JP6904388B2 - Pyrolysis method of organic substances - Google Patents

Description

The present invention relates to a method for thermally decomposing an organic substance such as waste plastic to thermally decompose it into a gaseous substance or the like.

In recent years, recycling of waste plastics and biomass has been promoted, but some of them are still incinerated. However, the incineration process _{has a high environmental load such as CO 2} generation, and there is also a problem of thermal damage to the incinerator, so establishment of chemical recycling technology is required.
Among the chemical recycling technologies, various technologies for converting organic substances into gas fuels and liquid fuels have been studied conventionally, centering on waste plastics. For example, Patent Document 1 describes that the technology was generated in a gasification melting furnace. Using exhaust gas containing carbon monoxide and hydrogen, excess water vapor is added to this exhaust gas to cause a shift reaction, and the shift reaction production gas is brought into contact with the organic substance to reform the organic substance. A method for reducing the molecular weight (pyrolysis) is disclosed.

Further, in Patent Document 2, in a fluidized bed type reactor in which a mixed gas obtained by a shift reaction between a carbon monoxide-containing gas and water vapor is used as a fluidized gas, the mixed gas is brought into contact with an organic substance. , A method of modifying an organic substance to reduce the molecular weight (pyrolysis) is disclosed. Further, in the same document, as one of the forms of charging an organic substance into a reactor, an organic substance such as waste plastic is compression-molded into granules, and the organic substance molded body is charged from the upper part of the reactor. It is stated that by adopting such a charging form, clogging troubles due to organic substances in the supply system (piping, etc.) can be prevented, and the organic substances can be smoothly supplied to the reactor.

Japanese Patent No. 5679088 JP-A-2017-436666

However, when the present inventors conducted an experiment to modify and reduce the molecular weight of an organic substance according to the methods of Patent Documents 1 and 2, it was found that there are the following problems. That is, the methods of Patent Documents 1 and 2 have the advantages of being easy to carry out and reducing the equipment cost because the reaction is carried out under relatively mild conditions in terms of equipment, but the obtained thermal decomposition product is obtained. Has a problem that the proportion of oily substances is high and the yield of gaseous substances is low. When considering transportation to the place of use, oily substances have poor handleability, such as the need for heat retention in order to maintain viscosity. Therefore, in the thermal decomposition of organic substances, it is desired to increase the yield of gaseous substances as much as possible.

Therefore, an object of the present invention is to solve the above-mentioned problems of the prior art, and to obtain a pyrolysis product by thermally decomposing an organic substance such as waste plastic or biomass, it is a gas product (gas at room temperature). It is an object of the present invention to provide a method for thermally decomposing an organic substance, which can increase the yield of a thermal decomposition product).

As a result of repeated studies to solve the above problems, the present inventors have compression-molded an organic substance such as waste plastic as shown in Patent Document 2, and this organic substance molded body is used in a fluidized bed reactor. In the method of charging from the upper part, the gasification reaction of the organic substance efficiently occurs by making the density of the molded body of the organic substance molded body and the bulk density of the fluidized bed in the reactor substantially equal to each other. It turned out that it could be solved. That is, by optimizing the molded body density of the organic substance molded body and the bulk density of the fluidized medium in the reactor so as to be substantially equal to each other, the organic substance molded body can be efficiently dispersed in the fluidized bed. As a result, the contact between the organic substance molded body and the fluidized medium is promoted, and as a result, the heat transfer and the gasification reaction are promoted, and the yield of the gas product (pyrolysis product which is a gas at room temperature) is increased. It turned out. Further, in order to make the density of the molded body of the organic substance molded body and the bulk density of the fluid medium in the reactor substantially equal to each other, when the organic substance molded body is obtained, a density adjusting agent (generally speaking) is added to the organic substance. It has been found that it is preferable to adjust the molded body density of the organic substance molded body by adding (a substance having a higher density than the organic substance) and performing compression molding. It was also found that in that case, there are suitable conditions for the shape and size of the density adjusting agent.

The present invention has been made based on such findings, and the gist of the present invention is as follows.
[1] An organic substance is mixed in a fluidized bed type reactor in which a mixed gas (g) containing at least hydrogen and carbon dioxide is introduced as a fluidized gas and a fluidized bed is formed by a powdery and granular fluidized medium (f). It is a method of thermally decomposing by contacting with gas (g).
In performing thermal decomposition of an organic substance by supplying an organic substance molded product (x) obtained by compression molding an organic substance into granules or lumps from the upper part of a reactor.
An organic substance characterized in that the molded body density ρx of the organic substance molded body (x) and the bulk density ρf of the fluidized medium (f) satisfy ρx / ρf = 0.99 to 1.10 during steady operation. Pyrolysis method.
[2] In the thermal decomposition method of the above [1], the organic substance molded product (x) is thermally decomposed by adding a density adjusting agent (a) to the organic substance and compression molding. Method.

[3] In the thermal decomposition method of the above [2], the organic substance molded product (x) obtained by adding a non-volatile density adjusting agent (a) to the organic substance and compression molding is supplied to the reactor to thermally decompose the organic substance. In doing
During steady operation, a part of the fluid medium (f) in the reactor (however, a fluid medium partially composed of the density modifier (a)) is extracted and discharged to the outside of the system, and a new fluid medium for the fluid medium is used. A method for thermally decomposing an organic substance, which comprises supplying powders and granules to a reactor.
[4] In the thermal decomposition method of [3] above, a part of the fluidized medium (f) in the reactor is extracted to the outside of the reactor, and a part of the extracted fluidized medium (f) is discharged to the outside of the system. , A method for thermally decomposing an organic substance, which comprises refluxing a fluid medium (f) that has not been discharged to the outside of the system to a reactor.

[5] The method for thermally decomposing an organic substance according to the above-mentioned [3] or [4], wherein the bulk density ρf of the fluidized medium (f) is calculated by the following equation (1).
ρf = {ρa × (Wp × A) + ρm × Wout-ρm × (Wp × A)} / Wout… (1)
However, ρf: bulk density of fluid medium (f) (g / cm ³ )
ρa: Bulk density of density modifier (a) (g / cm ³ )
Wp: Supply rate (kg / h) of the organic substance molded product (x) into the reactor
A: Mass fraction (-) of the density modifier (a) in the organic substance molded product (x)
Wout: Emission of the fluid medium (f) in the reactor to the outside of the system (kg / h)
^{ρm: Bulk density (g / cm 3} ) of new powder and granules for the fluid medium supplied to the reactor

[6] In any of the above [2] to [5], when the aspect ratio of the density adjuster (a) is [maximum width in the direction orthogonal to the major axis / major axis], the density. A method for thermally decomposing an organic substance, wherein the adjusting agent (a) has an average aspect ratio of 1 to 3.5.
[7] In any of the above [2] to [6], the average maximum width of the organic substance molded body (x) in the direction orthogonal to its major axis is D, and the density adjuster (a). A method for thermally decomposing an organic substance, characterized in that D / d is 3 to 300, where d is the average major axis of.
[8] A method for thermally decomposing an organic substance according to any one of the above [1] to [7], wherein the organic substance contains at least one selected from plastic and biomass.
[9] In any of the above [1] to [8], the organic substance molded product (x) is prepared by adding a density adjusting agent (a) to the organic substance, mixing the mixture, and using an extrusion molding machine. A method for thermally decomposing an organic substance, which is characterized by being compression-molded into a columnar shape.

According to the present invention, when an organic substance such as waste plastic is thermally decomposed to obtain a thermal decomposition product, the yield of a gas product (thermal decomposition product which is a gas at room temperature) can be dramatically increased. it can.

When silica sand is used as the powder for the fluid medium (f) and iron oxide powder, alumina powder, and graphite powder are used as the density adjusting agent (a) to be blended in the organic substance molded body (x), the organic substance is used. The relationship between the molded body density ρx of the molded body (x) and the blending amount of the density adjusting agent (a) in the organic substance molded body (x), and the conditions of the present invention (density ratio ρx / ρf = 0.99-1. A graph showing the range of the molded body density ρx of the organic substance molded body (x) for satisfying 10). Explanatory drawing schematically showing the flow of the thermal decomposition method of an organic substance by this invention and one Embodiment of a thermal decomposition equipment. Explanatory drawing schematically showing the flow of the thermal decomposition method of an organic substance according to the present invention and other embodiments of a thermal decomposition equipment. Explanatory drawing schematically showing the flow of the thermal decomposition method of an organic substance according to the present invention and other embodiments of a thermal decomposition equipment. In the present invention, since the density adjusting agent (a) blended in the organic substance molded body (x) is a non-volatile substance, a part of the fluidized medium (f) forming the fluidized bed is extracted and removed from the system. A drawing showing a mass balance of a fluidized medium and a density modifier in a reactor when discharging and supplying (replenishing) new powders and granules for a fluidized bed to the fluidized bed. In a method of thermally decomposing an organic substance by supplying an organic substance molded body (x) from the upper part of the reactor using a fluidized bed type reactor, the molded body density ρx of the organic substance molded body (x) and a fluidized medium. (F) A graph showing the relationship between the ratio ρx / ρf of the bulk density ρf and the amount of gas products produced in the reactor. Explanatory drawing which shows typically the ring die type extrusion molding machine for obtaining the organic substance molded article (x) used in this invention, and the implementation state of compression molding of the material using this.

