate having a hole of a hole. Further, the holes of the distribution plate 221 have such a size that the carbon adsorbent charged in the second reactor 220 can not flow out to the lower first reactor 210. This distribution plate 221 is a nickel plate having a plurality of holes. From an economic point of view, the distribution plate 221 is a nickel-plated nickel plate. For example, the distribution plate 221 is a nickel plate plated on a stainless steel plate. The nickel distribution plate separating the first reactor and the second reactor can simultaneously perform tar reduction and ammonia decomposition. That is, the nickel distribution plate decomposes the tar produced in the first reactor 210 according to the reaction formula shown below to reduce the tar content in the generated gas, and decomposes the ammonia generated in the first reactor 210 Thereby reducing the content of tar and ammonia in the gas obtained from the biomass by exhibiting the ammonia decomposition catalytic action of reducing the ammonia content in the produced gas.

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

ii) Ammonia decomposition catalysis: 2NH ₃ → N ₂ + 3H ₂ .

Reaction ii) is the reverse reaction of the reaction of ammonia with hydrogen gas and nitrogen gas. Nickel distribution plates are important because they can dramatically reduce the ammonia content, especially in the gasification of sewage sludge containing a large amount of nitrogen. As described above, the use of the nickel distribution plate according to the present invention reduces the loss of nickel and the deactivation of nickel compared to a configuration using a nickel catalyst particle layer inside a fluidized bed reactor or using a separate fixed bed nickel catalyst tower outside the reactor There are advantages to be able to. That is, the nickel distribution plate 221 can prevent the loss of the nickel catalyst which is entrained in the fluid (fluid medium) flow in the fluidized bed when adopting a configuration using a nickel catalyst particle layer inside the fluidized bed reactor For this reason, in this case, it is possible to solve the energy problem which is required to install and operate the second fixed bed nickel catalyst tower. In the case of using the nickel distribution plate according to the present invention, the energy required for the decomposition of the tar by the nickel can utilize the energy generated by the oxidation in the fluidized bed reactor. Also, in the case of using the nickel distribution plate according to the present invention, there is an advantage that the deactivation of nickel generated by deposition of coke on the nickel distribution plate is reduced. In general nickel catalysts are inactivated rapidly by sulfur, tar and the like. When biomass such as wood having low sulfur content, polyolefin waste plastic, etc. is gasified, the main deactivation route is generation of coke due to tar deposition. In the gasification apparatus according to the present invention, the active movement of the fluidized bed material such as the sand and / or the tar decomposition catalyst causes the continuous collision with the nickel distribution plate and the detachment of the coke is progressed, so that the inactivation can be drastically reduced. In addition, the carbon deposit formed on the nickel distribution plate can be continuously oxidized by the air supplied from time to time to the first reactor, so that the coke deposition can be further reduced. Also, CO ₂ and H ₂ O generated from the first gasification reactor may react with the coke (C) deposited on the nickel distribution plate to cause a coke decomposition reaction.

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 the biomass gasification apparatus having the dual biomass gasification reactor, it is possible to economically and efficiently produce the product gas in which the tar and ammonia contents are minimized from the biomass.

The second reactor 220 adsorbs or cracks the tar in the product gas generated in the first reactor 210 to reduce the content of tar. In the second reactor 220, a certain amount of carbon adsorbent And / or biochar). In this case, the carbon adsorbent serves to reduce the content of tar in the product gas and to accelerate the decomposition of tar, thereby not only reducing the content of the tar but also promoting the reaction with moisture in the product gas, do.

In addition, a cyclone 222 is installed inside the second reactor 220 to prevent the carbon adsorbent from leaking out of the second reactor 220 and to supply a product gas having reduced tar content to the refining means 40. The cyclone 222 preferably has a structure in which the lower end thereof is bent so as not to be disturbed by upward flow. Also, the excess carbon adsorbent flows toward the first reactor 210 along the second pipe 223 so that the carbon adsorbent charged in the second reactor 220 is always maintained at a constant level, And is stored in the accommodating portion 212. That is, one end of the second pipe 223 communicates with the inside thereof at a predetermined height of the second reactor 220, and the other end communicates with the inside thereof at a predetermined height of the first reactor 210. At this time, the second pipe 223 is curved so as not to be disturbed by upward flow.

In the dual biomass gasification reactor 20 having the above-described configuration, by charging a certain amount of carbon adsorbent into the second reactor 220, the tar in the product gas is adsorbed to reduce the content of tar, Thereby promoting the reaction with moisture in the generated gas to assist in the production of hydrogen, thereby enabling the production of gas of high calorific value.

