WO2017078225A1

WO2017078225A1 - Bio oil recovering apparatus using plasma wind

Info

Publication number: WO2017078225A1
Application number: PCT/KR2016/002273
Authority: WO
Inventors: 이병호; 황리호; 박상훈; 최문규; 곽민호; 박기만; 윤영민
Original assignee: 주식회사 대경에스코; 주식회사 비츠로테크
Priority date: 2015-11-06
Filing date: 2016-03-08
Publication date: 2017-05-11
Also published as: KR101831897B1; KR20170053789A

Abstract

The present invention relates to a bio oil recovering apparatus using plasma wind, the apparatus introducing organic waste into a reactor and recovering bio oil by means of pyrolysis using plasma wind. To this end, the bio oil recovering apparatus using plasma wind of the present invention is configured to include: a pyrolysis unit that uses plasma wind and pyrolyzes received organic waste; an oil recovery unit that separates, cools, and recovers bio oil contained in exhaust gas discharged from the pyrolysis unit; a gas circulation unit that supplies the exhaust gas discharged from the oil recovery unit to the pyrolysis unit and circulates the gas; and a thermal wind supply unit that supplies thermal wind for maintaining heat inside the pyrolysis unit or the gas circulation unit.

Description

Bio oil recovery device using plasma hot air

The present invention relates to a bio-oil recovery apparatus using plasma hot air, and more particularly, to a bio-oil recovery apparatus using plasma hot air for recovering bio oil through pyrolysis using plasma hot air by introducing organic waste into a reactor. .

Recently, various industrial wastes generated in various fields are recycled because they are manufactured from solid fuels such as RPF (Refuse Plastic Fuel) or RDF (Refuse Derived Fuel), which are not simply landfilled or incinerated.

However, organic wastes are low in calorific value and thus lack of economic feasibility to directly convert to solid fuels. Therefore, a technology for producing char and bio-oil by pyrolysing organic wastes at high temperature is being developed.

For example, Korean Patent No. 10-1376737 discloses a bio-oil production apparatus and a bio-oil production process using the same.

Specifically, a bio oil is supplied through a reactor for receiving biomass from a silo, a cyclone for receiving a synthesis gas discharged from the reactor and then performing a separation process, and cooling the synthesis gas that is separated from the cyclone in the cyclone. And a non-condensing gas storage unit for separating and storing the non-condensing gas discharged from the condensation unit in stages, wherein the non-condensing gas stored in the non-condensing gas supply unit can be supplied to the reactor again. It is configured to be.

Meanwhile, in order to rapidly pyrolyze the organic waste introduced into the reactor, high temperature hot air of about 450 ° C. to 550 ° C. needs to be continuously supplied to the reactor as a pyrolysis reaction gas. Since the exhaust gas is used as a pyrolysis reaction gas, the combustion air injected when the oil or the gas is combusted is subjected to the combustion reaction, and the surplus oxygen remaining in the reactor is supplied to the reactor so that the oxygen concentration in the reactor gradually increases during continuous operation.

For this reason, the oxygen remaining in the reactor is combined with the carbon constituting the organic waste is converted into carbon dioxide gas has a problem that the production of the bio-oil rapidly decreases as the operating time is longer.

Therefore, there is a problem in that the biooil production efficiency gradually decreases during long-term operation, and when the nitrogen gas is heated as a pyrolysis reaction gas by using a heat exchanger to heat up nitrogen gas as a high temperature exhaust gas generated by fuel combustion, heating of nitrogen gas due to heat exchange The efficiency is low, there is a problem that the fuel consumption increases.

In addition, the biooil recovered from the reactants produced by rapid pyrolysis of organic wastes has a higher viscosity than ordinary oils and is easily cured at room temperature so that they do not flow down as they stick to the inner surface of the reactor and the inner surface of the cyclone. Not only does the phenomenon occur frequently and the recovery rate drops, as well as a problem that takes a long time to clean the oil stuck to the inner surface of the reactor and the inner surface of the cyclone.