In the method of the present invention, an organic substance is introduced in a fluidized bed type reactor in which a mixed gas (g) containing at least hydrogen and carbon dioxide is introduced as a fluidized gas and a fluidized bed is formed by a powdery and granular fluidized medium (f). Is a method of thermally decomposing by contacting with a mixed gas (g), and the heat of the organic substance is supplied by supplying the organic substance molded body (x) obtained by compression-molding the organic substance into granules or lumps from the upper part of the reactor. In performing the decomposition, the ratio ρx / ρf of the compact density ρx of the organic substance molded body (x) and the bulk density ρf of the fluidized bed (f) during steady operation (hereinafter, for convenience of explanation, simply “density ratio ρx /” By setting ρf ”) to 0.99 to 1.10, the thermal decomposition of the organic substance is promoted.
Here, the molded body density of the organic substance molded body (x) is calculated by dividing the mass of one molded body (particle) by the volume of the molded body (particle).
In the following description, among the pyrolysis products of organic substances, the pyrolysis products that are liquid at room temperature are referred to as "oily substances", and the pyrolysis products that are gas at room temperature are referred to as "gaseous substances".

The fluidized bed type reactor used for the thermal decomposition of an organic substance in the present invention is excellent in heat conduction, so that the organic substance can be thermally decomposed at a high thermal decomposition rate. In this reactor, when a mixed gas (g) is introduced as a fluidized gas, a fluidized bed is formed by a powdery and granular fluidized medium (f), and the mixed gas (g) is thermally decomposed of an organic substance. Used for.
As the mixed gas (g) containing at least hydrogen and carbon dioxide used for the thermal decomposition of the organic substance in the present invention, for example, a gas generated in a gasification melting furnace or an ironmaking process, or a modified gas thereof is used. Can be used. That is, if the gas generated in the gasification melting furnace or the steelmaking process satisfies the predetermined gas composition, it can be used as it is, but for example, a gas rich in carbon monoxide and low in hydrogen such as a linz-Donaw gas is used. In this case, excess water vapor may be added to carry out the shift reaction. As a result, a mixed gas containing hydrogen originally contained, carbon dioxide and hydrogen generated in the shift reaction, and water vapor not consumed in the shift reaction is generated, and the gas composition suitable for thermal decomposition of organic substances is obtained. can do.

Here, the gasification melting furnace is a furnace facility that thermally decomposes waste by heating it in a low oxygen state, burns or recovers the gas generated by this thermal decomposition, and melts ash and incombustibles at a high temperature. There is a method in which thermal decomposition and melting are performed integrally, and a method in which thermal decomposition and melting are performed separately. Specifically, gasification reforming method (for example, thermoselect method), shaft furnace method (for example, coke bed type, oxygen type, plasma type, etc.), kiln furnace method, fluidized bed method, semi-dry distillation / negative pressure There is a combustion method and so on. In the present invention, the exhaust gas generated in any type of gasification and melting furnace may be used, or a mixture of two or more types of exhaust gas may be used. The exhaust gas generated in the gasification melting furnace includes, for example, an exhaust gas containing carbon dioxide and hydrogen having a carbon dioxide concentration of 20 to 60 vol% and a hydrogen concentration of 60 to 20 vol%, and an exhaust gas having a carbon monoxide concentration of 10 to 50 vol%. Exhaust gas containing carbon monoxide and hydrogen having a hydrogen concentration of 50 to 10 vol% can be mentioned, and a mixed gas (g) for thermal decomposition of an organic substance after reforming these exhaust gases as they are or to a predetermined gas composition. ) Can be used.
In addition, linz-Donaw gas and blast furnace gas in the steelmaking process are also usable gases, and in the case of gas lacking hydrogen as described above, hydrogen is generated by the so-called shift reaction, so the hydrogen concentration is about 10 vol%. Even so, the composition is suitable for the mixed gas (g) of the present invention.

It is generally known that high molecular weight organic substances such as waste plastics start thermal decomposition when heated at 300 to 400 ° C. or higher, but at this time, they become lighter and heavier. When hydrogen coexists during thermal decomposition, the hydrogenation reaction to the hydrocarbon species and the hydrocracking reaction proceed, which is effective in suppressing heaviness and reducing the molecular weight. However, there is a problem that high temperature is required for hydrocracking and hydrogen consumption is high.
On the other hand, steam reforming and carbon dioxide reforming can be regarded as the oxidation of hydrocarbons by oxygen in H 2 _O and CO ₂ molecules, low molecular weight carbonaceous product inhibition achieved with a small amount of hydrogen addition it can. Further, steam reforming and carbon dioxide reforming are characterized in that the reaction temperature decreases as the carbon chain of the organic molecule to be reformed becomes longer. By combining these hydrogenation, hydrocracking, steam reforming, and carbon dioxide reforming, it is possible to efficiently promote the reduction of molecular weight of organic substances even at a relatively low reaction temperature.
Therefore, the mixed gas (g) used in the present invention preferably contains water vapor in addition to hydrogen and carbon dioxide.

When an organic substance used in the present invention a hydrocarbon (C m _{H n),} the above reaction can be represented by the reaction formula shown below.
Hydrogenation: C _m H _n + H ₂ → C _m H _{n + 2}
Hydrogenation decomposition: C _m H _n + H ₂ → C _p H _q + C _r H _s (m = p + r, n + 2 = q + s)
Steam reforming: C _m H _n + H ₂ O → C _m-1 H _n-2 + CO + 2H ₂
Carbon dioxide reforming: C _m H _n + CO ₂ → C _m-1 H _n-2 + 2CO + H ₂
However, hydrogenation also includes the following CO and CO ₂ metanational reactions.
CO + 3H ₂ → CH ₄ + H ₂ O, CO ₂ + 4H ₂ → CH ₄ + 2H ₂ O
Even with H ₂ generated in the steam reforming and carbon dioxide reforming, hydrogenation and hydrogenolysis of the proceeds.

Further, if water vapor is added to the gas containing carbon monoxide and the shift reaction of (1) below is carried out, CO can be _{converted into H 2} and CO ₂ , so that it is suitable as the mixed gas (g) used in the present invention. It will be something like that.
CO + H ₂ O → H ₂ + CO ₂ … (1)
Since some exhaust gas generated in gasification and melting furnaces and gas generated in steelworks contain a large amount of carbon monoxide, according to this method, thermal decomposition is performed by controlling the shift reaction between carbon monoxide and steam. A mixed gas suitable for use can be obtained.

In particular, when steam is excessively added to the exhaust gas containing carbon monoxide, steam remains in the produced gas, so that the steam reforming reaction can be utilized. That is, by appropriately controlling the reaction rate of the shift reaction, the concentrations of water vapor, hydrogen, and carbon dioxide in the gas can be controlled to obtain a mixed gas (g) having a gas composition suitable for thermal decomposition of organic substances. ..
The reaction rate of the shift reaction can be controlled by adjusting the residence time in the shift reactor. For example, in order to shorten the residence time, it is common to reduce the shift reactor length or the catalyst filling amount, in which case the shift reactor length and the catalyst filling amount are almost in equilibrium. It may be about 1/2 to 1/4 of the case where the reaction is allowed to proceed.

The exhaust gas generated from the thermoselect type gasification melting furnace usually contains about _{20 to 40 vol% of CO, 40 to 20 vol% of CO 2} , and 20 to 40 vol% of H 2. Therefore, by simply mixing an appropriate amount of water vapor with the exhaust gas containing carbon dioxide and hydrogen, CO: 15 to 20 vol%, CO ₂ : 10 to 35 vol%, H ₂ : 15 to 20 vol%, H ₂ O: The composition is about 20 to 50 vol%, which is suitable as a mixed gas (g) for thermal decomposition of organic substances.
Further, the blast furnace gas and the linz-Donaw gas generated in the steelworks can be reformed to a gas composition suitable for thermal decomposition of organic substances by utilizing the same shift reaction.
When the gas generated by the shift reaction as described above is used as the mixed gas (g), if the organic substance to be charged into the reactor contains water, water vapor is generated in the reactor. It is preferable to adjust the excess ratio of water vapor added in the shift reaction in consideration of the amount.

