KR20180079148A - Torrefaction unification reactor for manufacturing bio-oil - Google Patents

Torrefaction unification reactor for manufacturing bio-oil Download PDF

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KR20180079148A
KR20180079148A KR1020170041852A KR20170041852A KR20180079148A KR 20180079148 A KR20180079148 A KR 20180079148A KR 1020170041852 A KR1020170041852 A KR 1020170041852A KR 20170041852 A KR20170041852 A KR 20170041852A KR 20180079148 A KR20180079148 A KR 20180079148A
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reactor
rotor
heat source
biomass
oil
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KR1020170041852A
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Korean (ko)
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KR101887028B1 (en
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이수민
정한섭
안병준
이재정
최돈하
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대한민국(산림청 국립산림과학원장)
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    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/24Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G31/00Refining of hydrocarbon oils in the absence of hydrogen, by methods not otherwise provided for
    • C10G31/06Refining of hydrocarbon oils in the absence of hydrogen, by methods not otherwise provided for by heating, cooling, or pressure treatment
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10Feedstock materials
    • C10G2300/1011Biomass
    • C10G2300/1014Biomass of vegetal origin
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40Characteristics of the process deviating from typical ways of processing
    • C10G2300/4037In-situ processes

Abstract

The present invention relates to a reactor comprising a reactor main body for generating and discharging a pyrolysis gas on a gaseous phase by rapid thermal decomposition reaction after thermal pretreatment of woody biomass put on the upper part, A rotor portion having a first rotor and a second rotor each having a structure in which a spiral screw is formed along an outer wall of a cylindrical body at an upper portion and a lower portion with respect to a longitudinal direction of the shaft, A first heat source for heating an upper portion of the reactor body to a first temperature range and a second heat source for heating a lower portion of the reactor body corresponding to the position of the second rotor to a second temperature range higher than the first temperature range, And a heat source, wherein, during rotation of the rotor part, the wood biomass is pivotally moved along the screw to lower the first heat source After the pre-treatment column to provide a one-piece pre-treatment reactor, for producing bio-oil that is rapid pyrolysis through the second heat source.
According to the present invention, heat pretreatment and rapid thermal decomposition reaction for woody biomass can be performed by one stop, and unlike conventional reactors, only woody biomass (wood chips) can be used without using sand as a heat transfer fluid medium There is an advantage that bio oil can be produced.

Description

[0001] The present invention relates to a reactor for preparing bio-oil,

The present invention relates to a pre-treatment integrated reactor for producing bio-oil, and more particularly, to a pre-treatment integrated reactor for producing bio-oil using a rapid thermal decomposition reaction.

Recently, renewable fuels such as bio-diesel and bio-ethanol have attracted attention as a part of establishing a sustainable energy system around the world. Research on biofuels has been actively pursued with the aim of reducing dependence on petroleum, reducing greenhouse gases, revitalizing agriculture, and expanding the supply of renewable energy.

Accordingly, it is expected that the production of biofuels such as bio-oil, which is an energy resource to replace conventional petrochemical fuels, and the related market size will be further increased. In addition, the demand for processes for producing biofuel products with improved quality and performance through the reforming of biofuels such as biodiesel and bio-oil is also rapidly increasing.

Bio-oil can be used in boilers, furnaces, engines and power generation turbines to replace oil fuels or diesel. In addition, food seasonings, resins, hydroacetaldehyde, agrochemicals, fertilizers and exhaust gas control agents can be extracted from bio-oils.

Bio-oil is a blackish brown liquid produced by applying pyrolysis technology that decomposes a sample at high temperature to biomass. It is also called pyrolysis oil, and about 70% of the total product is produced through pyrolysis process .

Generally, bio-oil (pyrolysis oil) can be produced by using a fast pyrolysis process in which the biomass is rapidly heated to about 500 ° C under oxygen-free conditions. The bio-oil produced can be used as fuel for power generation, industrial use, or transportation.

