KR101611486B1 - Method for fast pyrolysis of biomass using double tube type fluidized bed reactor - Google Patents

Abstract

The present invention relates to a rapid pyrolysis method of biomass using a double tube-type bubble fluidized bed reactor, which can be driven in a stable manner. The rapid pyrolysis method comprises: a first step for inserting a certain amount of fluidized media in an inner tube of the reactor equipped in the reactor; a second step for preheating the reactor at constant temperature; a third step for inserting a reaction raw material stored in a hopper through a raw material insertion unit at a constant flow rate into the reactor; a fourth step for performing pyrolysis with respect to the reaction raw material by heating the temperature of the reactor at the predetermined temperature; a fifth step for collecting bio-char through a lower unit of a cyclone and a lower unit of the appearance of the reactor at a constant time interval; and a sixth step for collecting bio-oil generated through a tar separator and a bio-oil collection tank.

Description

TECHNICAL FIELD [0001] The present invention relates to a method for rapidly pyrolyzing a biomass using a double tube type bubble fluidized bed reactor,

The present invention relates to a rapid pyrolysis method of biomass, more particularly, to a method for maintaining a stable bubble fluidized bed in a reactor inner tube constituting a dual tube type reactor, The present invention relates to a rapid pyrolysis method of biomass using a double-tubular bubble fluidized bed reactor capable of stable operation than a conventional bubble fluidized bed reactor by rapidly separating /

Excessive use of fossil fuels, such as coal and oil, can lead to exhaustion of energy resources and environmental problems such as global warming.

A variety of methods have been studied to solve this problem, one of which is to increase the proportion of renewable energy such as bioenergy.

Bio-energy sources such as tree-like wood-based materials and herbal materials such as hay, ie, biomass, contain micro oil droplets inside, which can be used to make bio-energy.

Rapid thermal decomposition of these solid-state biomass in an oxidizer-free atmosphere yields a black-brown liquid pyrolysis material called bio-oil or bio-crude-oil.

As a by-product, bio-char and meteoric flammable syngas can occur, but the main purpose of bio-oil production is to obtain liquid fuel.

This liquid fuel has a higher energy density than the solid phase biomass, and has a merit of low transportation and storage cost.

Generally, the rapid pyrolysis of biomass is performed at a temperature of around 500 ° C and under normal pressure reaction conditions.

In order to maximize the yield of the pyrolysis oil, it is necessary to supply heat to the solid-phase biomass material from the external heat source as quickly as possible, and the residence time of the reactor is shortened to within a few seconds.

The product must also be cooled rapidly to minimize side reactions. Under these optimum reaction conditions, pyrolysis oil yield can be up to 80% based on biomass feedstock drying.

Conventional rapid pyrolysis reactors for biomass rapid pyrolysis include Korean Patent Registration No. 10-1285879, which is a device for obtaining biomass through fluidized bed rapid pyrolysis, and a device for pyrolyzing fluidized bed pyrolysis , As shown in Korean Patent Registration No. 10-0659497.

However, in the single-tube reactor, the solid product and the vapor product produced after the pyrolysis reaction of the biomass are mixed in a single tube, and the discharge port of the solid product is connected to the portion where the fluidized bed is formed, But it was difficult to separate them.

DISCLOSURE Technical Problem The present invention has been conceived to solve the problems as described above, and it is an object of the present invention to provide a bubble-fluidized bed in which a stable bubble fluidized bed is maintained in an inner tube of a reactor by performing rapid pyrolysis of biomass using a double tube type reactor, The present invention aims to provide a rapid pyrolysis method of biomass using a dual-tubular bubble fluidized bed reactor capable of rapidly separating and removing bio-char from other products.

However, the object of the present invention is not limited to the above-mentioned objects, and other objects not mentioned can be clearly understood by those skilled in the art from the following description.