In the present invention, the organic substance to be thermally decomposed is not particularly limited, but since the compression-molded organic substance is charged into the reactor, the solid organic substance is the main component. Among them, high molecular weight organic substances are preferable, and examples thereof include plastics (usually waste plastics), biomass, oil-impregnated sludge, coal, and the like, and one or more of these can be targeted. Further, a liquid organic substance such as waste oil may be mixed with one or more of these organic substances. Further, from the viewpoint of compression molding to form a molded product, it is preferable that the organic substance contains at least one selected from plastic and biomass.
There are no particular restrictions on the types of target plastics, but in the case of waste plastics, for example, industrial waste systems, plastics subject to the Containers and Packaging Recycling Law, etc. can be mentioned. More specifically, polyolefins such as PE and PP, thermoplastic polyesters such as PA and PET, elastomers such as PS, thermosetting resins, synthetic rubbers and styrofoam can be mentioned.

Biomass includes, for example, sewage sludge, paper, wood (construction waste, thinned wood, etc.), agricultural waste (for example, paddy husks, tea husks, coffee husks (slag), etc.), as well as waste solid fuel (RDF). Processed biomass such as, but is not limited to these. Since biomass usually contains a large amount of water, it is preferable to dry it in advance from the viewpoint of energy efficiency.
In addition, in the case of biomass containing alkali metals such as sodium and potassium at a relatively high concentration, alkali metals may precipitate in the reactor, so the alkali metals should be eluted in advance by a method such as washing with water. Is preferable.

In the present invention, the above-mentioned organic substance is compression-molded into granules or lumps in advance to obtain an organic substance molded product (x), and the organic substance molded product (x) is supplied from the upper part of the reactor to form the organic substance. Perform thermal decomposition. The reason why the organic substance molded product (x) is used in this way is to prevent clogging trouble due to the organic substance in the supply system (piping, etc.) and to smoothly supply the organic substance to the fluidized bed reactor. Preferred molding conditions, molding methods and the like of this organic substance will be described in detail later.
Here, in the operation mode in which the organic substance molded body (x) is charged from above the fluidized bed type reactor in which the fluidized bed is formed by the powdery granular fluidized medium (f), the organic substance is gasified. As a result of examining the operating conditions capable of efficiently causing the reaction, the compact density ρx of the organic substance molded body (x) and the bulk density ρf of the fluidized bed (f) are almost the same during steady operation. Specifically, it was found that the density ratio needs to be about ρx / ρf = 0.99 to 1.10.

When the organic substance molded body (x) is charged on the upper part of the fluidized bed formed in the reactor, the molded body density ρx of the organic substance molded body (x) is smaller than the bulk density ρf of the fluidized medium (f). If it is too much, it is considered that the organic substance molded body (x) segregates on the upper part of the fluidized bed. The advantage of the fluidized bed is that the reactant (in this case, the organic material molded body) and the fluidized medium (powder) forming the fluidized bed frequently come into contact with each other, and therefore the reaction proceeds. When the substance is segregated on the upper part of the fluidized bed, the reaction promotion by contact with the fluidized bed and the heat exchange between the fluidized medium, which is also a heat transfer medium, and the reactant are also limited. As a result, it is not possible to efficiently generate a gasification reaction of an organic substance by taking advantage of the fluidized bed. On the contrary, if the molded body density ρx of the organic substance molded body (x) is too large with respect to the bulk density ρf of the fluidized medium (f), it is considered that the organic substance molded body (x) segregates in the lower part of the fluidized bed. Similarly, in the same case, the gasification reaction of the organic substance cannot be efficiently caused by taking advantage of the fluidized bed.

Specifically, when the density ratio ρx / ρf is less than 0.90 and more than 1.10, the gasification reaction of the organic substance cannot be efficiently caused for the above-mentioned reason. On the other hand, by adjusting the density ratio ρx / ρf in the range of 0.99 to 1.10, the organic substance molded body (x) can be efficiently dispersed in the fluidized bed, whereby the organic substance can be efficiently dispersed. The contact between the molded body (x) and the fluidized bed (f) is promoted, and as a result, the heat transfer and gasification reaction are promoted, and the yield of the gas product (pyrolysis product which is a gas at room temperature) is increased. Can be done.
When the density ratio ρx / ρf is in the range of 0.99 to 1.10, one or both of the molded body density ρx of the organic substance molded body (x) and the bulk density ρf of the fluidized medium (f) are adjusted. However, as will be described later, in general, the molded body density ρx of the organic substance molded body (x) obtained by compression molding only the organic substance such as plastic is considerably smaller than the bulk density ρf of the fluidized medium (f). Since the density ratio ρx / ρf <0.90, the density ρx of the organic material molded body (x) can be adjusted by blending a high-density substance as a density adjusting agent with the organic material molded body (x). I thought about doing (increasing). As a result of specific studies, when an organic substance molded body (x) is obtained, a substance having a higher density than the organic substance (for example, metal oxide) as a density adjusting agent (a) with respect to the organic substance such as plastic. It was found that the density ρx of the organic substance molded body (x) can be easily adjusted by performing compression molding by adding powders such as.

なお、かさ密度には、測定方法の違いにより「固めかさ密度（タップかさ密度）」と「ゆるみかさ密度」があるが、本発明では、流動層を形成する流動媒体（f）のかさ密度であることを考慮して、後者の「ゆるみかさ密度」とする。その測定方法は、ＪＩＳ Ｋ７３６５（プラスチック−規定漏斗から注ぐことのできる材料の見掛け密度の求め方）に準拠したものとする。 As the fluidized medium constituting the fluidized bed in the reactor, powder or granular material having a particle size of about 100 μm is generally used. Table 1 shows an example of a substance (powder and granules sized to a particle size of about 100 μm) used for the flow medium (f) and its bulk density. However, as the flow medium, not only the ones exemplified in Table 1 but also any kind of powders and granules that are stable and fluidize at high temperature can be used.

There are two types of bulk density, "solid bulk density (tap bulk density)" and "loose bulk density", depending on the measurement method. In the present invention, the bulk density of the flow medium (f) forming the fluidized layer is used. Considering this, the latter "looseness density" is used. The measuring method shall be in accordance with JIS K7365 (Plastic-How to determine the apparent density of the material that can be poured from the specified funnel).

Table 2 shows the densities (true densities) of various plastics and the densities of waste plastic molded bodies (those separated as plastic waste and compression-molded by a ring die type extrusion molding machine described later). Here, the molded body density is calculated by dividing the mass of one molded body (particle) by the volume of the molded body (particle). As shown in Table 2, the densities of plastics differ depending on the type, and the waste plastic molded product is obtained by compression molding plastic waste in which various plastics are mixed.

From Tables 1 and 2, it can be seen that the molded body density of the waste plastic molded body is generally smaller than the bulk density of the powder and granules for the fluid medium. In addition, biomass, which is a typical organic substance along with plastic, generally has a lower density than plastic, and therefore, molding of a molded product obtained by compression molding the biomass or a molded product obtained by compression molding a mixture of biomass and waste plastic. The body density is also generally considered to be smaller than the bulk density of the powder or granules for the fluid medium. Therefore, when obtaining the organic substance molded body (x), a substance having a higher density than the organic substance (for example, powder such as a metal oxide) as a density adjusting agent (a) with respect to the organic substance such as plastic or biomass). The density ratio ρx / ρf can be adjusted in the range of 0.99 to 1.10 by adjusting the density ρx of the organic substance molded body (x) to be higher by performing compression molding. In this case, the type (density) of the density adjusting agent (a) to be blended in the organic substance molded body (x) according to the molded body density ρx of the organic substance molded body (x) and the bulk density ρf of the fluidized medium (f). And the blending amount are appropriately selected.