Since the rapid thermal cracking process requires a reaction within a very short time at a high temperature, it is necessary to increase the thermal decomposition efficiency through the uniform heat transfer during the rapid heating and to prevent the problem that the yield is lowered due to the subsequent decomposition occurring after the thermal decomposition reaction do.

In order to improve the reactivity of the rapid pyrolysis process using biomass, it is necessary to pulverize the sample particles. In order to produce bio-oil, it is necessary to perform the reaction within a short period of time. The smaller the size of the raw material introduced through the pulverization process of the sample particles, the quicker and more efficient reaction can be obtained.

Typically, separate pulverization processes are required to pulverize the biomass. This is generally referred to as a preprocessing process. This preprocessing process involves a problem of cost loss. In addition, the rapid pyrolysis process technology has not yet been stabilized globally, and there is no commercialized plant that has proven technically superior.

1 shows a conventional circulating fluidized bed reactor. Circulating Fluidized Bed (CFB) is a representative technology related to rapid pyrolysis of bio-oil.

The circulating fluidized bed is a mixed fluidized bed which is mixed vigorously by gas. When the fluid is operated at a high speed, the particles are scattered and re-injected in the reactor, such as particle collection by cyclone and particle re- . Also, the reactor utilizing this is called a circulating fluidized bed reactor.

Briefly described with reference to FIG. 1, a biomass such as wood powder is injected into a reactor through a feeder. When the biomass introduced into the reactor is subjected to a rapid thermal decomposition reaction, pyrolysis gas, which is a byproduct thereof, is produced. All these reactions take place under anaerobic conditions (usually in the presence of nitrogen gas). When the pyrolysis gas discharged from the reactor is rapidly cooled, a liquid bio-oil can be produced.

Among the byproducts due to the rapid thermal decomposition reaction, there is also a solid phase char, which can be separated or discharged separately. The hot sand used in the reactor is a heat transfer fluid medium, which induces a rapid and uniform pyrolysis reaction to increase the pyrolysis efficiency of the biomass.

Such a circulating fluidized bed reactor is characterized in that the residence time of the char (residual char residue such as char) after the pyrolysis reaction is almost the same as the residence time of the bubbles and the gas. Although it is suitable for large capacity treatment, And the collected bio-oil has a disadvantage that it contains a large amount of char. In general, biocha is close to impurities, so an attempt should be made to reduce it.

2 is a view for explaining conventional modification and direct modification of conventional bio oil. BACKGROUND ART [0002] Conventionally, a modification technique for a bio-oil is mainly related to a bio-oil modification (normal modification) in a ' liquid ' state, which is characterized by an increase in process complexity and a high energy demand. The liquid phase bio oil obtained by ordinary modification maintains an unstable state at room temperature and is strongly acidic, so it can corrode the reactor and the water content is generally high.

Also, unlike ordinary reforming, a direct reforming method for reforming bio oil through contact with a catalyst layer immediately on a 'gas' has been known as a complementary method of the prior art. However, There are very few examples of direct modification of bio-oils.

The technology to be a background of the present invention is disclosed in Korean Patent No. 10-1524456 (published on June 1, 2015).

It is an object of the present invention to provide a pre-treatment integrated reactor for manufacturing bio-oil which can manufacture bio-oil without using sand only, and does not require a pulverization process of biomass, thereby reducing manufacturing cost.

The present invention relates to a reactor comprising a reactor main body for generating and discharging a pyrolysis gas on a gaseous phase by rapid thermal decomposition reaction after thermal pretreatment of woody biomass put on the upper part, A rotor portion having a first rotor and a second rotor each having a structure in which a spiral screw is formed along an outer wall of a cylindrical body at an upper portion and a lower portion with respect to a longitudinal direction of the shaft, A first heat source for heating an upper portion of the reactor body to a first temperature range and a second heat source for heating a lower portion of the reactor body corresponding to the position of the second rotor to a second temperature range higher than the first temperature range, And a heat source, wherein, during rotation of the rotor part, the wood biomass is pivotally moved along the screw to lower the first heat source After the pre-treatment column to provide a one-piece pre-treatment reactor, for producing bio-oil that is rapid pyrolysis through the second heat source.