In order to achieve the above object, a rapid pyrolysis method of a biomass using a dual-tubular bubble fluidized bed reactor according to an embodiment of the present invention includes a first pyrolysis step of introducing a certain amount of a fluidizing medium into an inner tube of a reactor provided in a reactor, A second step of preheating the reactor to a predetermined temperature, a third step of feeding the reaction feedstock stored in a hopper into the reactor at a constant flow rate through the feedstock inlet, A fifth step of collecting bio-char through a lower portion of the outer surface of the reactor and a lower portion of the cyclone at predetermined time intervals, and a fifth step of collecting bio- And a sixth step of collecting the bio-oil produced through the bio-oil.

Further, in the rapid pyrolysis method of biomass using the dual tubular bubble fluidized bed reactor according to the present invention, the fluidizing medium in the first step includes sand.

The method for rapid pyrolysis of biomass using the dual tubular bubble fluidized bed reactor according to the present invention is characterized in that it comprises the step of introducing a carrier gas into the reactor at a constant rate after the preheating in the second step.

Also, in the rapid pyrolysis method of biomass using the dual tubular bubble fluidized bed reactor according to the present invention, the reaction material stored in the hopper in the third step may include sawdust, empty fruit bunch (EFB) Or a product thereof.

Further, the rapid pyrolysis method of biomass using the dual tubular bubble fluidized bed reactor according to the present invention is characterized in that nitrogen is introduced into the hopper in which the reaction raw material is stored, followed by pressurization at a constant pressure.

Also, the rapid pyrolysis method of a biomass using the double-tubular bubble fluidized bed reactor according to the present invention is characterized in that the pyrolysis is performed by supplying nitrogen at a certain pressure from the outlet of the cyclone during the pyrolysis to remove the tar generated in the direction of the condenser .

Also, in the rapid pyrolysis method of biomass using the dual tubular bubble fluidized bed reactor according to the present invention, in the third step, the reacted raw material to be introduced has a particle size of 10 mm or less and a water content of 15 wt% or less, And the feeding rate of the reaction raw material is 1.0 to 3.0 kg / hL per unit volume of the inner tube of the reactor.

In the rapid pyrolysis method of biomass using the dual tubular bubble fluidized bed reactor according to the present invention, the temperature of the reactor is maintained at 420 ° C. to 530 ° C. during pyrolysis.

Further, in the rapid pyrolysis method of biomass using the dual tubular bubble fluidized bed reactor according to the present invention, the temperature of the freeboard and the cyclone during pyrolysis is maintained at 400 ° C to 500 ° C.

According to the rapid pyrolysis method of the biomass using the double pipe-type bubble fluidized bed reactor of the present invention, the EFB (empty fruit) generated in the palm oil-milking process, which occurs in the wood- bunch) and its torrefaction product, it is possible to maintain a stable bubble fluidized bed in the inner tube of the reactor and to rapidly separate and separate the bio-char, which is a solid product, from the solid product, There is a feature that can be removed.

Therefore, according to the present invention, there is an advantage that it is possible to operate more stably than the conventional bubble fluidized bed reaction apparatus.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic view showing a dual-tubular fluidized bed reactor for biomass rapid pyrolysis according to the present invention. FIG.
FIG. 2 is a view showing a double tube type bubble fluidized bed reactor equipped with a double-tube type fluidized bed reactor according to the present invention.
3 is a flowchart showing a rapid thermal decomposition method of biomass using the dual tubular bubble fluidized bed reactor according to the present invention.
4 is a graph exemplarily showing the effect of reaction temperature on the thermal decomposition product distribution from the rapid thermal decomposition of sawdust.
5 is a graph exemplarily showing the effect of pyrolysis temperature on total organic carbon content (TOC) and O / C ratio of bio-oil produced from rapid thermal decomposition of sawdust.
Fig. 6 is a graph exemplarily showing the fuel characteristics of the bio-tea according to the pyrolysis temperature.
7 is a graph exemplarily showing the influence of the feed rate of the reaction raw material on the yield of the product obtained from rapid thermal decomposition of sawdust.
8 is a graph exemplarily showing the influence of the feed rate of the reaction raw material on bio oil production from rapid thermal decomposition of sawdust.
9 is a graph exemplarily showing the influence of the feed rate of the reaction raw material on the bio-tea production from the rapid thermal decomposition of sawdust.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, a detailed description of preferred embodiments of the present invention will be given with reference to the accompanying drawings. In the following description of the present invention, detailed description of known functions and configurations incorporated herein will be omitted when it may make the subject matter of the present invention rather unclear.