In addition, in order to recover the biooil from the reaction product generated by pyrolysis in the reactor, the biofuel particles in the vapor state are cooled and condensed by the oil sprayed from the condensation recovery facility installed at the rear of the reactor, but the fine oil bioparticles of fine mist particles are recovered. Since it is recycled through the exhaust gas circulation duct with the exhaust gas without condensation, there is also a problem that the oil is stuck to the exhaust gas circulation duct and the blower blade, which is an important cause of mechanical failure.

An object of the present invention for solving the problems according to the prior art is to thermally decompose using the plasma hot air generated by a plasma hot air fan in which the pyrolysis reaction gas is supplied only to nitrogen air, so that oxygen supply is essentially blocked in the entire system. Therefore, even if the operation time is long, the production of bio oil is not reduced and stable operation can be continued. In addition, the reactor, the cyclone, and the electrostatic precipitator are formed in a double partition structure, and thermal hot air is supplied between the double partition walls. Therefore, as the whole wall is kept warm, bio-oil using plasma hot air can increase the recovery efficiency and lengthen the cleaning cycle by preventing the high viscosity bio oil from sticking to the inner wall of the reactor, cyclone and electrostatic precipitator. In providing a recovery device.

Bio oil recovery apparatus of the present invention for solving the above technical problem, pyrolysis unit for pyrolyzing the organic waste received by using the plasma hot air; An oil recovery unit for separating and cooling the biooil contained in the exhaust gas discharged from the pyrolysis unit to recover the oil; A gas circulation unit configured to circulate the exhaust gas discharged from the oil recovery unit to the pyrolysis unit; And an insulating hot wind supply unit for supplying thermal hot air for insulating the inside of the pyrolysis unit or the gas circulation unit.

Preferably, the pyrolysis unit, the reactor for supplying the organic waste to discharge the pyrolyzed exhaust gas to the oil recovery unit; And a plasma hot air fan for supplying the mixed hot air to the inside of the reactor by mixing the plasma hot air and the exhaust gas supplied from the gas circulation unit.

Preferably, the reactor is formed of a double partition structure, the heat insulating hot air supply unit may supply the hot air for keeping warm between the double partition walls of the reactor to keep the interior of the reactor.

Preferably, the inner bottom of the reactor may be provided with a plurality of flow nozzles or porous plates connected to the plasma hot air, and the mixed hot air may be supplied into the reactor through the plurality of flow nozzles or the porous plates.

Preferably, the plasma hot air may be generated by using nitrogen gas as a carrier gas.

Preferably, the hot air in which the plasma hot air and the exhaust gas supplied from the gas circulation unit are mixed may be 450 ° C to 550 ° C.

Preferably, the oil recovery unit, a cyclone for performing a separation process after receiving the exhaust gas discharged from the pyrolysis unit; A cooling condenser connected to a rear end of the cyclone to recover bio-oil through cooling and condensing the exhaust gas which is separated from the fan in the cyclone; And an electrostatic precipitator connected to the rear end of the cooling condenser to recover the biooil on the fine particles not recovered from the cooling condenser by an electrostatic precipitating method.

Preferably, the cyclone and the electrostatic precipitator is formed in a double partition structure, the heat insulating hot air supply unit may supply the hot air for insulating between the double partition of the cyclone and the electrostatic precipitator to insulate the interior of the cyclone and the electrostatic precipitator .

Preferably, the electrostatic precipitator may be configured such that one or two or more of the electrostatic precipitators are connected in series using either a flat electrostatic precipitator or a cylindrical electrostatic precipitator.

Preferably, the gas circulation unit, the storage tank for storing the exhaust gas discharged from the oil recovery unit; It may be configured to include; and a blower for supplying the exhaust gas stored in the reservoir to the pyrolysis unit.