Here, the wood-based biomass is subjected to the heat pretreatment by the first heat source while being lowered by turning along the screw of the first rotor, and then, while descending by turning along the screw of the second rotor, The above-mentioned rapid pyrolysis can be performed.

Also, the first temperature range may be 250 to 300 ° C, and the second temperature range may be 450 to 550 ° C.

The first heat source and the second heat source may be respectively provided in an upper portion and a lower portion of an inner wall of a case for accommodating the reactor body so as to heat the corresponding portions on the outer side of the reactor body.

The space between the outer wall of each rotor and the inner wall of the reactor body may gradually become narrower toward the lower side at each of the positions of the first and second rotors.

In addition, the wood biomass is lowered while being rotated along the screw to widen the areas of the heat treatment and the pyrolysis reaction, and the woody biomass is pulverized as it goes downward due to the gradually narrowing space The size of the woody biomass can be reduced.

In addition, the diameter of the reactor body becomes narrower toward the lower side, and the diameters of the first and second rotors may be constant in the vertical direction.

According to the pre-treatment integrated reactor for producing bio oil according to the present invention, heat pretreatment and rapid thermal decomposition reaction for woody biomass can be performed with one-stop, and unlike conventional reactors, There is an advantage that bio-oil can be produced using only biomass (wood chips).

In addition, since the present invention can simultaneously perform rapid thermal decomposition and size control of wood chips in a reactor, a particle pretreatment process such as crushing of a wood chip is not required in advance, thereby simplifying the production process of bio oil, Can be greatly reduced.

1 shows a conventional circulating fluidized bed reactor.
2 is a view for explaining conventional modification and direct modification of conventional bio oil.
FIG. 3 is a view showing the construction of a pre-treatment integrated reactor for producing bio oil according to an embodiment of the present invention.
FIG. 4 is a diagram illustrating a bio-oil production system including the reactor of FIG. 3. FIG.
5 is a view illustrating a case in which a reactor according to an embodiment of the present invention is accommodated.

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings so that those skilled in the art can easily carry out the present invention.

The present invention relates to a pre-treatment integrated reactor for producing bio oil, and it is possible to manufacture a bio-oil by only biomass without sand, unlike the conventional method, and does not require a pulverization process of biomass, Heat pretreatment and rapid thermal decomposition reaction of the pre-treatment integrated reactor can be performed by one-stop.

FIG. 3 is a view showing the construction of a pre-treatment integrated reactor for producing bio oil according to an embodiment of the present invention, and FIG. 4 is a view illustrating a bio oil production system including the reactor of FIG.

Referring to FIGS. 3 and 4, a pre-treatment integrated reactor 100 according to an embodiment of the present invention includes a reactor body 110, a rotor 120, and first and second heat sources (not shown).

The pre-treatment integrated reactor 100 according to the embodiment of the present invention produces a vaporized gas (pyrolysis gas) by heat-pretreatment and rapid pyrolysis of the biomass introduced therein, . The pyrolysis gas is produced as a liquid bio-oil after cooling process.

The reactor main body 110 is formed by heat pretreatment (roasting) the woody biomass (ex, wood chips) injected through the upper part at a first high temperature environment (ex. 250 to 300 ° C) Deg.] C to generate and discharge pyrolysis gas on the gaseous phase. The pyrolysis gas is then rapidly cooled and produced as a liquid bio-oil. The composition of the high-temperature environment may be formed by a separate heat source for heating the reactor 100 itself outside the reactor 100. The heat source will be described in detail later.

In the embodiment of the present invention, the woody biomass is introduced into the inlet 111 formed in the upper part of the reactor body 110. The introduced biomass falls into a space between the inner wall of the main body 110 and the rotor 120 and is pyrolyzed and pyrolyzed by torrefaction according to the composition of the high temperature environment, .