Table 3 shows some substances (coal tar pitch, silica, calcium carbonate, magnesium oxide, alumina, iron oxide powder, graphite) suitable as the density adjusting agent (a) and their densities (true densities). For the density adjusting agent (a), for example, one or more of these can be used. Further, substances other than those shown in Table 3 that can be used as the density adjusting agent (a) include, for example, coke, iron ore, steel mill dust (blast furnace dust, converter dust, dust collector dust, rolling mill scale, etc.). Minerals (dromite, limestone, stone, etc.), sea sand, river sand, crushed stone powder, concrete, brick, iron slag, quartz glass scrap, etc. can be mentioned, and one or more of these can be used. Some of these contain one or more of the substances shown in Table 3 as a part of the components, but all of them are inexpensive and easily available. However, the density adjusting agent (a) is not limited to these, and a mixture with an organic substance can be compression-molded, and by blending, the molded body density ρx of the organic substance molded product (x) is increased. Any type can be used as long as it can be used. Therefore, the density modifier (a) may be either a volatile substance (= a substance that volatilizes at the temperature in the reactor) or a non-volatile substance (= a substance that does not volatilize at the temperature in the reactor). In the case of the solid density adjusting agent (a), a powder or granular material is generally used.

Further, the preferable conditions for the shape and size of the density adjusting agent (a) are as follows.
First, as for the shape of the density adjusting agent (a), powder granules are suitable as described above, and when a fibrous or fragmented material is used, cracks are likely to occur in the organic substance molded product (x). Because. That is, the fibrous or fragmented density modifier (a) is difficult to disperse in the organic substance molded product (x) and easily creates voids, so that the homogeneity and density of the molded product are lowered and cracks are generated. It will be easier. In addition, since the number of voids increases, the density of the organic substance molded product (x) is unlikely to increase. As the definition of the particle shape, it can be treated quantitatively by using the aspect ratio shown in JIS Z8900. That is, when a microscopic image of the particles of the density adjusting agent (a) is imaged and the [maximum width in the direction orthogonal to the major axis / major axis] is set as the aspect ratio, the average aspect of the density adjusting agent (a) There is no particular problem when the ratio is in the range of 1 to 3.5, but when the average aspect ratio exceeds 3.5, cracks are likely to occur in the organic material molded body (x). As a result, the organic substance and the density adjusting agent (a) are separated by decomposition in the reactor, so that the original effect that the density adjusting agent (a) adjusts the density of the organic substance molded product (x) can be obtained. It becomes difficult. Therefore, the density adjuster (a) preferably has an average aspect ratio of 1 to 3.5. Here, the average aspect ratio of the density adjusting agent (a) is the average value of the aspect ratios of 100 particles randomly selected from the density adjusting agent (a).

Regarding the size of the density modifier (a), if it is too large, cracks are likely to occur in the organic substance molded body (x), and if it is too small, crushing is required, which increases the cost and becomes a dust source during molding. May impair hygiene. Therefore, when the average maximum width of the organic substance molded body (x) in the direction orthogonal to the major axis is D (mm) and the average major axis of the density adjusting agent (a) is d (mm), D / d is preferably 3 to 300, and particularly preferably 4.5 to 30. Here, the average maximum width D of the organic material molded product (x) is the average of the maximum width D of 100 organic material molded products (particles) randomly selected from the organic material molded products (x). The average major axis d of the density adjusting agent (a) is the average value of the major axis d of 100 particles randomly selected from the density adjusting agent (a).

In general, the compounding of the density adjusting agent (a) increases the molding density ρx of the organic substance molded product (x). ^{In FIG. 1, silica sand having a bulk density ρf of 1.1 g / cm 3} is used as a powder or granule for the fluid medium (f), and iron oxide is used as the density adjusting agent (a) to be blended in the organic substance molded product (x). When powder, alumina powder, and graphite powder (see Table 3 for their respective densities) are used, the density ρx of the organic substance molded body (x) and the density adjusting agent in the organic substance molded body (x) are used. The range (upper limit) of the molded body density ρx of the organic substance molded body (x) for satisfying the relationship with the blending amount of (a) and the conditions of the present invention (density ratio ρx / ρf = 0.99 to 1.10). , Lower limit). According to this, when the density adjusting agent (a) is not blended, the density ratio ρx / ρf is 0.89, which is out of the conditions of the present invention, but an appropriate amount of the density adjusting agent (a) is added to the organic substance molded body (x). ) Can be added to make the density ratio ρx / ρf in the range of 0.99 to 1.10.

When the density adjusting agent (a) is a volatile substance (= a substance that volatilizes at the temperature in the reactor) such as coal tar pitch, the density adjusting agent in the organic substance molded body (x) Since (a) is decomposed or burned at a high temperature in the reactor, gasified and discharged to the outside of the system as a gas, the amount and bulk density of the fluidized medium (f) forming the fluidized bed are almost constant during operation. Is maintained at. Therefore, the operation can be continued without taking any special measures.
On the other hand, when the density adjusting agent (a) is a non-volatile substance (= a substance that does not volatilize at the temperature in the reactor), the density adjusting agent (a) contained in the organic substance molded body (x). ) Remains in the reactor and becomes a part of the fluidized bed (f), so that the amount of the fluidized bed (f) forming the fluidized bed gradually increases, and finally the height of the fluidized bed becomes excessive. It becomes difficult to continue the gasification reaction. Therefore, it is necessary to extract the fluidized medium (f) forming the fluidized bed. Further, if the fluid medium (f) is only extracted and new powders and granules for the fluid medium are not supplied (replenished), the original fluid medium is replaced with the density adjusting agent (a), so that the fluid medium (f) The concentration of the density modifier (a) in f) increases. In this case, since a high-density powder or granule is generally used as the non-volatile density adjusting agent (a), the density ratio ρx / ρf can be adjusted by adjusting the molded body density ρx of the organic substance molded body (x). It becomes difficult to adjust to the range of 0.99 to 1.10. Therefore, it is necessary to extract a part of the fluidized medium (f) forming the fluidized bed and supply (replenish) new powders and granules for the fluidized bed to the fluidized bed.

That is, in order to keep the amount of the fluid medium (f) in the reactor constant and the density ratio ρx / ρf appropriately maintained in the range of 0.99 to 1.10 during steady operation. , In order to extract a part of the fluid medium (f) in the reactor (however, a fluid medium partially composed of the density modifier (a)) and discharge it to the outside of the system, and to compensate for the discharge of this fluid medium. Supply (replenish) new powders and granules for the fluid medium to the reactor.
Further, in this case, the concentration of the density adjusting agent (a) in the flow medium (f) forming the flow layer becomes constant during the steady operation (therefore, the bulk density ρf of the flow medium (f) becomes constant. ), The discharge rate of the density adjusting agent (a) in the flow medium (f) discharged to the outside of the system is the same as the supply rate of the density adjusting agent (a) by the organic substance molded body (x). In addition, the supply rate of new powders and granules for the fluidized medium is set to the powdered particles other than the density adjuster (a) in the fluidized medium (f) discharged to the outside of the system (powder and granules for the fluidized medium). It is preferable that the discharge rate is the same as that of the product).
When the density adjusting agent (a) is a volatile substance as described above, the bulk density ρf of the fluidized medium (f) is the bulky density of the powder or granules for the original fluidized medium. For example, the calculated value as shown in FIG. 1 can be applied as it is. On the other hand, when the density adjusting agent (a) is a non-volatile substance as described above, the density adjusting agent (a) remaining in the reactor becomes a part of the flow medium (f). , The bulk density ρf of the fluidized medium (f) is different from the bulky density of the original powder and granules for the fluidized medium. The bulk density ρf of the flow medium (f) in this case will be described in detail later.

The reaction temperature in the fluidized bed reactor is preferably about 400 to 800 ° C, more preferably about 600 to 700 ° C. If the reaction temperature is less than 400 ° C., the thermal decomposition of the organic substance is difficult to proceed, and the yield of the gaseous substance becomes low. On the other hand, when the reaction temperature exceeds 800 ° C., the thermal decomposition of C1 to C4 compounds among the gaseous substances of the thermal decomposition products proceeds _{to generate CO and CO 2} , the calorific value of the gaseous substances decreases, and the gaseous fuel The value as is reduced.
When the reaction temperature is high, the amount of gaseous substances produced tends to increase and the amount of oily substances produced tends to decrease, but the lower the reaction temperature, the lower the energy cost, so the reaction at as low a temperature as possible is advantageous. Is. Since the influence of pressure is hardly observed, it is economical to operate the reactor with a slight pressure of about ^{normal pressure to several kg / cm 2.}

Further, in the present invention, a catalyst is not particularly required for the thermal decomposition of the organic substance, but those having a catalytic function in a part or all of the powders and granules for a fluid medium may be used. Further, the density adjusting agent (a) of the organic substance molded product (x) may have a catalytic function. As the catalyst, one kind or two or more kinds of catalysts having steam reforming activity, carbon dioxide reforming activity, hydrogenation activity, and hydrocracking activity, respectively, can be used. Specific examples include a Ni-based reforming catalyst, a Ni-based hydrogenation catalyst, and a Pt / zeolite-based petroleum refining catalyst. Further, converter-generated dust, iron ore, etc., which are known to be composed of fine Fe particles, can also be used as a reforming catalyst or a hydrocracking catalyst.