Preferably, the thermal insulation hot air supply unit, a combustion burner for generating thermal insulation; It may be configured to include; and a blower for blowing and supplying the heat of insulation.

In the present invention as described above, the high-temperature plasma hot air generated by using nitrogen as a carrier air in a plasma torch at the bottom of the reactor after inputting organic waste such as sawdust, palm oil residues, grasses, agricultural residues into the reactor as a pyrolysis reaction gas. It has the advantage of stable recovery of char and bio oil, which are economical, from the reactants generated by thermal decomposition of carbon components among the various components constituting the organic waste by supplying through cooling, collecting, and recycling.

In addition, since the pyrolysis reaction gas is pyrolyzed using the plasma hot air generated by the plasma hot air supplied only with nitrogen air, the oxygen supply is fundamentally blocked in the entire system, so that the production amount of bio oil does not decrease even if the operation time is long. There is an advantage that stable operation can be continued without.

In addition, the reactor, the cyclone, the electrostatic precipitator is formed in a double partition structure, and as the hot air for thermal insulation is supplied between the double partition walls, the biooil with high viscosity is maintained in the reactor, cyclone, electrostatic precipitator. It is advantageous to increase the recovery efficiency and lengthen the cleaning cycle by suppressing the adhesion to the inner wall.

In addition, by collecting the fine biooil mist in the exhaust gas through the electrostatic precipitator has the advantage of preventing the biooil mist due to the circulation use of the exhaust gas attached to the device to reduce the failure factor of the device to extend the service life of the equipment .

1 is a block diagram showing the overall connection between the components of the bio-oil recovery apparatus using the plasma hot air according to an embodiment of the present invention.

2 is a block diagram illustrating a pyrolysis unit of a biooil recovery apparatus using plasma hot air according to an embodiment of the present invention.

3 is a block diagram showing an oil recovery unit of the bio-oil recovery apparatus using the plasma hot air according to an embodiment of the present invention.

Figure 4 is a block diagram showing a gas circulation unit of the bio-oil recovery apparatus using the plasma hot air according to an embodiment of the present invention.

5 is a block diagram showing a heat insulation hot wind supply unit of the bio-oil recovery apparatus using the plasma hot air according to an embodiment of the present invention.

100: pyrolysis unit 101: reactor

102: body 103: flow nozzle

104: raw material input conveyor 105: raw material input opening

106: fluid carrier storage tank 107: fluid carrier

108: plasma hot air fan 109: supply port

110: fluid flow outlet 111: connection conveyor

112: heat insulation hot air inlet 113: heat insulation hot air outlet

114: plasma torch 115: exhaust gas circulation duct

116: negative electrode 117: positive electrode

200: Oil recovery part 201: Cyclone

202: cooling condenser 203: spray nozzle

204: electrostatic precipitator 300: gas circulation unit

301: reservoir 302, 402: blower

303: gas vent valve 400: heat insulation hot air supply

401: burner

The present invention can be embodied in many other forms without departing from the spirit or main features thereof. Therefore, the embodiments of the present invention are merely examples in all respects and should not be interpreted limitedly.

Terms such as first and second may be used to describe various components, but the components should not be limited by the terms.

The terms are used only for the purpose of distinguishing one component from another. For example, without departing from the scope of the present invention, the first component may be referred to as the second component, and similarly, the second component may also be referred to as the first component.

The term and / or includes a combination of a plurality of related items or any item of a plurality of related items.

When a component is referred to as being "connected" or "connected" to another component, it may be directly connected to or connected to that other component, but it may be understood that other components may exist in the middle. It should be. \

On the other hand, when a component is said to be "directly connected" or "directly connected" to another component, it should be understood that there is no other component in between.

The terminology used herein is for the purpose of describing particular example embodiments only and is not intended to be limiting of the present invention. Singular expressions include plural expressions unless the context clearly indicates otherwise.

In this application, the terms "comprise", "comprise", "have", and the like are intended to indicate that there is a feature, number, step, operation, component, part, or combination thereof described in the specification. Or other features or numbers, steps, operations, components, parts or combinations thereof in any way should not be excluded in advance.