The biomass injected into the reactor body 110 is lowered while being rotated according to the rotation of the rotor part 120. Due to the structure of the internal space and the rotation of the rotor, the particle size gradually decreases, and at the same time, It generates pyrolysis gas, which is a by-product of the gas phase, and a by-product (impurity such as char or char), which is a by-product of the solid phase.

The heavier of the bio-car is discharged through the lower outlet 113 and the lighter weight escapes with the pyrolysis gas through the upper outlet 112. 4, the pyrolysis gas may be discharged through the upper outlet 112 and then be produced as bio-oil through the cyclone 200 and the cooler 300 in sequence.

The cyclone 200 separates the pyrolysis gas and the bio-car by dropping the bio-car that has flowed along with the gas down to remove impurities as much as possible from the gas. The cooler 300 rapidly cools the pyrolysis gas passing through the cyclone 200 to produce a liquid bio-oil. It is to be understood that the process at the rear end of the reactor 100 is merely an example and that various known processes can be used.

In general, the rapid pyrolysis process is carried out under anaerobic conditions (ex. Nitrogen gas environment). To this end, nitrogen gas (fluidizing gas) may be injected into the reactor body 110, and a separate gas inlet may be formed at a predetermined position.

As described above, bio-oil production using rapid thermal decomposition of woody biomass corresponds to a known technique, so that a more detailed explanation of the principle is omitted. Next, the structure of the rotor portion 120 will be described in more detail.

The rotor 120 is rotatable about a vertical axis while being coupled to the reactor body 110 and includes a first rotor 121 and a second rotor 122 at the upper and lower portions in the longitudinal direction on the vertical axis Respectively.

Each of the rotors 121 and 122 has a structure in which helical screws 121a and 122a are formed along the outer wall of the rotating cylindrical body. The structure for rotatably coupling the rotor in the main body can use various known methods, so a detailed description of the coupling structure is omitted.

The first rotor 121 corresponds to the heat pretreatment reaction unit and the second rotor 122 corresponds to the rapid thermal decomposition reaction unit. That is, the rotor unit 120 has a structure in which the upper portion of the heat pretreatment reaction unit and the lower portion of the rapid thermal decomposition reaction unit are integrated with respect to the longitudinal direction. Heat pretreatment refers to the process of roasting or semi-carbonization of the input biomass, and the rapid pyrolysis reaction refers to the pyrolysis process of the biomass.

That is, the space between the outer wall of the first rotor 121 and the inner wall of the main body 110 is a space for heat pretreatment (roasting) the introduced woody biomass in the first temperature range, The space between the inner walls of the main body 110 means a space for rapidly pyrolyzing the woody biomass to be thermally treated and dropped to a second temperature range higher than the first temperature range.

The screws 121a and 122a of the rotors 121 and 122 have the effect of forming a stepped spiral along the outer circumferential surface of the rotors 121 and 122, respectively. Therefore, when rotating the rotors 121 and 122, the woody biomass (wood chip) swirls along the screw while descending, thereby widening the reaction area (contact area).

The screws 121 formed on the surfaces of the rotating rotors 121 and 122 increase the fluidity to draw the wood biomass (wood chips) down. As the screws 121 themselves have steps like the steps, It stops at a certain part and then descends downward to increase reaction efficiency.

The first heat source (not shown) heats the upper portion of the reactor body 110 corresponding to the position of the first rotor 121 to a first temperature range (ex, 250 to 300 ° C). The second heat source (not shown) heats the lower portion of the reactor body 110 corresponding to the position of the second rotor 122 to a second temperature range (ex, 450 to 550 ° C) higher than the first temperature range.

That is, the portion of the first rotor 121 at the upper portion is 250 to 300 占 폚 and the portion of the second rotor 122 at the lower portion is at 450 to 300 占 폚 with respect to the center portion of the reactor main body 110 in the up- 550 C < / RTI >

According to this structure, the wood biomass (wood chip) can be thermally treated through the first heat source while descending along the screw during rotation of the rotor unit 120, and then thermally decomposed rapidly through the second heat source. That is, the woody biomass can be semi-carbonized by the first heat source while descending and pivoting along the screw 121a of the first rotor 121, and thereafter, along the screw 122a of the second rotor 122 And can be rapidly pyrolyzed to the second heat source while being turned and lowered.

