WO2016075912A1

WO2016075912A1 - Method of pyrolysis of organic substances, method for producing pyrolysate of organic substances, and furnace for pyrolysis of organic substances

Info

Publication number: WO2016075912A1
Application number: PCT/JP2015/005557
Authority: WO
Inventors: 石井　純; ▲高▼木　克彦; 浩一百野; 稔淺沼
Original assignee: Ｊｆｅスチール株式会社
Priority date: 2014-11-11
Filing date: 2015-11-05
Publication date: 2016-05-19
Also published as: JPWO2016075912A1; TW201623390A

Abstract

In the present invention, particulate organic substances are blown diagonally downward into a lower region of a bed 3 through an inlet 2 provided on a lower side face of a pyrolysis furnace 1. This action allows the following effects to be achieved in combination: (i) the bed material in the lower region of the bed will become fluidized such that the bed material throughout the entire bed will function sufficiently, since bed material with large particle sizes can be prevented from settling in the lower regions of the bed; (ii) the particulate organic substances blown into the lower region of the bed will move (float) from the lower region of the bed to an upper region and in the process can cause a pyrolytic gasification reaction, allowing the entire bed to be effectively used for the pyrolytic gasification reaction; and (iii) the particulate organic substances will be loaded into the bed at high speed at a constant solid/gas ratio so that a feedstock loading inlet will not be blocked up for example by molten resins. The above effects allow organic substances such as resins to be efficiently pyrolyzed.

Description

Organic substance thermal decomposition method, organic substance thermal decomposition product manufacturing method, and organic substance thermal decomposition furnace

The present invention relates to a method and a pyrolysis furnace for efficiently pyrolyzing an organic substance such as a resin to produce a high calorific gas or oil.

In recent years, the energy problem has become a major issue, and as an approach to solve this problem, a method of effectively utilizing the latent heat of an organic substance is considered. In particular, resin waste such as waste plastics has a high calorific value, and may be effectively used as a fuel to replace fossil fuels. However, since resin waste has poor thermal conductivity and takes a long time to increase its temperature, the combustion speed is very slow, and it is difficult to use it as a fuel substitute if it remains solid. Therefore, a method has been considered in which resins are decomposed and converted into gas or oil before being used as fuel.

For example, Patent Document 1 discloses a method of thermally decomposing car shredder dust containing plastic with a kiln. In this method, molten slag generated in a combustion melting furnace is introduced into the kiln together with car shredder dust in order to prevent adhesion and solidification of molten plastic inside the kiln.
However, the kiln method used in the method of Patent Document 1 has low heat transfer efficiency, and it is necessary to reduce the solid space factor in the furnace in order to stably convey the raw material. Further, since slag is contained in the solid, the space factor of the shredder dust itself is further lowered, and there is a problem that the apparatus must be enlarged to obtain a sufficient processing speed.

On the other hand, in Patent Document 2, an organic substance is gasified by pyrolysis using a fluidized bed reactor, the carbon adhering to the fluidized medium is combusted in a combustion furnace, and the fluidized medium is returned to the fluidized bed as a heating medium. The process is shown. In the method of Patent Document 2, by using a fluidized bed, the heat transfer rate to an organic substance is improved, and gasification can be efficiently performed at a low temperature.

JP 2012-237549 A International Publication No. 2008/107928

However, in the method of Patent Document 2, when resins such as waste plastics are subjected to thermal decomposition, the entire fluidized bed cannot be efficiently used for the thermal decomposition of the resins. It has been found that it is difficult to perform efficient thermal decomposition of resins due to problems such as easy clogging.
Therefore, the object of the present invention is to solve the above-mentioned problems of the prior art, and use a fluidized bed type pyrolysis furnace, and a pyrolysis method capable of efficiently pyrolyzing organic substances such as resins, It is in providing the manufacturing method and pyrolysis furnace of a pyrolysis product.