Unless defined otherwise, all terms used herein, including technical or scientific terms, have the same meaning as commonly understood by one of ordinary skill in the art.

Terms such as those defined in the commonly used dictionaries should be construed as having meanings consistent with the meanings in the context of the related art, and are not construed in ideal or excessively formal meanings unless expressly defined in this application. Do not.

Hereinafter, exemplary embodiments of the present invention will be described in detail with reference to the accompanying drawings, and the same or corresponding components will be denoted by the same reference numerals regardless of the reference numerals and redundant description thereof will be omitted.

In the following description of the present invention, if it is determined that the detailed description of the related known technology may obscure the gist of the present invention, the detailed description thereof will be omitted.

1 is a block diagram showing the overall connection relationship between the components of the bio-oil recovery apparatus using the plasma hot air according to an embodiment of the present invention, Figure 2 is a bio-oil using plasma hot air according to an embodiment of the present invention 3 is a block diagram illustrating a pyrolysis unit of a recovery device, FIG. 3 is a block diagram showing an oil recovery unit of a biooil recovery device using plasma hot air according to an embodiment of the present invention, and FIG. 4 is an embodiment of the present invention. FIG. 5 is a diagram illustrating a gas circulation unit of a biooil recovery apparatus using plasma hot air, and FIG. 5 is a diagram illustrating a heat insulation hot wind supply unit of a biooil recovery apparatus using plasma hot air according to an embodiment of the present invention.

Bio oil recovery apparatus using a plasma hot air according to an embodiment of the present invention, as shown in Figure 1, the thermal decomposition unit 100, oil recovery unit 200, gas circulation unit 300 and thermal insulation hot air supply unit ( 400).

The pyrolysis unit 100 is a component that thermally decomposes the organic waste received using plasma hot air.

The oil recovery unit 200 is a component for separating and cooling the biooil contained in the exhaust gas discharged from the pyrolysis unit 100 and recovering the oil.

The gas circulation unit 300 is a component that circulates the exhaust gas discharged from the oil recovery unit 200 to the pyrolysis unit 100.

The heat insulation hot air supply unit 400 is a portion for supplying heat insulation for warming the inside of the thermal decomposition unit 100 or the gas circulation unit 300.

On the other hand, during the initial operation of the biooil recovery apparatus using the plasma hot air of the present embodiment, in order to block the inflow of oxygen into the low-temperature exhaust gas circulated during continuous operation, all the facilities are filled with nitrogen to start the operation. It is preferable.

First, the thermal decomposition unit 100 will be described.

As illustrated in FIG. 2, the pyrolysis unit 100 includes a reactor 101 and a plasma hot air blower 108.

The reactor 101 is a component for supplying the organic waste and exhausting the pyrolyzed exhaust gas to the oil recovery part 200. The outer wall is formed in a double wall structure and has a cylindrical body 102 arranged vertically. It is configured to include.

The thermal hot air supplied from the thermal hot air supply unit 400 is supplied between the double wall structures, and the inside of the reactor 101 may be warmed by the thermal hot air, and thus, the reactor 101 ) It is possible to prevent the biooil having a high viscosity from adhering to and sticking to the inner inner wall.

In detail, the main body 102 of the reactor 101 has a heat insulating hot air inlet 112 formed at one point of the outer wall of the double wall structure, and the heat insulating hot air outlet 113 is formed at another point of the outer wall of the double wall structure. The wall temperature of the reactor 101 is maintained at an average of 300 ° C. by the hot air of about 150 ° C. to 400 ° C. supplied from the heat insulating hot air supply unit 400.