FIG. 2 schematically shows a flow of a method for thermally decomposing an organic substance according to the present invention and an embodiment of a pyrolysis facility. In this embodiment, since there is no means for extracting a part of the fluidized medium (f) forming the fluidized bed, the density adjusting agent (a) blended in the organic substance molded product (x) is derived from the volatile substance. It is applicable when
In FIG. 2, reference numeral 1 denotes a fluidized bed type reactor (pyrolysis furnace), and a fluidized medium (f) constituting the fluidized bed 2 is filled on the dispersion plate 3 in the reactor 1. A mixed gas (g), which is a fluidized gas, is introduced into the air box 4 below the dispersion plate 3, and the mixed gas (g) is blown out from the dispersion plate 3 to cause a fluidized medium (f). ) Is formed. The reaction temperature in the reactor 1 is about 400 to 800 ° C., and a heater 8 is arranged around the reactor body to compensate for the endothermic reaction caused by the temperature rise to the reaction temperature and gasification. The inside of 1 is heated.

A supply pipe 6 is connected to the upper part of the reactor 1, and the organic substance molded product (x) cut out by the quantitative cutting device 7 is quantitatively supplied into the reactor 1 through the supply pipe 6.
The gas generated by the gasification reaction in the reactor 1 is taken out through the gas take-out pipe 9 connected to the upper part of the reactor 1 and discharged to the outside of the system for use as fuel gas or the like. Further, since the produced gas discharged from the reactor 1 is accompanied by powder (fluid medium), a gas cleaning device 10 is installed in the gas take-out pipe 9 as needed, and the produced gas is cleaned to remove the powder. It may be removed. As the gas cleaning device 10, for example, a scrubber or the like that sprinkles water on the rising generated gas from above and collects the powder in the gas with water can be used. Further, a cyclone type or an electrostatic precipitator can also be used, and the determination may be made in consideration of the place where the obtained gas is used.
A new powder or granule for a fluid medium is stored in the storage tank 11, and if necessary, the powder or granule is cut out by the quantitative cutting device 12 and supplied to the reactor 1 through the supply pipe 13.

In the present embodiment, the fluidized bed 2 is formed by supplying the mixed gas (g), which is a fluidized gas, into the reactor 1 through the supply pipe 5, and the inside of the reactor 1 is brought to a predetermined temperature by the heater 8. The temperature is raised. The organic substance molded body (x) is quantitatively supplied into the reactor 1 through the supply pipe 6, and the organic substance is thermally decomposed (gasification reaction). At this time, by supplying the organic substance molded product (x) in which the type and amount of the density adjusting agent (a) to be blended are selected to the reactor 1, the density ratio ρx / ρf is 0.90 during steady operation. Control in the range of ~ 1.10. The generated gas generated by the thermal decomposition (gasification reaction) of the organic substance in the reactor 1 (however, the unreacted gas component of the mixed gas (g) may inevitably be contained) is passed through the gas take-out pipe 9. It is taken out, cleaned by the gas cleaning device 10 as needed, and then sent to the outside of the system as fuel gas or the like.

FIG. 3 schematically shows a flow of a thermal decomposition method for an organic substance according to the present invention and another embodiment of a thermal decomposition facility, and is a density adjusting agent (a) blended in an organic substance molded body (x). Is provided with a means for extracting a part of the fluidized medium (f) forming the fluidized bed and discharging it to the outside of the system in order to apply it when the substance is composed of a non-volatile substance.
In this embodiment, a discharge pipe 14 for extracting a part of the fluidized medium (f) forming the fluidized bed 2 and discharging it to the outside of the system is connected to the lower part of the reactor 1. The discharge pipe 14 is provided with a discharge amount control device 15, so that the discharge amount control device 15 can control the discharge amount of the flow medium (f).
Since other configurations are the same as those of the embodiment shown in FIG. 2, the same reference numerals are given and detailed description thereof will be omitted.

Also in this embodiment, the organic substance is thermally decomposed (gasification reaction) in the same manner as in the embodiment of FIG. 2, and the type and amount of the density adjusting agent (a) to be blended are selected for the organic substance molded body (x). ) Is supplied to the reactor 1 to control the density ratio ρx / ρf in the range of 0.99 to 1.10 during steady operation, but the density modifier (a) is a non-volatile substance. Since the density modifier (a) remains in the reactor and becomes a part of the fluidized medium (f), as described above, a part of the fluidized medium (f) forming the fluidized bed is extracted and at the same time. It is necessary to supply (replenish) new powders and granules for the fluidized bed to the fluidized bed. Therefore, a part of the fluidized medium (f) forming the fluidized bed 2 is extracted through the discharge pipe 14 and discharged to the outside of the system, and is stored in the storage tank 11 in order to compensate for the discharged portion of the fluidized medium. A new powder or granule for the fluidized medium is supplied (replenished) to the reactor 1 through the supply pipe 13.
In this case, as described above, during steady operation, the concentration of the density adjusting agent (a) in the flow medium (f) forming the flow layer 2 becomes constant (thus, the bulk of the flow medium (f)). In order to make the density ρf constant), the discharge rate of the density adjusting agent (a) in the flow medium (f) discharged to the outside of the system is set to the density adjusting agent (a) by the organic substance molded body (x). ), And the supply rate of new powders and granules for the flow medium is set to the same as the supply rate of the powders and granules other than the density adjuster (a) in the flow medium (f) discharged to the outside of the system. It is preferable that the discharge rate is the same as that of the powder and granules for the fluid medium.

FIG. 4 schematically shows a flow of a thermal decomposition method for an organic substance according to the present invention and another embodiment of a thermal decomposition facility, and is blended in an organic substance molded body (x) as in the embodiment of FIG. In order to apply this when the density modifier (a) is made of a non-volatile substance, a means for extracting a part of the fluidized medium (f) forming the fluidized bed and discharging it to the outside of the system is provided. However, it also has a circulation heating system that heats a part of the fluidized medium extracted from the fluidized bed and returns it to the reactor.

That is, in this embodiment, in order to heat the fluidized bed, a circulation pipeline 16 for returning a part of the fluidized medium (f) forming the fluidized bed 2 to the fluidized bed 2 after extracting and heating the fluidized bed 2 is provided. The flow medium outlet 160 (upstream end in the flow medium circulation direction) of the circulation pipeline 16 is provided at the lower part of the reactor 1, and the flow medium introduction port 161 (downstream end in the flow medium circulation direction) reacts. Each is provided on the upper part of the vessel 1. The circulation conduit 16 is provided with a circulation amount control device 17 and a heating device 18 (for example, a heating furnace such as a kiln) for the flow medium (f) in order from the upstream side, whereby the circulation amount of the flow medium (f) is provided. It is possible to control and heat the. Then, a discharge pipe 14 for extracting a part of the flow medium (f) circulating in the circulation pipe 16 and discharging it to the outside of the system is connected to the pipe line portion between the circulation amount control device 17 and the heating device 18. ing. The discharge pipe 14 is provided with a discharge amount control device 15, so that the discharge amount control device 15 can control the discharge amount of the flow medium (f) to the outside of the system.
In the present embodiment, the circulation amount control device 17 and the heating device 18 are separately provided, but instead of providing the heating device 18, the circulation amount control device 17 can be provided with a heating function. Further, as shown by the virtual line, the heater 8 similar to the embodiment shown in FIG. 2 may be provided, and the heater 8 may be used in combination for heating the flow medium (f).
Since other configurations are the same as those of the embodiment shown in FIG. 2, the same reference numerals are given and detailed description thereof will be omitted.

In this embodiment as well, as in the embodiment of FIG. 3, the density adjusting agent (a) is a non-volatile substance, and the density adjusting agent (a) remains in the reactor and becomes a part of the fluidized medium (f). Therefore, it is necessary to extract a part of the fluidized medium (f) forming the fluidized bed and supply (replenish) new powders and granules for the fluidized bed to the fluidized bed. Therefore, a part of the flow medium (f) forming the fluidized bed 2 is extracted into the circulation pipe line 16, heated by the heating device 18, and then refluxed to the reactor 1, and the flow medium in the circulation pipe line 16 is returned. A part of (f) is extracted through the discharge pipe 14 and discharged to the outside of the system. At the same time, in order to make up for the discharged portion of the fluid medium, new powders and granules for the fluid medium stored in the storage tank 11 are supplied (replenished) to the reactor 1 through the supply pipe 13.
In this case, as described above, during steady operation, the concentration of the density adjusting agent (a) in the flow medium (f) forming the flow layer 2 becomes constant (thus, the bulk of the flow medium (f)). In order to make the density ρf constant), the discharge rate of the density adjusting agent (a) in the flow medium (f) discharged to the outside of the system is set to the density adjusting agent (a) by the organic substance molded body (x). ), And the supply rate of new powders and granules for the flow medium is set to the same as the supply rate of the powders and granules other than the density adjuster (a) in the flow medium (f) discharged to the outside of the system. It is preferable that the discharge rate is the same as that of the powder and granules for the fluid medium.