As a result of detailed investigations on problems in the case of thermally decomposing resins in a fluidized bed type pyrolysis furnace, the present inventors have found that the factors that hinder efficient pyrolysis treatment are as follows. I found out.
(I) The fluidized media used in the fluidized bed have a certain particle size distribution (particle size width), although there are some differences depending on the type, and among them, fluidized media with a large particle size have poor fluidity and fluidity. It tends to stay in the lower region of the layer. For this reason, the fluidized medium does not function sufficiently as the whole fluidized bed.
(Ii) Resins have a specific gravity smaller than that of fluid media (usually silica sand etc.), and are easily floated and separated on the upper part of the fluidized bed after being charged. The lower part of the fluidized bed is not effectively used for the pyrolysis gasification reaction.
(Iii) The raw material charging port of the fluidized bed is likely to be clogged with molten resins.

The present inventors have studied a method for solving the above-mentioned problems and enabling efficient thermal decomposition treatment of resins. As a result, the resins to be pyrolyzed are granulated by granulation, pulverization, classification, etc., and these granular resins are fed to the lower region of the fluidized bed through the blowing port provided in the fluidized bed type pyrolysis furnace. We found that the method of blowing obliquely downward is effective. That is, according to this method, the following effects (1) to (3) can be obtained with respect to the problems (i) to (iii) described above, so that efficient thermal decomposition treatment of resins can be achieved. I found it possible.

(1) By blowing granular resins obliquely downward to the lower region of the fluidized bed, the fluidized state of the fluidized medium in the lower region of the fluidized bed is activated, and the flow having a large particle size in the lower region of the fluidized bed It is possible to prevent the medium from staying. For this reason, a fluid medium fully functions in the fluidized bed as a whole, and the heat transfer rate to the resins and the reaction rate of thermal decomposition can be greatly improved.
(2) Since the granular resins blown into the lower region of the fluidized bed move (float) from the lower region to the upper region of the fluidized bed, a pyrolytic gasification reaction can occur in the process, The entire region of the fluidized bed can be used effectively for the pyrolysis gasification reaction, and the gasification rate is greatly improved.
(3) Since the resins are charged into the fluidized bed at a constant solid-gas ratio at high speed, there is almost no risk that the raw material charging port will be clogged by the molten resins.

The present invention has been made on the basis of such knowledge and has the following gist.
[1] A method for thermally decomposing granular organic substances in a fluidized bed type pyrolysis furnace,
An organic material characterized in that the granular organic material to be pyrolyzed is blown obliquely downward into the lower region of the fluidized bed (3) through the blow port (2) provided on the lower side surface of the pyrolysis furnace (1). Method for pyrolysis of substances.
[2] In the thermal decomposition method of [1], the blowing direction of the granular organic material to the lower region of the fluidized bed (3) has an inclination angle of 25 to 45 ° downward with respect to the horizontal direction. Method for thermal decomposition of organic substances.