Meanwhile, a hot air supplied from the plasma hot air blower 108 is connected to the inside of the reactor 101 at the bottom of the inner bottom of the main body 102 forming the overall shape of the reactor 101. A plurality of flow nozzles 103 for supplying are provided, and a supply port 109 connected to the plasma hot air fan 108 is formed below the main body 102, and hot air supplied through the supply port 109 is provided. Hot air may be uniformly supplied through the plurality of flow nozzles 103. In order to supply the hot air evenly, the plurality of flow nozzles 103 may be replaced to allow hot air to be injected through the porous plate through the porous plate.

In addition, a raw material input conveyor 104 for dumping organic waste is installed on one side of the main body 102 so that the organic waste supplied through the raw material input conveyor 104 is supplied into the reactor 101. The raw material injection hole 105 is formed.

In addition, a flow yarn inlet 107 for supplying the flow yarn supplied from the flow yarn storage tank 106 to the inside of the reactor 101 is formed at the other side of the center portion of the body 102, and The other side of the lower side is formed with a flow yarn discharge port 110 for discharging the supplied flow yarn, the rear end of the flow yarn discharge port 110 is connected conveyor 111 for transferring the discharged flow yarn to the flow yarn storage tank 106 Is installed.

The plasma hot air blower 108 mixes the plasma hot air generated by itself and the exhaust gas supplied from the gas circulation unit 300 to mix the hot air mixed into the reactor 101 (plasma hot air and exhaust gas are mixed. Hot air).

Specifically, the plasma hot air blower 108 is formed in a rocket shape, the plasma torch 114 is provided at the inlet portion (left side of FIG. 2), the exhaust gas circulation duct 115 is connected to the middle portion thereof, and the outlet portion ( 2 is connected to the supply port 109.

On the other hand, the plasma torch 114 is composed of a cathode 116 and an anode 117, and when a high current of DC is applied between the cathode 116 and the anode 117 between the cathode 116 and the anode 117 Plasma flame is generated in this case, and when nitrogen, which is a reaction gas, is blown into the plasma torch 114, a nitrogen-based ultra high temperature plasma flame of about 1200 ° C. to 1500 ° C. is generated.

On the other hand, since the temperature of the reaction gas suitable for supplying the reactor 101 is about 500 ° C., it is mixed with the low temperature circulating exhaust gas supplied from the exhaust gas circulation duct 115 inside the plasma hot air fan 108 to 450 ° C. A reaction gas in the range of 550 ° C. is generated and supplied to the reactor 101.

Through the thermal decomposition unit 100 as described above, it is possible to thermally decompose organic waste such as sawdust, palm oil residues, grasses, agricultural residues, etc. supplied into the main body 102 of the reactor 101.

Next, the oil recovery unit 200 will be described.

As shown in FIG. 3, the oil recovery unit 200 includes a cyclone 201, a cooling condenser 202, and an electrostatic precipitator 204.

The cyclone 201 is a component for recovering char by separating the particulate matter by centrifugal force after accommodating the exhaust gas that is pyrolyzed and discharged from the pyrolysis unit 100, and has an outer wall having a double wall structure.

Between the double-wall structure of the cyclone 201 is supplied with the hot air for warmth supplied from the warm hot air supply unit 400, the inside of the reactor 101 by the warm hot air can be kept warm, Therefore, it is possible to prevent the biooil having a high viscosity from adhering to and sticking to the inner wall of the reactor 101.

In detail, an inlet for insulated hot air and an outlet for insulated hot air flow are formed at one point and another point of the outer wall of the double wall structure of the cyclone 201, respectively, and are supplied from the hot air supply unit 400. The hot air of about 150 ℃ to 400 ℃ to maintain the wall temperature of the cyclone 201 can be an average of 300 ℃.

Centrifuged 촤 is collected and collected at the center lower portion of the cyclone 201, and exhaust gas containing bio-oil is supplied to the cooling condenser 202 through the upper portion of the cyclone 201.

The cooling condenser 202 is connected to a rear end of the cyclone 201 to recover bio-oil through cooling and condensation of the exhaust gas that is separably treated from the cyclone 201 and cooling condensation. The bio oil is recovered through.