Embodiments in accordance with the concepts of the present invention can make various changes and have various forms, so that specific embodiments are illustrated in the drawings and described in detail in this specification or application. It is to be understood, however, that it is not intended to limit the embodiments according to the concepts of the present invention to the particular forms of disclosure, but includes all modifications, equivalents, and alternatives falling within the spirit and scope of the invention.

It is to be understood that when an element is referred to as being "connected" or "connected" to another element, it may be directly connected or connected to the other element, . On the other hand, when an element is referred to as being "directly connected" or "directly connected" to another element, it should be understood that there are no other elements in between. Other expressions that describe the relationship between components, such as "between" and "between" or "neighboring to" and "directly adjacent to" should be interpreted as well.

The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. The singular expressions include plural expressions unless the context clearly dictates otherwise. In this specification, the terms "comprises ",or" having ", or the like, specify that there is a stated feature, number, step, operation, , Steps, operations, components, parts, or combinations thereof, as a matter of principle.

FIG. 1 is a schematic view of a dual-tubular fluidized-bed reactor for biomass rapid pyrolysis according to the present invention. As shown in FIG. 1, a dual-tubular fluidized bed reactor 100 includes a hopper 111, The reactor inner tube 121, the dispersion plate 122, the carrier gas chamber 123, the reactor outer tube 131, the bio-char collector 133, the freeboard 137, the carrier gas inlet 141 and a product discharge unit 150. [

The raw material or herbaceous material, which is a raw material for biomass, can be supplied through the raw material input portion 111. The neck base material or herbaceous base material can be, for example, waste wood, waste paper, rice husks, sawdust, stem of plants, and the like.

One end of the raw material input portion 111 is connected to the reactor inner pipe 121 so that the biomass is accommodated in the inner space of the reactor inner pipe 121 and the biomass is rapidly pyrolyzed through the reaction to generate a steam phase product and a solid phase product .

For example, a screw feeder may be installed in the raw material input portion 111, and the biomass may be introduced into the reactor inner pipe 121 without being blocked by the raw material input portion 111.

The dispersion plate 122 may be disposed between the transfer gas chamber 123 disposed at the lower portion of the reactor inner tube 121 and the reactor inner tube 121. The carrier gas in the carrier gas chamber 123 may pass through the dispersion plate 122 to pyrolyze the biomass in the inner space of the reactor inner tube 121 to form a fluidized bed.

Pressure gauges 125a and 125b are installed at the upper part of the dispersion plate 122 and the end point of the in-reactor inner pipe 121, respectively.

The closer the pressure difference (? P) between the two pressure gauges is to zero, the higher the yield of the bio-oil. In addition, the reactor inner tube 121 is provided with a thermocouple 126 spaced apart at a predetermined interval to measure the temperature of the reactor inner tube 121.

The dispersion plate 122 is filled with a certain amount of fluidizing medium and is mixed with the fluidized bed to help efficiently transfer heat to the biomass. The fluidization medium is a material with a hard and uniform particle size, for example sand.

Further, a carrier gas inlet 141 for supplying a carrier gas is formed at a lower side surface of the carrier gas chamber 123. The carrier gas is heated and introduced at a high temperature. Particularly, the carrier gas is a material which is not reactive in the thermal decomposition reaction. For example, the carrier gas may be nitrogen (N ₂ ), carbon dioxide (CO ₂ ) The gas may be oxygen (O ₂ ), carbon monoxide (CO), water vapor (H ₂ O), sulfur dioxide gas (SO ₂ ), and the like.

Since the fine solid material, for example, bio-char, produced in the fluidized bed can be transferred to the carrier gas chamber 123 through the dispersion plate 122, A valve 124 capable of removing the car can be mounted.