[3] In the thermal decomposition method of [1] or [2] above, part or all of the carrier gas for the granular organic substance is composed of a gas that becomes a gasifying agent for the granular organic substance in the fluidized bed (3). A method for thermally decomposing an organic substance.
[4] In the thermal decomposition method of any one of [1] to [3] above, the inner diameter D of the blowing port (2) provided in the pyrolysis furnace and the blowing port (2) from the lower end position of the fluidized bed (3) The organic material pyrolysis method is characterized in that the height h to the lower end position and the stationary height L of the fluid medium satisfy the following formula (1):
3D ≦ h ≦ L / 3 (1)
[5] The method for pyrolyzing an organic substance according to any one of [1] to [4] above, wherein the fluidized medium is dust generated from a steel mill.
[6] A method of pyrolyzing a granular organic substance in a fluidized bed type pyrolysis furnace to produce a pyrolysis product of the organic substance,
An organic material characterized in that the granular organic material to be pyrolyzed is blown obliquely downward into the lower region of the fluidized bed (3) through the blow port (2) provided on the lower side surface of the pyrolysis furnace (1). A method for producing a thermal decomposition product of a substance.
[7] In the production method of [6], the blowing direction of the granular organic material into the lower region of the fluidized bed (3) has an inclination angle of 25 to 45 ° downward with respect to the horizontal direction. A method for producing a thermal decomposition product of an organic substance.
[8] In the production method of [6] or [7] above, a part or all of the carrier gas for the granular organic substance is composed of a gas that becomes a gasifying agent for the granular organic substance in the fluidized bed (3). A method for producing a thermal decomposition product of an organic substance.
[9] In the manufacturing method of any one of [6] to [8] above, the inner diameter D of the blowing port (2) provided in the pyrolysis furnace and the flow port (3) from the lower end position of the blowing port (2) A method for producing a thermal decomposition product of an organic substance, wherein the height h to the lower end position and the stationary height L of the fluid medium satisfy the following formula (1):
3D ≦ h ≦ L / 3 (1)
[10] The method for producing a pyrolysis product of an organic substance according to any one of the above [6] to [9], wherein the fluidized medium is dust generated from a steel mill.
[11] A fluidized bed type pyrolysis furnace for pyrolyzing organic substances,
An organic substance pyrolysis furnace characterized by having an inlet (2) for injecting granular organic substance obliquely downward into a lower region of a fluidized bed formed in the furnace on a lower side surface of the furnace body.
[12] In the pyrolysis furnace of [11] above, the blowing direction of the granular organic material from the blowing port (2) to the lower region of the fluidized bed has an inclination angle of 25 to 45 ° downward with respect to the horizontal direction. An organic material pyrolysis furnace characterized by that.
[13] In the pyrolysis furnace of [11] or [12] above, a blowing pipe (8) is connected to the blowing port (2), and the blowing pipe (8) is used for gas transportation of particulate organic substances. A pyrolysis furnace for organic substances, characterized in that a supply pipe (9) is connected.
[14] In the pyrolysis furnace according to any one of [11] to [13], the inner diameter D of the blowing port (2) and the height h from the lower end position of the fluidized bed to the lower end position of the blowing port (2); The pyrolysis furnace for organic substances, wherein the stationary height L of the fluid medium satisfies the following formula (1):
3D ≦ h ≦ L / 3 (1)

According to the present invention, in the pyrolysis of an organic substance using a fluidized bed type pyrolysis furnace, the following effects (1) to (3) can be obtained in combination, whereby organic substances such as resins can be obtained. Pyrolysis can be efficiently performed.
(1) By blowing granular organic material obliquely downward with respect to the lower region of the fluidized bed, the fluidized state of the fluidized medium in the lower region of the fluidized bed is activated, and the flow having a large particle size in the lower region of the fluidized bed It is possible to prevent the medium from staying. For this reason, the fluidized medium functions sufficiently in the entire fluidized bed, and the heat transfer rate to the organic substance and the reaction rate of thermal decomposition can be greatly improved.
(2) Since the granular organic material blown into the lower region of the fluidized bed moves (floats) from the lower region to the upper region of the fluidized bed, a pyrolysis gasification reaction can occur in the process. The entire region of the fluidized bed can be used effectively for the pyrolysis gasification reaction, and the gasification rate is greatly improved.
(3) Since the granular organic material is charged into the fluidized bed at a constant solid-gas ratio at high speed, there is almost no risk that the raw material charging port will be clogged with molten resins.

FIG. 1 is an explanatory view showing an example of a fluidized bed type pyrolysis furnace used in the present invention and an embodiment of the method of the present invention using the same. FIG. 2 is a partially enlarged view of a lower region of the pyrolysis furnace of FIG. FIG. 3 is an explanatory diagram showing an outline of the fluidized bed gasification test apparatus used in the examples.

In the present invention, there is no particular restriction on the organic substance (solid) to be thermally decomposed, but a high molecular weight organic substance is suitable, for example, resins (usually waste plastic), biomass, etc. One or more of these can be targeted.
Examples of resins include polyolefins such as PE (Poly Ethylene) and PP (Polypropylene), thermoplastic polyesters such as PA (Polyamide) and PET (Poly Ethylene Terephthalate), elastomers such as PS (Poly Styrene), Examples thereof include, but are not limited to, thermosetting resins, synthetic rubbers and foamed polystyrene.
Examples of biomass include, but are not limited to, sewage sludge, paper, wood (for example, construction waste wood, packaging / transport waste wood, thinned wood, etc.).
These organic substances are used in a granular form for gas conveyance and blowing into the fluidized bed. In order to granulate the organic substance, pretreatment such as granulation, pulverization and classification is appropriately performed.