Also, the biomass gasification reactor 20 can reduce the amount of particles contained in the generated gas through the following components. The surplus biochar in the first reactor 210 is discharged to the receiving part 212 through the first pipe 211 and the surplus biochar in the first reactor 210 is discharged through the distribution plate 221 of the second reactor 220, 210 to filter the biochar in the product gas flowing into the second reactor 220 along the ascending air flow and prevent the outflow of the carbon adsorbent inside the second reactor 220 through the third cyclone 222 The amount of particles contained in the product gas can be reduced by discharging excess carbon adsorbent in the second reactor 220 through the second pipe 223 to the receiving 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 to supply water vapor as necessary, and is constituted by a general configuration used in a fluidized bed gasification apparatus.

The purification means 40 serves to purify the exhaust gas discharged from the second reactor 220 so that it can be used for electric power production or the like, and has a general constitutional relationship used in the fluidized bed gasification apparatus.

Second Embodiment

The gasification apparatus according to the second embodiment of the present invention is configured in the same manner as the gasification apparatus of the first embodiment except for a part of the structure of the reactor. Therefore, like or similar elements to those of the first embodiment will be denoted by similar reference numerals and the description thereof will be omitted.

4 is a conceptual diagram of a gasification apparatus 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 of the present embodiment is constructed so that the biomass injected through the biomass injection means 10a is supplied to the external heat source supplied from the heat source supply means 30a, A first reactor 210a for gasification using a heat source and a second reactor 220a for reducing the content of tar by adsorbing or decomposing tar in the product gas generated in the first reactor 210a. Here, the second reactor 220a has a larger size and a larger volume than the first reactor 210a, and is installed just above the first reactor 210a. Accordingly, the first and second reactors 210a and 220a have a two-tiered shape, and the connecting portion thereof has a tapered shape.

The first reactor 210a may be configured such that a certain amount of sand is filled in the first reactor 210a and the surplus biochar produced during the process is stored in the receiver 212a along the first pipe 211a, 1 < / RTI > reactor < RTI ID = 0.0 > 210. < / RTI >

The second reactor 220a is filled with a certain amount of carbon adsorbent (activated carbon and / or biochar). The second reactor 220a has a nickel distribution plate 221a communicating with the first reactor 210a, A cyclone 222a for supplying a product gas in which the content of tar is reduced as well as the outflow of the adsorbent to the purification means 40a and a second pipe 223a for connecting the first and second reactors 210a and 220a, And has the same function and role as the second reactor 220 of the first embodiment. Unlike the nickel distribution plate 221 of the first embodiment, the nickel distribution plate 221a may be configured such that a hook-shaped pipe protrudes toward the upper end of each hole toward the second reactor 220a have.

The air in the first reactor 210a is supplied to the connecting portion of the first and second reactors 210a and 220a to supply tar in the product gas flowing into the second reactor 220a, An air supply line 310a for reducing the amount of tar in the generated gas is installed so as to communicate with the heat source supply means 30a. By supplying air in this way, the content of the tar in the generated gas can be reduced by oxidizing it.

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

In addition, the dual biomass gasification reactor of the present invention and the biomass gasification apparatus having the same have a separate inner reactor or a two-stage reactor, and contain a carbon adsorbent in the upper reactor, And generate high calorific gas, so that it can be designed to have a medium size power generation capacity. Thus, it is possible to overcome the limitation that a conventional fixed bed gasifier can be used for a miniature power generation system.

The dual biomass gasification reactor of the present invention and the biomass gasification apparatus having the dual biomass gasification reactor can also produce gas of high calorific value having low amount of tar and ammonia which can be stably used for electric power generation and the like by having the dual biomass gasification reactor.

The dual biomass gasification reactor of the present invention and the biomass gasification apparatus having the dual biomass gasification reactor can also be constructed in a double structure 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 in which a biomass gasification apparatus according to the present invention constructed as described above is manufactured and tested will be described.

1 kg of dry sewage sludge with a size of 250 ~ 425 ㎛ was used as the biomass feed material and 500 g of activated carbon was used as carbon adsorbent.

The gasification apparatus was constructed as shown in FIG. 5, and a two-stage gasification reactor made of STS-316 was used. Here, the lower reactor had a size of 100 mm in diameter and 360 mm in height, and filled with silica sand. Three thermocouples were installed in the lower reactor for flow stability testing. The upper reactor had a size of 160 mm in diameter and 340 mm in height, and filled with activated carbon. Two thermocouples were installed in the upper reactor for flow stability testing.