Next, as in the embodiment of FIGS. 3 and 4, since the density adjusting agent (a) blended in the organic substance molded body (x) is a non-volatile substance, a fluidized medium (flowing medium) forming a fluidized bed ( Definition (how to obtain) the bulk density ρf of the fluidized bed (f) when a part of f) is extracted and discharged to the outside of the system and new powders and granules for the fluidized bed are supplied (replenished) to the fluidized bed. ) Will be explained.
Here, during steady operation, the concentration of the density adjusting agent (a) in the flow medium (f) forming the flow layer becomes constant (thus, the bulk density ρf of the flow medium (f) becomes constant). Therefore, the discharge rate of the density adjusting agent (a) in the flow medium (f) discharged to the outside of the system is made the same as the supply rate of the density adjusting agent (a) by the organic substance molded body (x). In addition, the supply rate of new powders and granules for the fluidized medium is adjusted to the powdered particles other than the density adjusting agent (a) in the fluidized medium (f) discharged to the outside of the system (powdered granules for the fluidized medium). Consider the case where the discharge rate is the same as that of.

For example, in the embodiment of FIG. 4 having the circulation pipeline 16, when the mass balance of the fluidized medium and the density adjusting agent during steady operation is taken as shown in FIG. 5, in the fluidized bed (f) forming the fluidized bed. The following equation (ia) is derived with respect to the mass fraction (concentration) conc of the density adjusting agent (a).
Wp x A + conc x (Wf-Wout) = conc x Wf ... (ia)
However, conc: mass fraction (-) of the density modifier (a) in the flow medium (f)
Wp: Supply rate (kg / h) of the organic substance molded product (x) into the reactor
A: Mass fraction (-) of the density modifier (a) in the organic substance molded product (x)
Wf: Extraction speed (kg / h) of the flow medium (f) into the circulation pipeline
Wout: Emission of fluid medium (f) out of the system (kg / h)
Further, in the case of the embodiment of FIG. 3, since there is no circulation pipeline as in the embodiment of FIG. 4, the following equation (ib) is derived.
Wp x A = conc x Wout ... (ib)

The following equation (ii) is derived from the above equation (ia) or equation (ib),
conc ＝ Wp × A / Wout… (ii)
Therefore, the bulk density ρf of the flow medium (f) can be calculated by the following equation (1).
ρf ＝ conc × ρa ＋ (1-conc) × ρm
ρf = {ρa × (Wp × A) + ρm × Wout-ρm × (Wp × A)} / Wout… (1)
However, ρf: bulk density of fluid medium (f) (g / cm ³ )
conc: Mass fraction (-) of density modifier (a) in fluid medium (f)
ρa: Bulk density of density modifier (a) (g / cm ³ )
Wp: Supply rate (kg / h) of the organic substance molded product (x) into the reactor
A: Mass fraction (-) of the density modifier (a) in the organic substance molded product (x)
Wout: Emission of fluid medium (f) out of the system (kg / h)
ρm: Bulk density of new powders and granules for the fluid medium supplied to the reactor (g / cm ³ )

That is, the molded body density ρx of the organic substance molded body (x) and the bulk density ρf of the flow medium (f) calculated by the above equation (1) satisfy the ratio ρx / ρf = 0.99 to 1.10. In addition, the molded body density ρx of the organic substance molded body (x) and the bulk density ρf of the fluidized medium (f) may be adjusted.
When adjusting the bulk density ρf of the flow medium (f) calculated by the above equation (1), for example, if ρa, ρm, and A are determined, the bulk density ρf of the flow medium (f) can be adjusted by adjusting Wout. Can be adjusted. On the other hand, when Wout is fixed, the bulk density ρf of the flow medium (f) can be adjusted by adjusting ρa, A, and ρm. At this time, the supply rate Win (kg / h) of the new powder and granules for the fluid medium supplied to the reactor and Wp, A, and Wout have the relationship of the following equation (2).
Win + Wp x A = Wout ... (2)
Similar to the bulk density ρf of the flow medium (f), the bulk density ρa of the density modifier (a) and the bulk density ρm of the new powder and granules for the fluid medium supplied to the reactor are both "looseness". "Density", and the measuring method shall be in accordance with JIS K7365 (Plastic-How to determine the apparent density of the material that can be poured from the specified funnel).

In order to investigate the effect of the density ratio ρx / ρf on the amount of gaseous substances produced, a gasification experiment was carried out in the same manner as in the examples described later. The result is shown in FIG.
As for the experimental conditions, silica sand (bulk density ρf: 1.1 g / cm ³ ) was used as the powder for the fluid medium, and the density was adjusted as necessary for the organic substance molded product (x) (waste plastic molded product). Iron oxide powder was added as the agent (a) to adjust the density of the molded product.
This gasification experiment, the equipment configuration shown in FIG. 4, the fluidized bed in the reactor, the fluidizing gas (and organic material pyrolysis gas) as _{H 2: 20vol%, CO:} 21vol%, CO 2: A mixed gas having a gas composition of 19 vol%, H ₂ O: 37 vol%, N ₂ ^{: 4 vol% was supplied at a flow rate of 172 Nm 3} / h, and a waste plastic molded product was supplied at a supply rate of 880 kg / h, and the reaction temperature was changed. The waste plastic was thermally decomposed at 600 ° C. In order to prevent the temperature inside the reactor from dropping sharply, the mixed gas, which is a fluidized gas (and a gas for thermal decomposition of organic substances), was heated to 430 ° C. by a preheater.

The basic operation mode in this gasification experiment is that the concentration of the density adjusting agent (a) in the fluid medium (f) forming the fluidized layer becomes constant (hence, the bulk density of the fluidized medium (f)). In order to make ρf constant), the discharge rate of the density adjusting agent (a) in the flow medium (f) discharged to the outside of the system is set to the density adjusting agent (a) by the organic substance molded body (x). The supply rate of the new powders and granules for the flow medium is the same as the supply rate of the above, and the supply rate of the powders and granules other than the density adjuster (a) in the flow medium (f) discharged to the outside of the system (flow). The discharge rate is the same as that of the powder and granules for the medium), but when operating at a low density ratio of ρx / ρf, the flowable layer can be reduced by reducing the amount of the flow medium (f) discharged to the outside of the system. Increase the concentration of the density modifier (a) in the fluid medium (f) to be formed (ie, relatively increase the concentration of iron oxide powder heavier than silica sand in the fluid medium (f)), thereby the fluid medium ( The bulk density ρf of f) was increased so that the density ratio ρx / ρf was decreased.
As shown in FIG. 6, the yield of the gaseous substance is remarkably increased in the range of the density ratio ρx / ρf of 0.99 to 1.10.

Next, a compression molding method for an organic substance for obtaining an organic substance molded product (x) will be described.
There are no particular restrictions on the compression molding method for organic substances (including the case of organic substances to which the density modifier (a) is added), but a compression molding method using an extrusion molding machine (compression molding machine), a press molding machine, or the like. Of these, the use of an extrusion molding machine is particularly preferable because a molded product can be continuously produced.
The extrusion molding machine (compression molding machine) includes a ring die type, a piston type, a screw type, and the like, but any of them may be used. The ring die type is easy to increase in size and is suitable for mass processing. Further, the screw type is relatively hard because it is relatively easy to increase the compressive force, and in particular, the biaxial screw type is easy to apply a large compressive force as compared with the single shaft screw type. Suitable for molding things. The optimum extrusion molding machine may be selected according to the type of organic substance to be compression molded and the molding conditions.