FIG. 1 is an explanatory view showing an example of a pyrolysis furnace used in the present invention and an embodiment of the method of the present invention using the same, and FIG. 2 is a partially enlarged view of a lower region of the pyrolysis furnace of FIG. 1 is a fluidized bed type pyrolysis furnace, and 3 is a fluidized bed.
In this pyrolysis furnace 1, a flowing gas (gasification agent) is introduced into the wind box portion 6 below the dispersion plate 5 through the gas supply pipe 4, and the flowing gas is blown out from the dispersion plate 5, whereby the dispersion plate 5. A fluidized bed 3 made of a fluidized medium is formed above the substrate. The organic substance put into the pyrolysis furnace 1 is pyrolyzed in the fluidized bed 3 to become a gas product. After the gas containing the gas product is discharged through the discharge pipe 7, the fluid medium and the ash content of the organic substance scattered in the gas are collected by a dust collector (not shown).
The lower side surface of the pyrolysis furnace 1 is provided with a blowing port 2 for blowing the gas-carrying granular organic substance into the furnace. In the present invention, the gas-carrying granular material is fed through the blowing port 2. The organic material is blown obliquely downward with respect to the lower region of the fluidized bed 3.

Hereinafter, the principle of the present invention will be described by taking as an example the case where the granular organic material to be thermally decomposed is a resin. Resins are basically low in specific gravity, and therefore easily float when charged into the fluidized bed 3. Therefore, the present inventors have thought that by supplying resins to the lower region of the fluidized bed 3, it is possible to advance the reaction efficiently during the ascent process. However, since the lower region of the fluidized bed 3 needs to be equal to or higher than the thermal decomposition temperature of the resin, it is difficult to apply a normal charging method using a feeder or the like because the possibility of clogging at the charging port is high. Therefore, in the present invention, granular resins are blown into the lower region of the fluidized bed 3 with the carrier gas. Since the blown granular resin moves (floats) from the lower region to the upper region of the fluidized bed 3, a pyrolysis gasification reaction can be caused in the process, and thus the entire region of the fluidized bed 3 is heated. It can be used effectively for cracking gasification reaction. In the fluidized bed 3, the fluidized medium is basically in a fluidized state and has a high porosity, so that the granular resin can be blown at a lower blowing gas flow rate than when blown into the packed bed.

Furthermore, the fluidized medium used in the fluidized bed has a certain particle size distribution (width of the particle size), although there are some differences depending on the type of the fluidized medium. However, in the present invention, the granular resin is inclined obliquely downward with respect to the lower region of the fluidized bed 3. By blowing, the fluidized state of the fluidized medium in the lower region of the fluidized bed 3 is activated, and it is possible to prevent the fluidized medium having a large particle size from staying in the lower region of the fluidized bed 3. For this reason, a fluid medium fully functions in the fluidized bed as a whole, and the heat transfer rate to the resins and the reaction rate of thermal decomposition can be greatly improved. In addition, for the problem that the raw material inlet of the fluidized bed is blocked by the molten resin, in the present invention, the resins are charged at a high rate into the fluidized bed at a constant solid-gas ratio. There is almost no fear that the raw material charging port (blowing port 2) is blocked by the melted resins.
As described above, in the present invention, it is possible to efficiently perform thermal decomposition of organic substances such as resins.