Particularly, for the operation of the valve 124 installed at the lower end of the carrier gas chamber 123, the bio-tea collecting part 133 is connected to the reactor outer tube 131 and the joint part 134 such as a flange as shown in the figure So that attachment and detachment can be facilitated.

A heater may be installed on the outer wall of the reactor inner pipe 121, the reactor outer pipe 131 and the transfer gas chamber 123 to maintain the proper temperature by heating the reactor 100, though not shown.

The inside of the reactor outer tube 131 is spaced apart from the outer side of the reactor inner tube 121 and may be formed so as to surround the reactor inner tube 121 and may be formed between the reactor outer tube 131 and the reactor inner tube 121 May be connected by a connecting device 132 of a size that is not disturbed by the falling of the bio-car.

A bio-disc collecting unit 133 is located inside the outer surface 131 of the reactor 131, and the bio-disc produced through the rapid thermal decomposition reaction is dropped by gravity and collected. As a result, the bio-car can be collected in a space different from the space in which the vapor phase product is collected, thereby enabling efficient separation.

The bio-tea collected in the bio-tea collecting unit 133 can open and discharge the valve 135 at the lower end. At this time, a certain amount of the collected bio-tea can be left to minimize the heat loss from the outside of the reactor 100.

The freeboard 137 is positioned between the upper end of the reactor outer tube 131 and the upper end of the inner reactor tube 121 to collect the vapor phase material generated through the rapid thermal decomposition reaction, 138 are mounted on the free board 137 to measure the temperature of the free board 137.

A forced discharge pipe 136 is mounted on one side of the freeboard 137 so that the bio-car separated from the freeboard 137 can not be separated from the reactor exterior pipe 131 due to the blockage of the bio-lane.

The product discharge portion 150 is connected to the upper surface of the freeboard 137 to discharge the vapor phase product to the outside.

FIG. 2 is a schematic view showing a biomass rapid thermal cracking apparatus 200 having a dual-tubular fluidized bed reactor 100 according to the present invention, and FIG. 3 is a schematic view showing a rapid pyrolysis method of biomass using a double- A hopper 112 for storing biomass as a reaction raw material, a feed inlet 111, a reactor inner pipe 121, a reactor outer pipe 131, A bio-oil collecting unit 133, a freeboard 137, a cyclone 210, a condenser 221, a bio-oil collecting tank 222, a cooler (not shown) A tar separator 232, a tar separator 233,

Hereinafter, a rapid pyrolysis method of the biomass using the dual tubular bubble fluidized bed reactor will be described with reference to FIGS. 2 and 3. FIG.

A flange (not shown) at the upper part of the reactor inner pipe 121 is opened and an appropriate amount of a fluidizing medium, for example, sand is charged, and then the flange is closed (S101).

Thereafter, the reactor 100 is preheated through the heating device (S102), and the preheated high-temperature carrier gas is supplied to the in-reactor tube 121 at a predetermined flow rate to flow the fluidizing medium.

The reactor 100 is heated and the biomass as a reaction raw material prepared in advance so as to have a proper moisture content and particle size is supplied from the hopper 112 to the reactor inner pipe 121 by using the feed inlet 111, (S103).

At this time, a stirrer 113 may be installed in the hopper 112 to smoothly inject the reaction material into the hopper 112, and the reaction material may be stirred at a predetermined speed, for example, about 10 rpm. ), And then pressurized at a constant pressure.

The biomass as a reaction raw material may be any one of sawdust generated in a wood-making mill or pellet producing process, empty fruit bunch (EFB) generated in palm oil-milking process or its torrefaction product.

The reaction raw material used in the embodiment of the present invention is sawmill sawdust and may have a particle size of 10 mm or less and a moisture content of 15 wt% or less.

In the inner tube 121 of the reactor, a fluidized bed is formed while the transported biomass and medium are fluidized by the high temperature carrier gas supplied through the dispersion plate 122, and a high temperature fluidizing medium flowing therethrough collides with the biomass, The pyrolysis process can be performed by rapidly supplying heat (S104).