FIG. 7 schematically shows a ring die type extrusion molding machine and the implementation status of compression molding of a material using the ring die type extrusion molding machine. This extrusion molding machine has a die ring 19 in which a large number of die holes 190 (round holes, etc.) are penetrated all around, and the inside of the die ring 19 is rotatable so as to be in contact with the inner peripheral surface of the die ring. It includes one or more rolling rollers 20 arranged, and a cutter 21 for cutting the molded product extruded from the die hole 190 and scraping it from the outer peripheral surface of the die ring. Both the die ring 19 and the rolling roller 20 are rotatably supported by a device body (not shown), but the die ring 19 is rotationally driven by a driving device, whereas the rolling roller 20 is undriven and free. The roller body of the die ring 19 rotates with the rotation of the die ring 19 due to friction with the inner peripheral surface of the die ring. The hole diameter of the die hole 190 is determined according to the size (diameter) of the molded product, but is usually about 3 to 20 mm.

In this ring die type extrusion molding machine, the die ring 19 is rotationally driven in the direction of the arrow in the drawing, and the rolling roller 20 is also rotated in the direction of the arrow accordingly. In this state, organic substances (and density adjusters) such as waste plastic and biomass that have been crushed to an appropriate size in advance according to the size of the die hole diameter are charged into the inside of the die ring 19 from an input port (not shown). The charged material is pushed into the die hole 190 of the die ring 19 while being crushed and compressed between the rolling roller 20 and the inner peripheral surface of the die ring (there is also a crushing action due to the crushing). The material pushed into the die hole 190 is compression-molded in the process of passing through the die hole 190. The material that has passed through the die ring 190 is sequentially extruded in a columnar shape toward the outer peripheral surface side of the die ring 19, and when the extruded molded product reaches the position of the cutter 21 by the rotation of the die ring 19, the cutter 21 It is scraped off from the outer peripheral surface of the die ring 19 to obtain a granular organic substance molded product. In the process of the material passing through the die hole 190, the plastic, biomass, etc. on the surface (the surface in contact with the inner peripheral surface of the die hole) were partially melted or softened by the frictional heat between the material and the inner peripheral surface of the die hole. After that, when it is extruded to the outer peripheral surface side of the die ring 19, it solidifies, and an outer shell using this solidified material as a binder may be formed.

The gaseous substance obtained by the method of the present invention is composed of carbon monoxide and hydrocarbons of about C1 to C4 as combustible components, and its LHV is about 4 to 8 Mcal / Nm ³ and has a high calorific value. Therefore, the gaseous substance obtained by the method of the present invention is suitable as a gaseous fuel, and can also be used as a reducing agent for a blast furnace or a coagulant for a sinter production process as a substitute for natural gas.

-Invention Example 1
Gas generated from a refined thermoselect gasification and melting furnace (Thermoselect Waste Gasification and Reforming Process), and after removing impurities such as hydrogen chloride, water vapor is added to the exhaust gas (hereinafter referred to as "Purified synthesis gas"). Was used as a mixed gas (g) for thermal decomposition of organic substances. For this reason, a branch pipe is provided in the thermogas discharge pipe so that a part of the thermogas can be taken out through this branch pipe, and a flow control valve, a steam mixer, and a gas preheater are installed on the downstream side of this branch pipe. Placed.

The average composition of the thermogas was H ₂ : 31 vol%, CO: 33 _{vol%, CO 2} : 30 vol%, H ₂ O: <1 _{vol%, N 2} : 6 vol%. Thermogas was supplied to the steam mixer at 108 Nm ³ / h, and steam at a pressure of 10 kg / cm ² G was supplied as steam at 64 Nm ³ / h, and the temperature was raised to 430 ° C. with a preheater. The gas composition after steam mixing is H ₂ : 20 vol%, CO: 21 vol%, CO ₂ : 19 vol%, H ₂ O: 37 vol%, N ₂ : 4 vol%, and the flow rate is 172 Nm ³ / h (mass flow rate). It was 171 kg / h). This gas was used as a mixed gas (g) for thermal decomposition of organic substances, and a thermal decomposition treatment of waste plastic was carried out according to the embodiment of FIG.

^{Silica sand (bulk density ρf: 1.1 g / cm 3} ) was used as the powder or granular material for the fluidized bed of the fluidized bed. The waste plastic molded body (organic substance molded body (x)) was obtained by the ring die type extrusion molding machine shown in FIG. 7, and the waste plastic molded body (molded body density: 0) shown in Table 2. .975 g / cm ³ ) was mixed with 2% by mass of coal tar pitch as the density adjusting agent (a), and the molded product density ρx was 1.0 g / cm ³ . As a result, the density ratio ρx / ρf during steady operation was set to 0.91. When the waste plastic molded product shown in Table 2 is used, the density ratio ρx / ρf during steady operation is 0.89.
Here, the waste plastic molded body (organic substance molded body (x)) is a cylinder having a diameter of 7 mm and a length of 10 mm, and therefore has a major axis of 10 mm and a maximum width of 7 mm in the direction orthogonal to the major axis. is there. The coal tar pitch had a shape close to an ellipse with a major axis of 2 mm, and the average aspect ratio of 100 particles was 1.87.

The fluidized bed type reactor 1 is preheated to 600 ° C. by the heater 8, and the mixed gas (g) is introduced into the reactor 1 and the waste plastic molded product is supplied at 880 kg / h. The temperature was raised to the reaction temperature of 620 ° C. After reaching 620 ° C., the thermal decomposition treatment of the waste plastic was continued for one day. The components of the produced gas reached a steady state about 2 hours after the start of the experiment.
During the experiment, the LHV of the produced gas and the amount of gaseous substances produced were measured.
In the example of the present invention, the average LHV of the produced gaseous substance was 7.2 Mcal / Nm ³ , which was 4.0 times higher than that of the thermogas (1.8 Mcal / Nm ^3). The amount of gaseous substances produced showed a high value of 756 kg / h.

-Invention Example 2
Water vapor was added to the gas generated from the converter of the steelworks to carry out a shift reaction, and the gas obtained by this was used as a mixed gas (g) for thermal decomposition of organic substances. For this reason, a branch pipe is provided in the linz-Donaw gas discharge pipe so that part of the linz-Donaw gas can be extracted through this branch pipe, and a flow control valve, steam mixer, etc. are located downstream of this branch pipe. A gas preheater and a shift reactor (cylindrical vertical type) filled with a Fe-Cr high-temperature shift catalyst were arranged.

The average composition of the _{linz-Donaw gas was H 2} : 1 vol%, CO: 65 vol%, CO ₂ : 15 vol%, H ₂ O: 1 vol%, N ₂ : 18 vol%. 70 Nm ³ / h the converter gas to steam mixer, after the steam pressure 10 kg / cm ² G was 101 nm ³ / h supplied as steam, was preheated to 320 ° C. at a gas preheater, into the shift reactor did. The shift reaction was an exothermic reaction and the shift reactor temperature rose to 430 ° C. The gas composition after the shift reaction was H ₂ : 26 vol%, CO: 0 vol%, CO ₂ : 30 vol%, H ₂ O: 35 vol%, N ₂ : 9 vol%, and the flow rate was 171 Nm ³ / h (mass flow rate). It was 171 kg / h). This gas was used as a mixed gas (g) for thermal decomposition of organic substances, and a thermal decomposition treatment of waste plastic was carried out according to the embodiment shown in FIG. 4 (however, the embodiment in which the heater 8 was used in combination).

^{Silica sand (bulk density ρf: 1.1 g / cm 3} ) was used as the powder or granular material for the fluidized bed of the fluidized bed. The waste plastic molded body (organic substance molded body (x)) was obtained by the ring die type extrusion molding machine shown in FIG. 7, and the waste plastic molded body (molded body density: 0) shown in Table 2. .975 g / cm ³ ) was mixed with 2% by mass of iron oxide powder as the density adjusting agent (a), and the molded product density ρx was 1.06 g / cm ³ . In the example of the present invention, the supply amount of the waste plastic molded product was set to 880 kg / h, and the out-of-system discharge amount of the fluidized medium (f) forming the fluidized bed 2 in the reactor 1 was set to 1200 kg / h. The bulk density ρf of the fluidized medium (f) calculated by the equation) is 1.16 g / cm ³ . As a result, the density ratio ρx / ρf during steady operation was set to 0.94.
Here, the waste plastic molded body (organic substance molded body (x)) is a cylinder having a diameter of 7 mm and a length of 10 mm, and therefore has a major axis of 10 mm and a maximum width of 7 mm in a direction orthogonal to the major axis. .. The iron oxide powder had a shape close to a sphere with a major axis of 1.5 mm, and the average aspect ratio of 100 particles was 1.08.