In FIG. 1, a blowing pipe 8 (blowing lance) is connected to the blowing port 2, and the particulate organic material that has been conveyed by the supply pipe 9 flows from the blowing port 2 through the blowing pipe 8. Blown into layer 3; Note that the blowing ports 2 may be provided at a plurality of locations in the furnace circumferential direction.
In the present invention, there is no particular limitation as long as the blowing angle (downward blowing angle) of the particulate organic material from the blowing port 2 is 0 degree (horizontal) or more. From the viewpoint of prevention of clogging, about 25 to 45 ° is preferable. That is, it is preferable that the blowing direction of the granular organic material has an inclination angle θ of 25 to 45 ° downward with respect to the horizontal direction. When the inclination angle θ is less than 25 °, the effect of blowing the granular organic material obliquely downward with respect to the lower region of the fluidized bed 3 is reduced, and the flow into the blowing pipe 8 is stopped when the blowing of the granular organic material is stopped. The medium may easily enter, and the air inlet 2 and the air pipe 8 may be clogged. On the other hand, when the inclination angle θ exceeds 45 °, the flow rate of the carrier gas at the tip of the blowing pipe 8 (blowing port 2) is lowered, and the carrying property of the granular organic substance is likely to be lowered.

Although there is no restriction | limiting in particular in the height position which provides the blowing inlet 2, In order to blow a granular organic substance diagonally downward with respect to the lower area | region of the fluidized bed 3 through the blowing outlet 2, the internal diameter D of the blowing inlet 2 and The height h from the lower end position of the fluidized bed 3 to the lower end position of the inlet 2 and the stationary height L of the fluidized medium (the height L of the fluidized medium in a stationary state where no fluid gas is supplied) are as follows ( 1) It is preferable to satisfy the formula.
3D ≦ h ≦ L / 3 (1)
When h> L / 3, the position of the blowing port 2 is too high, so that it becomes difficult to blow the particulate organic material into the lower region of the fluidized bed 3. On the other hand, when 3D> h, since the position of the blowing port 2 is too low, the blowing gas reaches the gas dispersion portion at the lower end of the fluidized bed, and the blowing gas may flow backward to the cracked gas inlet.

There is no particular limitation on the type of fluidized gas (gasifying agent) supplied to the fluidized bed 3, and a known fluidized gas (gasifying agent), for example, a mixed gas (generated in a metallurgical furnace) disclosed in JP 2014-37524 A By adding excess water vapor to the exhaust gas containing carbon monoxide and causing the shift reaction to occur, a mixed gas containing hydrogen and carbon dioxide gas generated by the shift reaction and water vapor not consumed in the shift reaction) Can be used.
The kind of carrier gas (injection gas) for the particulate organic substance is not particularly limited, and for example, a gas containing one or more of N ₂ , CO _{2 and the} like can be used. From the viewpoint of accelerating the thermal decomposition reaction of the granular organic substance in the fluidized bed 3, a part or all of the carrier gas is a gas (reacts with the organic substance that becomes a gasifying agent for the particulate organic substance in the fluidized bed 3). And a gas that promotes the decomposition thereof. As the gas to be such a gasifying agent include CO _2. Accordingly, the carrier gas is preferably a CO ₂ -containing gas, particularly a gas having a relatively high CO ₂ concentration. For example, combustion exhaust gas from a blast furnace hot stove contains about 25% of CO ₂ and is suitable as a carrier gas.

The carrier gas preferably has a gas temperature of 50 ° C. or lower and does not contain oxygen in order to ensure the transportability of the organic substance.
The carrier gas needs to have a flow velocity so that a space called a raceway is created in the fluidized bed 3 by blowing. If the raceway is not possible, the particulate organic substance cannot enter the fluidized bed, and clogging may occur in the blowing pipe 8. Since the limit flow velocity for generating the raceway is greatly influenced by the inner diameter of the air inlet 2, the particle size, shape, porosity, and flow state of the fluid medium, it is preferable to obtain in advance by a model experiment that allows internal observation.