The high temperature carrier gas can also be heated in the preheater 142 to supply nitrogen to the reactor inner tube 121 through the carrier gas chamber 123 and the dispersion plate 122 without additional reaction to the pyrolysis reaction, An electric heating furnace (not shown) may be installed on the outer wall of the carrier gas chamber 123, the reactor outer tube 131, the freeboard 137, and the cyclone 210. [

This allows the temperature of the reactor 100 to be maintained at 420 ° C. to 530 ° C. or the temperature of the freeboard 137 and the cyclone 210 to be maintained at about 400 ° C. to 500 ° C. during pyrolysis.

The fluidized bed at the time of pyrolysis is formed in the entire inner tube 121 of the reactor and separated from the vapor phase product having a larger particle size in the freeboard 137, that is, the bio-char is lighter than the vapor phase product, The bio-disc collecting unit 133 may be separated from the bio-disc collecting unit 133 (S105).

In this way, since a constant fluidized bed can be maintained in the reactor inner pipe 121, stable operation can be performed.

The remaining product having a large particle size and a heavy solid product separated from the freeboard 137 flows into the cyclone 210 to further separate the remaining solid product and then flows into the condenser 221 and rapidly cooled to condense the bio- Of the synthesis gas.

A bio-oil collecting tank 222 is disposed under the condenser 221 to separate and collect condensed liquid bio-oil (S106).

Since the synthetic gas discharged from the upper portion of the condenser may contain a small amount of tar, a cooler 231, a tar separator 232, a tar separator 233, and the like are installed to separate and remove the tar.

Particularly, as the temperature is suddenly cooled in the duct between the cyclone 210 and the condenser 221, the tar in the produced material becomes solidified and the duct can be closed. Therefore, the tar produced by supplying the high pressure nitrogen through the gas pipe inserted into the cyclone 210 in the direction of the condenser 221, that is, the tube 211, can be removed toward the condenser 221.

≪ Result of rapid pyrolysis >

The results of rapid pyrolysis using the double tube type bubble fluidized bed reactor 200 according to the present invention are as follows.

(1) Pyrolysis reaction temperature

The effect of reaction temperature on the thermal decomposition product distribution from the rapid pyrolysis of sawdust is shown in FIG.

The pyrolysis reaction temperature may be the temperature of the top of the dispersion plate, the temperature of the feedstock at the point of introduction of the feedstock, and the temperature of the feedstock, And the average value of the upper temperature.

Feeding rate of reaction material was expressed by dividing biomass input per hour divided by reactor inner tube volume. The carrier gas flow rate was set so that the residence time of the reactant was about 2 seconds (s).

The amount of bio-syngas generated in the product was calculated by subtracting the amount of bio-oil and bio-char from the feed amount of the reaction product.

As shown in the figure, the yield of bio-oil reached 60.3 wt% at about 440 ° C, and gradually decreased with increasing reaction temperature and dropped to 41.3 wt% at about 530 ° C.

On the other hand, the gas product remained at 18.3 wt% at 426 ° C, but increased at higher reaction temperature and showed 38.7 wt% at 530 ° C.

The bio-char, the solid product, showed a tendency to be opposite to the gas product. That is, the maximum value was 28.7 wt% at 426 DEG C and reached the lowest value at 20.0 wt% at 528 DEG C.

More than 80 wt% of bio - tea was obtained at the bottom of the reactor. The lower the reaction temperature, the higher the ratio obtained at the bottom of the reactor.

From these results, it can be seen that the optimum pyrolysis reaction temperature suitable for producing bio oil from sawdust is 440 ° C.

5 is a graph exemplarily showing the effect of thermal decomposition temperature on the total organic carbon content (TOC) and O / C ratio of bio-oil produced from rapid thermal decomposition of sawdust.

As shown in the figure, the TOC of the bio-oil did not show a significant change to about 400 g / L in the reaction temperature range of 420 to 530 ° C, but the O / C ratio showed a minimum value of 1.1 near 440 ° C.

It increased with the increase of pyrolysis temperature and showed the maximum value at 1.8 ℃ at 530 ℃.