As a result, in the portion of the first rotor 121, the wood chip is thermally pretreated (semi-carbonized) while roasting at a temperature of 250 to 300 ° C and heated at 450 to 550 ° C higher than that of the lower portion of the second rotor 122 It can be pyrolyzed at high temperature while being finely crushed.

Here, the space between the outer wall of each of the rotors 121 and 122 and the inner wall of the reactor main body 110 at the positions of the first and second rotors 121 and 122 may be gradually narrowed toward the lower side. For example, as shown in FIG. 3, the diameter of the reactor body 110 becomes narrower toward the lower side, and the diameters of the first and second rotors 121 and 122 may be uniform in the up-and-down direction.

Here, the diameter of each of the rotors 121 and 122 may mean the diameter of the section corresponding to the portion where the actual screw is formed. For example, the portion where the screw is not formed, that is, the upper end portion or the lower end portion of each rotor has a shape in which the diameter is gradually widened or narrowed so as to facilitate the introduction of the sample. However, .

Since the space between the outer wall of the rotors 121 and 122 and the inner wall of the reactor body 110 becomes gradually narrower toward the lower side, the woody biomass is pulverized as it goes downward, so that the size of the woody biomass can be reduced . In other words, the input woody biomass can be broken down into a smaller size while the biomass is pivoted in a gradually narrowing space, and the pyrolysis efficiency is increased as the particles are smaller.

That is, in the embodiment of the present invention, by using the structure of the rotor and the screw rotating in the reactor, the woody biomass is lowered while rotating along the screw to widen the areas of the heat treatment and the pyrolysis reaction, And the woody biomass is pulverized as it goes downward due to the gradually narrowed space, thereby reducing the size of the woody biomass.

In the case of the conventional rapid thermal decomposition reactor, the wood chip is finely pulverized and pulverized (in the form of a wood powder) is put into a pyrolysis reaction without using the wood chip as it is. (Diameter of ~ 3 cm) can be supplied as it is. Therefore, it is not necessary to perform particle pretreatment (pulverization) of the wood chips before the injection, and the process can be simplified. Of course, it is obvious that the embodiment of the present invention can produce bio oil even by using already powdered wood powder.

As described above, according to the embodiment of the present invention, it is possible to maximize the reaction efficiency and the reactivity of the sample in the thermal decomposition reaction in the vertical direction on the internal structure of the reactor main body 110 and maximize the contact surface between the sample (biomass) Can be maximized. Therefore, unlike the conventional method, it is possible to manufacture bio-oil using only woody biomass without using sand (heat transfer fluid medium) used for increasing the reaction efficiency, and the size of the woody biomass as the raw material does not need to be small The size limitation of the sample particles is small, and the manufacturing cost of the bio-oil can be largely reduced.

Meanwhile, in the embodiment of the present invention, the first and second heat sources, which respectively heat the upper and lower portions of the reactor body 110, may be embedded in a case (case) housing the reactor 100.

5 is a view illustrating a case in which a reactor according to an embodiment of the present invention is accommodated. The reactor 100 is mounted in a separate case C provided with two heat sources H1 and H2.

In the case C, the internal environment is set to a high-temperature environment according to the operation of the first and second heat sources H1 and H2 to heat the upper and lower spaces of the reactor 100 to an individual temperature, Heat pretreatment and rapid thermal decomposition of the biomass injected therein are performed.

The surface and the interior of the reactor 100 are heated to a high temperature by a heat source, thereby pyrolyzing the reacted sample. In addition to the reactor 100, the cyclone 200 may be installed in the case C as well. However, the cooler 300 is installed outside the case C for cooling efficiency.