For example, the cooling condenser 202 may be configured such that one or two or more are connected in series, and the biooil condensed through the cooling condenser 202 is stored in a separate oil storage tank (not shown). Can be.

On the other hand, the condensation of the biooil in the cooling condenser 202 may be achieved by spraying the bio-oil recovered in the oil storage tank through the injection nozzle 203 installed on the cooling condenser 202, the initial operation Since there is no biooil recovered from the cooling condenser 202, it is preferable to use paraffin oil or oil similar in physical properties to biocondensate as the condensate until the biooil is recovered to a certain amount.

The electrostatic precipitator 204 is connected to the rear end of the cooling condenser 202 to recover the biooil on the fine particles that are not recovered from the cooling condenser 202, to recover the biooil through the electrostatic precipitating method do.

Bio-oil contained in the gas is almost collected in the cooling condenser 202, but in the exhaust gas discharged from the cooling condenser 202, the bio-oil on the microparticles, which are not condensed and fly again, remain. One or two or more units are provided in series at the rear end of the cooling condenser 202 to collect oil.

On the other hand, the outer wall of the electrostatic precipitator 204 is formed of a double partition wall structure, the heat insulating hot air supply unit 400 supplies the hot air for insulating between the double partition walls of the electrostatic precipitator 204 to the electrostatic precipitator 204 It is configured to insulate the interior of the.

In detail, an inlet for insulated hot air and an outlet for inflowing the warmed hot air are formed at one point and the other point of the outer wall of the double partition wall structure of the electrostatic precipitator 204, respectively. The hot air supplied from about 150 ° C. to 400 ° C. maintains the wall temperature of the cyclone 201 to be 300 ° C. on average.

On the other hand, the electrostatic precipitator 204 may be any one of a flat plate-type electrostatic precipitator having a flat plate or a cylindrical electrostatic precipitator having a cylindrical plate, but to increase the mist collecting efficiency of the droplet state contained in the exhaust gas, a cylindrical electrostatic precipitator. It is preferable to use a flat type electrostatic precipitator for stable operation, and it is preferable to configure the cylindrical electrostatic precipitator and the flat type electrostatic precipitator in order to achieve both mist collection efficiency and stable operation.

Through the oil recovery unit 200 as described above, it is possible to recover the bio-oil contained in the exhaust gas supplied from the pyrolysis unit 100, in particular, fine contained in the exhaust gas through the electrostatic precipitator 204 Since the biooil on the particles is collected and recovered, the biooil microparticles are prevented from mechanical failure due to attachment and fixation inside the components, and the recovery rate of the biooil can be maximized.

Next, the gas circulation unit 300 will be described.

As shown in FIG. 4, the gas circulation unit 300 includes a reservoir 301 and a blower 302.

The storage tank 301 is a component for storing the exhaust gas discharged from the oil recovery unit 200, the blower 302 for supplying the exhaust gas stored in the storage tank 301 to the pyrolysis unit 100. Component.

Specifically, the blower 302 allows the exhaust gas stored in the reservoir 301 to be supplied into the plasma hot air blower 108 through the circulation duct 115 connected to the middle portion of the plasma hot air blower 108.

On the other hand, the reservoir 301 and the exhaust gas circulation duct 115 is preferably configured in a closed structure, because the outside air is introduced into the exhaust gas while the oxygen is not included, and the organic waste is thermally decomposed Char and bio-oil are recovered from the generated reactants, but the remainder is gasified to be included in the exhaust gas, and if the operation continues, the amount of exhaust gas gradually increases, so that the gas vent valve 303 is attached to the upper portion of the exhaust gas storage tank 301. It is preferable to allow some of the exhaust gas to be discharged manually or automatically.

Through the gas circulation unit 300 as described above, the bio-oil is recovered, and the low temperature exhaust gas is supplied back to the plasma hot air fan 108 so that the temperature of the plasma hot air can be properly adjusted.