Although there is no change in the organic carbon content, the oxygen content of the bio - oil is affected by the pyrolysis temperature relatively, considering that there is a large change in the O / C ratio.

Also, the O / C non - tendency of the bio - oil to the reaction temperature was completely opposite to the yield. In conclusion, the maximum O / C ratio and maximum calorific value can be obtained when the bio oil yield is maximum.

Bio-char and bio-syngas are produced as a byproduct of rapid pyrolysis of biomass. These by-products can be used as a pyrolysis heat source by burning. If there is an industrial demand, The economical efficiency of the pyrolysis process can be enhanced.

In particular, bio-tea has high calorific value and potentially high added value because it can be reproduced by a material such as activated carbon with high adsorption capacity and high purity carbon through a relatively simple process. Therefore, it is important to understand the characteristics of bio-tea which is a by-product of pyrolysis.

FIG. 6 exemplarily shows the fuel characteristics of the bio-tea according to the pyrolysis temperature.

As the pyrolysis temperature increased, the ash content steadily increased. As the reaction temperature increased, the carrier gas velocity increased and the amount of pyrolysis vapor increased. As a result, some of the sand as a fluidization medium was lost in the inner tube and contained in the bio- .

Generally, the fuel characteristics such as the heating value of the bio-tea and the O / C ratio are not significantly changed in the range of 420 to 500 ° C.

(2) Reaction feed rate

7 is a graph exemplarily showing the influence of the feed rate of the reaction raw material on the yield of the product obtained from rapid thermal decomposition of sawdust.

As shown in the figure, it can be seen that the product distribution is not greatly influenced by the feeding rate.

The bio-oil and bio-tea products showed the highest yields of 62.2wt% and 25.5wt%, respectively, when the feed rate of the raw material was 2.6kg / h · L, and the bio-syngas were 1.2 kg / h · L, the highest value was 17.0 wt%.

When no feedstock is added, that is, only the carrier gas is fed, the reactor residence time of the carrier gas is about 2 seconds (s) at the reaction temperature.

When rapid reaction of raw materials is carried out and pyrolysis proceeds and a large amount of vapor phase product is produced, the residence time of the reactor becomes shorter than 2 seconds, so that the residence time of the reactor in which the maximum bio oil yield can be obtained is within 2 seconds .

FIG. 8 shows an example of the influence of the feeding rate of the reaction raw material on bio oil production from the rapid thermal decomposition of sawdust.

In the range of reaction temperature 440 ℃ and feed rate 1.2 ~ 2.6kg / h · L, there was no significant change in bio oil yield and fuel characteristics. However, as the feed rate increased, the yield of bio-oil and O / C ratio tended to increase.

This is a tendency different from the influence on the pyrolysis temperature shown in FIG. Also, the O / C ratio is more sensitive to the feed rate than the yield or TOC.

9 is a graph exemplarily showing the influence of the feed rate of the reaction raw material on the bio-tea production from the rapid thermal decomposition of sawdust. As shown in the figure, the yield and the calorific value of the bio- The ash content decreased significantly from 10 to 3.8 as the feed rate increased from 1.2 to 2.6 kg / h · L.

This can be attributed to the fact that the increased feedstock in the reactor at high feed rates reduced the loss by suppressing the overflow of sand, the fluidizing medium.

Therefore, based on the above-described results, the optimal operation condition for performing the biomass rapid thermal decomposition using the dual-tubular bubble fluidized bed reactor according to the present invention can be set as follows.

First, the reaction raw material uses woody biomass, but the particle size may vary depending on the size of the reactor or the purpose of pyrolysis.

Therefore, the maximum particle size should be smaller than the distance between the inner tube and the outer surface of the reactor, and the purpose of rapid pyrolysis should be 10 mm or less in the case of bio-oil production as the liquid product, and as the water content is high, In order to prevent the burden from increasing in the treatment process, it is preferably 15 wt% or less.

In addition, when the reaction material is charged, a cover is provided on the upper part of the hopper, and then oxygen-free gas such as nitrogen or pyrolysis gas is introduced into the hopper to maintain a pressure of about 0.02 bar.