The fluid medium is preferably a metal powder that also functions as an organic substance decomposition catalyst. As such a granular material, a known Ni-based reforming catalyst, Ni-based hydrogenation catalyst, or the like can be used. Dusts generated in each step of the steel mill because of its high catalytic activity because it contains a lot of iron, it is suitable as a fluid medium because it is fine particles, and it is available in large quantities and is inexpensive. That is, ironworks generated dust is preferable. A typical example of dust generated in a steel mill includes, but is not limited to, converter dust. Among the dust generated in steelworks, converter dust is most suitable as a fluid medium having a catalytic function because of its high iron component ratio and very high thermal conductivity. Converter dust is iron-containing dust generated in a steelmaking process performed using a converter. Examples of the steel making process include, but are not limited to, a dephosphorization process, a decarburization process, and a stainless steel refining process.

Using a fluidized bed gasification test apparatus shown in FIG. 3, a gasification test was conducted in which waste plastic particles were gasified at 600 ° C. The diameter of the fluidized bed 3 (fluidized bed gasifier) was 66 mm, and converter dust was used as the fluidized medium. The height L of the fluid medium at rest was 198 mm. As a flowing gas (gasifying agent), a mixed gas of H ₂ , N ₂ , CO ₂ , and H ₂ O was supplied at 4 L / min. As the granular waste plastics, those obtained by freezing and pulverizing waste plastic particles molded to about 6 mmφ × 15 mm by a ring die molding machine and sieving them with a sieve having an opening of 2.0 mm were used. The average diameter in the fixed direction was about 1 mm.

In the example of the present invention, the waste plastic particles put into the hopper 10a are cut out by the table feeder 11a (cutting speed 300 g / h), and the waste plastic particles cut out by this fixed amount are composed of CO ₂ : 25 vol% and N ₂ : 75 vol%. A blow-in port provided by a carrier gas (a carrier gas supplied from the

gas cylinders

12 and 13 through a gas supply pipe 14) and provided at a height h of 30 mm from the lower end (distribution plate 5) of the fluidized bed 3 2 (inner diameter D: 10 mm) was blown into the fluidized bed 3 at an inclination angle θ of 30 °.

In order to compare with the case where waste plastic is supplied from the upper part of the apparatus, a hopper 10b is also provided on the upper part of the fluidized bed 3, so that waste plastic particles can be quantitatively cut out by the table feeder 11b and supplied from the upper part of the fluidized bed 3. . In the comparative example, the waste plastic particles put in the hopper 10b were cut out by the table feeder 11b (cutting speed 300 g / h), and the waste plastic particles cut out by this fixed amount were dropped into the fluidized bed 3 and charged.
The gas in the fluidized bed 3 is taken out through the discharge pipe 7 and cooled by the gas cooler 15 (18 is a gas trap), then the gas flow rate is continuously measured by the mass flow meter 16, and further the gas is chromatographed by the gas chromatography 17. The composition was measured.

Table 1 shows the results of calculating the lower gas calorific value and the gasification rate from the gas generation amount and the gas composition for the inventive example and the comparative example. The gasification rate is obtained by the following equation, and the “gasification raw material” is waste plastic particles.
F = (G × C2) / (M × C1) × 100
Where F: Gasification rate (%)
M: Gasification raw material supply amount (kg / h)
G: Amount of generated gas (kg / h)
C1: Carbon concentration in gasification raw material (%)
C2: Carbon concentration in product gas (%)

In the example of the present invention in which waste plastic particles were blown into the lower region of the fluidized bed, it was possible to continuously supply the waste plastic particles without any problem, but in the comparative example in which waste plastic particles were fed from the upper part of the fluidized bed, the temperature near the supply port was As the melted waste plastic closed the supply port, the vicinity of the waste plastic supply port of the upper flange was cooled with a blower, enabling continuous supply.
In the comparative example, the calorific value of the product gas was 3870 kcal / Nm ³ and the gasification rate was 41%. However, in the inventive example, the calorific value and gasification rate of the product gas increased, and the calorific value was 4950 kcal / Nm ^3. The gasification rate was 68%.