Next, the thermal insulation hot air supply unit 400 will be described.

The warm hot air supply unit 400, as shown in Figure 5, comprises a combustion burner 401 and a blower 402.

The combustion burner 401 is a component that generates warm heat through combustion using LNG or oil as fuel, and the blower 402 is a component that blows and supplies the warm heat.

Specifically, the blower 402 is blown so that hot air can be supplied through the inlet of the thermal hot air of the reactor 101, the cyclone 201, the electrostatic precipitator 204.

Through the thermal insulation hot air supply unit 400 as described above, the wall temperature of the reactor 101, the cyclone 201, the electrostatic precipitator 204 can be maintained to be an average of 300 ℃, through which the bio-oil It can flow along the inner wall of the to increase the collection efficiency, it is possible to increase the internal cleaning cycle of the recovery facility.

Although the present invention has been described with reference to the accompanying drawings, it will be apparent to those skilled in the art that many different and obvious modifications are possible without departing from the scope of the invention from this description. Therefore, the scope of the invention should be construed by the claims described to include many such variations.

Claims

A pyrolysis unit for pyrolysing the organic wastes supplied using plasma hot air;

An oil recovery unit for separating and cooling the biooil contained in the exhaust gas discharged from the pyrolysis unit to recover the oil;

A gas circulation unit configured to circulate the exhaust gas discharged from the oil recovery unit to the pyrolysis unit; And

And a thermal hot air supply unit for supplying hot air for warming the thermal decomposition unit or the gas circulation unit.
The method of claim 1,

The pyrolysis unit,

A reactor configured to receive the organic waste and discharge the pyrolyzed exhaust gas to the oil recovery unit; And

And a plasma hot air fan for supplying hot air mixed into the reactor by mixing plasma hot air and exhaust gas supplied from the gas circulation unit.
The method of claim 2,

The reactor is formed of a double partition structure, wherein the heat insulating hot air supply unit to maintain the interior of the reactor by supplying hot air for keeping warm between the double partition walls of the reactor.
The method of claim 2,

The inner bottom of the reactor is provided with a plurality of flow nozzles or porous plates connected to the plasma hot air, and the mixed hot air is supplied to the inside of the reactor through the plurality of flow nozzles or porous plates. Device.
The method of claim 2,

The plasma hot air is generated by using nitrogen gas as a carrier gas.
The method of claim 2,

The hot air mixed with the plasma hot air and the exhaust gas supplied from the gas circulation unit is 450 ℃ to 550 ℃ bio oil recovery apparatus, characterized in that.
The method of claim 1,

The oil recovery unit,

A cyclone that receives the exhaust gas discharged from the pyrolysis unit and then performs a separation process;

A cooling condenser connected to a rear end of the cyclone to recover bio-oil through cooling and condensing the exhaust gas which is separated from the fan in the cyclone; And

And an electrostatic precipitator connected to a rear end of the cooling condenser to recover the biooil on the fine particles not recovered from the cooling condenser by an electrostatic precipitating method.
The method of claim 7, wherein

The cyclone and the electrostatic precipitator is formed in a double partition structure, wherein the thermal insulation hot wind supply unit to supply the hot air for thermal insulation between the double partition of the cyclone and the electrostatic precipitator, characterized in that to warm the interior of the cyclone and the electrostatic precipitator Oil recovery unit.
The method of claim 7, wherein

The electrostatic precipitator is a bio-oil recovery apparatus, characterized in that one or two or more are configured in series by using any one of a flat type electrostatic precipitator or a cylindrical electrostatic precipitator.
The method of claim 1,

The gas circulation unit,

A storage tank for storing the exhaust gas discharged from the oil recovery unit; And

And a blower for supplying the exhaust gas stored in the storage tank to the pyrolysis unit.
The method of claim 1,

The thermal insulation hot wind supply unit,

A combustion burner that generates heat; And

And a blower for blowing and supplying the warm heat.