In the case of a pyrolysis reactor, the pyrolysis temperature of biomass should be in the range of 420-530 ° C for bio-oil production purposes, and the pressure should be within 0.3 bar. It is also preferred that the feed rate be maintained in the range of 1.0 - 3.0 kg / hL per reactor inner tube volume.

In addition, the cyclone temperature connected to the freeboard (FB) in the upper part of the reactor is operated in the range of 400-500 ° C, and 450 ° C is suitable as far as possible.

Since the tar between the cyclone and the condenser is suddenly cooled, the tar is solidified and the pipeline can be closed. Therefore, the gas pipe is inserted in the direction of the condenser from the cyclone, and the gas at about 5 bar The tar is cooled for one second and removed from the pipeline. At this time, it is preferable that the condenser is operated so that the product can be quenched as much as possible, but the product outlet temperature is not higher than 20 ° C at the maximum.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is to be understood that the invention is not limited to the disclosed embodiments, but, on the contrary, is intended to cover various modifications and equivalent arrangements included within the spirit and scope of the appended claims. will be. Accordingly, the true scope of the present invention should be determined by the technical idea of the appended claims.

100: Double tube type fluidized bed reactor
111: Feedstock feeding part 112: Hopper 112
121: Reactor inner tube 122: Dispersion plate
123: Carrier gas chamber 124, 135: Valve
125a, 125b: pressure gauges 126, 127, 138: thermocouple
131: Reactor Appearance 132: Connection Device
133: bio-char collecting unit 134:
136: Forced discharge pipe 137: Free board (FB)
141: gas inlet 142: preheater
150:
200: double tube type bubble fluidized bed reactor
210: Cyclone 221: Capacitor
222: Bio-oil collection tank 231: Cooler
232: tar separator 233: tar separator

Claims (9)

In a rapid pyrolysis method of a biomass using a double tube type bubble fluidized bed reactor,
A first step of injecting a certain amount of a fluidizing medium into a reactor inner tube provided in the reactor;
A second step of preheating the reactor to a predetermined temperature;
A third step of feeding a reaction material stored in a hopper into the reactor at a constant flow rate through a raw material input part;
A fourth step of performing pyrolysis on the reaction material by heating the temperature of the reactor to a predetermined temperature;
A fifth step of collecting bio-char through the lower part of the outer appearance of the reactor and the lower part of the cyclone at regular time intervals; And
And a sixth step of collecting the bio-oil produced through the bio-oil collecting tank and the tar separator,
The method according to claim 1, wherein in the third step, nitrogen is introduced into the hopper in which the reaction material is stored, and then the mixture is pressurized at a constant pressure.
The method according to claim 1,
Wherein the fluidizing medium comprises sand in the first step. 2. The method of claim 1, wherein the fluidizing medium comprises sand.
The method according to claim 1,
Wherein the step of introducing the carrier gas into the reactor at a predetermined rate comprises the step of introducing the carrier gas into the reactor at a constant rate.
The method according to claim 1,
In the third step, the reaction material stored in the hopper is any one of sawdust, empty fruit bunch (EFB), and torrefaction products thereof. In the double-tubular bubble fluidized bed reactor, Pyrolysis method.
delete The method according to claim 1,
Wherein the pyrolysis is performed by supplying nitrogen at a predetermined pressure from the outlet of the cyclone to remove tar generated in the direction of the condenser. 2. The pyrolysis method of biomass according to claim 1,
The method according to claim 1,
In the third step,
The reaction raw material to be added has a particle size of 10 mm or less, a water content of 15 wt% or less,
Wherein the feeding rate of the reaction material is 1.0 to 3.0 kg / hL per volume of the inner tube of the reactor.
The method according to claim 1,
Wherein the temperature of the reactor is maintained at 420 ° C to 530 ° C during pyrolysis.
The method according to claim 1,
Wherein the temperature of the freeboard and the cyclone at the time of pyrolysis is maintained at 400 ° C. to 500 ° C. 2. A method for rapid pyrolysis of biomass using a double tube type bubble fluidized bed reactor,

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