The first heat source H1 and the second heat source H2 are respectively provided in the upper portion and the lower portion of the inner wall of the case C so as to heat the corresponding portions on the outer side of the reactor body 110 respectively. The first heat source H1 heats the upper portion of the reactor main body 110 to a first temperature range (250 to 300 ° C) and the second heat source H2 heats the lower portion except the upper portion to a second temperature range (450 to 550 < 0 > C). Thus, the wood chip can be heat-pretreated while being heated and roasted at the upper part, and can be pyrolysed to a higher temperature at a higher temperature while brittle at a higher temperature in the lower part.

The first and second heat sources H1 and H2 are installed along the inner surface of the case C as shown in the drawing and may have a heat wire shape heated by electricity or the like. In addition, it may be provided in a zigzag form closely in the up and down direction for heating efficiency. Of course, there may be more various embodiments of the structure and shape of the heat source. In this case, the temperature environment (the ambient temperature of the reactor) inside the case C can be divided into the upper and lower regions to form different temperature ranges (upper portion is 250 to 300 ° C, lower portion is 450 to 550 ° C) 100 may be heated to different temperature ranges.

According to the pre-treatment integrated reactor for producing bio oil according to the present invention, it is possible to heat pretreatment and rapid thermal decomposition reaction of woody biomass to one-stop, and, unlike conventional reactors, There is an advantage that bio-oil can be produced using only wood-based biomass (wood chip) without use.

In addition, according to the present invention, rapid thermal decomposition and size control of the wood chips can be performed in the reactor, and thus a particle pretreatment process such as crushing of a wood chip is not required in advance, The manufacturing cost can be greatly reduced.

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

100: reactor 110: reactor body
111: inlet 112: upper outlet
113: Lower outlet 120:
121: first rotor 122: second rotor
121a, 122a: Screw 200: Cyclone
300: cooler

Claims (7)

  1. A reactor main body for subjecting the woody biomass supplied to the upper part to rapid pyrolysis reaction after heat pretreatment to generate and discharge pyrolysis gas on the gas phase;
    A first rotor rotatable about a vertical axis in a state of being coupled to the reactor main body and having a spiral screw formed along the outer wall of the cylindrical body at upper and lower portions thereof in the longitudinal direction on the vertical axis, A rotor portion having a rotor;
    A first heat source for heating an upper portion of the reactor body corresponding to the position of the first rotor to a first temperature range; And
    And a second heat source for heating a lower portion of the reactor body corresponding to the position of the second rotor to a second temperature range higher than the first temperature range,
    Wherein the wood biomass is thermally treated through the first heat source while being lowered by turning the screw along the screw, and then pyrolyzed rapidly through the second heat source.
  2. The method according to claim 1,
    The wood-based biomass is thermally pretreated by the first heat source while descending along the screw of the first rotor, and is then heated by the second heat source while descending by turning along the screw of the second rotor The pre-treatment integrated reactor for producing the bio-oil which is pyrolyzed rapidly.
  3. The method according to claim 1 or 2,
    Wherein the first temperature range is 250 to 300 ° C, and the second temperature range is 450 to 550 ° C.
  4. The method according to claim 1,
    Wherein the first heat source and the second heat source comprise:
    Wherein the reactor body is provided at an upper portion and a lower portion of an inner wall of a case for accommodating the reactor body, respectively, so as to heat the corresponding portion outside the reactor body.
  5. The method according to claim 1,
    Wherein the space between the outer wall of each rotor and the inner wall of the reactor body is gradually narrowed toward the lower side at each of the positions of the first and second rotors.
  6. The method of claim 5,
    The wood-based biomass is lowered while being rotated along the screw to widen the areas of the thermal treatment and the pyrolysis reaction, and the wood-based biomass is pulverized as it goes downward due to the gradually narrowing space, Pre-treatment integrated reactor for bio-oil production that reduces the size of biomass.
  7. The method of claim 5,
    Wherein the diameter of the reactor body is narrower toward the lower side and the diameters of the first and second rotors are constant in the up and down direction.
KR1020170041852A 2016-12-30 2017-03-31 Torrefaction unification reactor for manufacturing bio-oil KR101887028B1 (en)

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