DESCRIPTION OF SYMBOLS 1 Pyrolysis furnace 2 Blowing inlet 3 Fluidized bed 4 Gas supply pipe 5 Dispersion plate 6 Wind box part 7 Discharge pipe 8 Blow pipe 9 Supply pipe 10a Hopper 10b Hopper

11a Table feeder

11b Table feeder 12 Gas cylinder 13 Gas cylinder 14 Gas supply pipe 15 Gas Cooler 16 Mass Flow Meter 17 Gas Chromatography 18 Gas Trap

Claims

A method of thermally decomposing particulate organic substances in a fluidized bed type pyrolysis furnace,
An organic material characterized in that the granular organic material to be pyrolyzed is blown obliquely downward into the lower region of the fluidized bed (3) through the blow port (2) provided on the lower side surface of the pyrolysis furnace (1). Method for pyrolysis of substances.
2. The method for thermally decomposing an organic material according to claim 1, wherein the blowing direction of the granular organic material into the lower region of the fluidized bed (3) has an inclination angle of 25 to 45 ° downward with respect to the horizontal direction. .
The pyrolysis of the organic substance according to claim 1 or 2, characterized in that a part or all of the carrier gas for the particulate organic substance is composed of a gas that becomes a gasifying agent for the particulate organic substance in the fluidized bed (3). Method.
The inner diameter D of the blowing port (2) provided in the pyrolysis furnace, the height h from the lower end position of the fluidized bed (3) to the lower end position of the blowing port (2), and the stationary height L of the fluid medium are as follows ( The method for pyrolyzing an organic substance according to any one of claims 1 to 3, wherein the formula (1) is satisfied.
3D ≦ h ≦ L / 3 (1)
The method for thermally decomposing an organic substance according to any one of claims 1 to 4, wherein the fluid medium is dust generated from a steel mill.
A method of pyrolyzing a granular organic substance in a fluidized bed type pyrolysis furnace to produce a pyrolysis product of the organic substance,
An organic material characterized in that the granular organic material to be pyrolyzed is blown obliquely downward into the lower region of the fluidized bed (3) through the blow port (2) provided on the lower side surface of the pyrolysis furnace (1). A method for producing a thermal decomposition product of a substance.
The pyrolytic production of organic substances according to claim 6, characterized in that the blowing direction of the granular organic substances into the lower region of the fluidized bed (3) has an inclination angle of 25-45 ° downward with respect to the horizontal direction. Manufacturing method.
The pyrolysis of an organic substance according to claim 6 or 7, characterized in that part or all of the carrier gas for the granular organic substance comprises a gas that becomes a gasifying agent for the granular organic substance in the fluidized bed (3). Product manufacturing method.
The inner diameter D of the blowing port (2) provided in the pyrolysis furnace, the height h from the lower end position of the fluidized bed (3) to the lower end position of the blowing port (2), and the stationary height L of the fluid medium are as follows ( The method for producing a thermal decomposition product of an organic substance according to any one of claims 6 to 8, wherein the formula (1) is satisfied.
3D ≦ h ≦ L / 3 (1)
The method for producing a thermal decomposition product of an organic substance according to any one of claims 6 to 9, wherein the fluid medium is dust generated from a steel mill.
A fluidized bed type pyrolysis furnace for pyrolyzing organic substances,
An organic substance pyrolysis furnace characterized by having an inlet (2) for injecting granular organic substance obliquely downward into a lower region of a fluidized bed formed in the furnace on a lower side surface of the furnace body.
The organic substance according to claim 11, wherein the blowing direction of the granular organic substance from the blowing port (2) to the lower region of the fluidized bed has an inclination angle of 25 to 45 ° downward with respect to the horizontal direction. Pyrolysis furnace.
A blow pipe (8) is connected to the blow inlet (2), and a supply pipe (9) for gas transportation of particulate organic substances is connected to the blow pipe (8). A pyrolysis furnace for organic substances according to 11 or 12.
The inner diameter D of the blowing port (2), the height h from the lower end position of the fluidized bed to the lower end position of the blowing port (2), and the fluid medium stationary height L satisfy the following formula (1). The organic substance pyrolysis furnace according to any one of claims 11 to 13.
3D ≦ h ≦ L / 3 (1)