Cyclone was used to filter particles of 10 μm or more, and hot filter to filter particles of 1 μm or more. The condenser cooled the condensate liquid to 0 ° C. The resulting gas was analyzed using GCs and GC-MS systems.

 Comparative Example 1 Comparative Example 2 Example 1 Experimental conditions Upper reactor temperature (캜) 807 800 793 Lower reactor temperature (캜) 812 779 794 Operating time (min) 91 93 93 Equivalent ratio * 0.20 0.21 0.20 Bed material (g) Natural olivine
2,500 g Natural olivine
2,500 g Natural olivine
2,500 g In the upper reactor
Charged amount of activated carbon (g) Not used Used
2,000 g Used
2,000 g Distribution plate material Stainless steel
Distribution plate Stainless steel
Distribution plate Stainless steel plate with nickel-plated distribution 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

* The equivalence ratio represents the amount of air that is actually supplied in the gasification / amount of air required for chemical oxidation for complete oxidation.

Referring to Table 2, in the case of Example 1 using a nickel-plated stainless steel distribution plate, compared with Comparative Example 2 (0.06 g / Nm ³ ) which was tested under the same conditions except that a stainless steel distribution plate was used in place of the nickel distribution plate, (About 0.01 g / Nm &lt; ³ &gt;) was reduced by about 6 times or more. It was confirmed that the ammonia content (about 12 mg / L) of the product gas obtained in Example 1 was reduced by about 58.3 times as compared with Comparative Example 2 (700 mg / L). In addition, inactivation of the nickel distribution plate of Example 1 was not observed when the change of the product gas component was observed under the above-described experimental conditions.

Therefore, it was confirmed that the content of the tar in the case of Comparative Example 1 in which the stainless steel distribution plate was used as in Comparative Example 2 but the activated carbon was not charged in the upper reactor (the second reactor) was increased. The ammonia content of Comparative Example 1 was not measured, but it is considered to be more than 700 mg / L considering the properties of activated carbon having ammonia adsorption.

It will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit of the invention.

10: Biomass injection means
20: Gasification reactor
30: Heat source supply means
40: Purification means
210: first reactor
211: first pipe
212:
220: second reactor
221: Distribution board
222: Cyclone
223: Second pipe.

Claims (11)

A first reactor for gasifying the injected biomass using an external heat source and an oxidizing heat source of the biomass itself, wherein a sand or tar decomposition catalyst is filled therein and flows along the air stream of the external heat source, A first reactor for gasifying and generating a bio-char
The first reactor is connected to the first reactor and uses the heat source of the first reactor. The carbon adsorbent is filled in the first reactor, thereby reducing the content of tar in the product gas generated in the first reactor and increasing the production of hydrogen. A second reactor for supplying the reactants; And
A distribution plate disposed in a communicating portion between the first and second reactors to prevent the flow of the bichar and the sand or tar decomposition catalyst in the first reactor toward the second reactor, A distribution plate for preventing the adsorbent from flowing out toward the first reactor,
Wherein the distribution plate is a nickel plate. 2. The reactor according to claim 1, wherein the second reactor is fixed to the upper side of the inner side of the first reactor so as to be located on the upper side inside the first reactor, and is spaced apart from the inner circumference of the first reactor And a second biomass gasification reactor. The dual biomass gasification reactor according to claim 1, wherein the second reactor is installed at the upper end of the first reactor to form a two-stage reactor. The dual biomass gasification reactor according to claim 1, wherein the distribution plate is a nickel plate plated with an iron-based metal plate. 2. The dual biomass gasification reactor according to claim 1, wherein the distribution plate has a shape of a perforated plate having a plurality of holes. 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 according to claim 1, wherein the carbon adsorbent is activated carbon or biochar. [2] The apparatus of claim 1, wherein the first reactor comprises: a first pipe communicating with the interior of the first reactor to discharge surplus biochar to the outside so as to maintain a predetermined amount of the biochar in the first reactor; And
Further comprising a receiving portion for storing the surplus biochar discharged by gravity along the first pipe. 2. The process according to claim 1, wherein a cyclone is further provided in the second reactor to discharge a product gas in which a content of tar is reduced in a subsequent process and prevent the carbon adsorbent charged therein from flowing out. Biomass gasification reactor. The method of claim 1, further comprising a second pipe communicating the first and second reactors to flow excess carbon adsorbent toward the first reactor so that the carbon adsorbent inside the second reactor maintains a predetermined amount A dual biomass gasification reactor characterized by. 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.
A heat source supply means for supplying air preheated to the gasification reactor; And
And a purification means for purifying the exhaust gas discharged from the gasification reactor.

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