The fluidized bed type reactor 1 is preheated to 600 ° C. by the heater 8 in advance, and the mixed gas (g) is introduced into the reactor 1 and the waste plastic molded product is supplied at 880 kg / h to carry out the planned reaction. The temperature was raised to 620 ° C., which is the temperature. A new silica sand for a fluid medium was supplied in an amount commensurate with the above equation (2) according to the supply amount of the waste plastic molded product. After reaching 620 ° C., the thermal decomposition treatment of the waste plastic was continued for one day. The components of the produced gas reached a steady state about 2 hours after the start of the experiment.
During the experiment, the LHV of the produced gas and the amount of gaseous substances produced were measured.
In the example of the present invention, the average LHV of the produced gaseous substance was 5.7 Mcal / Nm ³ , which was 2.9 times higher than that of the linz-Donaw gas (2.0 Mcal / Nm ^3). The amount of gaseous substances produced showed a high value of 772 kg / h. The amount of recirculation of the flow medium (f) by the circulation flow path 16 was varied in the range of 0 to 1200 kg / h, but the result was hardly affected.

・ Invention Example 3
Water vapor was added to the gas generated from the converter of the steelworks to carry out a shift reaction, and the gas obtained by this was used as a mixed gas (g) for thermal decomposition of organic substances. For this reason, a branch pipe is provided in the linz-Donaw gas discharge pipe so that part of the linz-Donaw gas can be extracted through this branch pipe, and a flow control valve, steam mixer, etc. are located downstream of this branch pipe. A gas preheater and a shift reactor (cylindrical vertical type) filled with a Fe-Cr high-temperature shift catalyst were arranged.

The average composition of the _{linz-Donaw gas was H 2} : 1 vol%, CO: 65 vol%, CO ₂ : 15 vol%, H ₂ O: 1 vol%, N ₂ : 18 vol%. 70 Nm ³ / h the converter gas to steam mixer, after the steam pressure 10 kg / cm ² G was 101 nm ³ / h supplied as steam, was preheated to 320 ° C. at a gas preheater, into the shift reactor did. The shift reaction was an exothermic reaction and the shift reactor temperature rose to 430 ° C. The gas composition after the shift reaction was H ₂ : 26 vol%, CO: 0 vol%, CO ₂ : 30 vol%, H ₂ O: 35 vol%, N ₂ : 9 vol%, and the flow rate was 171 Nm ³ / h (mass flow rate). It was 171 kg / h). This gas was used as a mixed gas (g) for thermal decomposition of organic substances, and a thermal decomposition treatment of waste plastic was carried out according to the embodiment shown in FIG. 4 (however, the embodiment in which the heater 8 was used in combination).

^{Silica sand (bulk density ρf: 1.1 g / cm 3} ) was used as the powder or granular material for the fluidized bed of the fluidized bed. The waste plastic molded body (organic substance molded body (x)) was obtained by the ring die type extrusion molding machine shown in FIG. 7, and the waste plastic molded body (molded body density: 0) shown in Table 2. .975 g / cm ³ ) was mixed with 2% by mass of iron oxide powder as the density adjusting agent (a), and the molded product density ρx was 1.06 g / cm ³ . In the example of the present invention, the supply amount of the waste plastic molded product was set to 880 kg / h, and the out-of-system discharge amount of the fluidized medium (f) forming the fluidized bed 2 in the reactor 1 was set to 1200 kg / h. The bulk density ρf of the fluidized medium (f) calculated by the equation) is 1.16 g / cm ³ . As a result, the density ratio ρx / ρf during steady operation was set to 0.94.
Here, the waste plastic molded body (organic substance molded body (x)) is a cylinder having a diameter of 7 mm and a length of 10 mm, and therefore has a major axis of 10 mm and a maximum width of 7 mm in a direction orthogonal to the major axis. .. The iron oxide powder had a shape close to a sphere with a major axis of 3 mm, and the average aspect ratio of 100 particles was 1.11.

The fluidized bed type reactor 1 is preheated to 600 ° C. by the heater 8 in advance, and the mixed gas (g) is introduced into the reactor 1 and the waste plastic molded product is supplied at 880 kg / h to carry out the planned reaction. The temperature was raised to 620 ° C., which is the temperature. A new silica sand for a fluid medium was supplied in an amount commensurate with the above equation (2) according to the supply amount of the waste plastic molded product. After reaching 620 ° C., the thermal decomposition treatment of the waste plastic was continued for one day. The components of the produced gas reached a steady state about 2 hours after the start of the experiment.
During the experiment, the LHV of the produced gas and the amount of gaseous substances produced were measured.
In the example of the present invention, the average LHV of the produced gaseous substance was 5.3 Mcal / Nm ³ , which was 2.7 times higher than that of the linz-Donaw gas (2.0 Mcal / Nm ^3). The amount of gaseous substance produced was 704 kg / h, which was slightly lower than that of Invention Example 2, but showed a sufficiently high value. It is presumed that this is because the size of the density adjusting agent (a) is slightly larger than that of Invention Example 2. The amount of recirculation of the flow medium (f) by the circulation flow path 16 was varied in the range of 0 to 1200 kg / h, but the result was hardly affected.

・ Invention Example 4
Water vapor was added to the gas generated from the converter of the steelworks to carry out a shift reaction, and the gas obtained by this was used as a mixed gas (g) for thermal decomposition of organic substances. For this reason, a branch pipe is provided in the linz-Donaw gas discharge pipe so that part of the linz-Donaw gas can be extracted through this branch pipe, and a flow control valve, steam mixer, etc. are located downstream of this branch pipe. A gas preheater and a shift reactor (cylindrical vertical type) filled with a Fe-Cr high-temperature shift catalyst were arranged.

The average composition of the _{linz-Donaw gas was H 2} : 1 vol%, CO: 65 vol%, CO ₂ : 15 vol%, H ₂ O: 1 vol%, N ₂ : 18 vol%. 70 Nm ³ / h the converter gas to steam mixer, after the steam pressure 10 kg / cm ² G was 101 nm ³ / h supplied as steam, was preheated to 320 ° C. at a gas preheater, into the shift reactor did. The shift reaction was an exothermic reaction and the shift reactor temperature rose to 430 ° C. The gas composition after the shift reaction was H ₂ : 26 vol%, CO: 0 vol%, CO ₂ : 30 vol%, H ₂ O: 35 vol%, N ₂ : 9 vol%, and the flow rate was 171 Nm ³ / h (mass flow rate). It was 171 kg / h). This gas was used as a mixed gas (g) for thermal decomposition of organic substances, and a thermal decomposition treatment of waste plastic was carried out according to the embodiment shown in FIG. 4 (however, the embodiment in which the heater 8 was used in combination).

^{Silica sand (bulk density ρf: 1.1 g / cm 3} ) was used as the powder or granular material for the fluidized bed of the fluidized bed. The waste plastic molded body (organic substance molded body (x)) was obtained by the ring die type extrusion molding machine shown in FIG. 7, and the waste plastic molded body (molded body density: 0) shown in Table 2. .975 g / cm ³ ) was mixed with 2% by mass of alumina as the density adjusting agent (a), and the molded product density ρx was 1.04 g / cm ³ . In the example of the present invention, the supply amount of the waste plastic molded product was set to 880 kg / h, and the out-of-system discharge amount of the fluidized medium (f) forming the fluidized bed 2 in the reactor 1 was set to 1200 kg / h. The bulk density ρf of the fluidized medium (f) calculated by the equation) is 1.14 g / cm ³ . As a result, the density ratio ρx / ρf during steady operation was set to 0.91.
Here, the waste plastic molded body (organic substance molded body (x)) is a cylinder having a diameter of 7 mm and a length of 10 mm, and therefore has a major axis of 10 mm and a maximum width of 7 mm in a direction orthogonal to the major axis. .. The alumina powder had an elongated shape with a major axis of 2 mm, and the average aspect ratio of 100 particles was 4.00.

The fluidized bed type reactor 1 is preheated to 600 ° C. by the heater 8 in advance, and the mixed gas (g) is introduced into the reactor 1 and the waste plastic molded product is supplied at 880 kg / h to carry out the planned reaction. The temperature was raised to 620 ° C., which is the temperature. A new silica sand for a fluid medium was supplied in an amount commensurate with the above equation (2) according to the supply amount of the waste plastic molded product. After reaching 620 ° C., the thermal decomposition treatment of the waste plastic was continued for one day. The components of the produced gas reached a steady state about 2 hours after the start of the experiment.
During the experiment, the LHV of the produced gas and the amount of gaseous substances produced were measured.
In the example of the present invention, the average LHV of the produced gaseous substance was 5.3 Mcal / Nm ³ , which was 2.7 times higher than that of the linz-Donaw gas (2.0 Mcal / Nm ^3). The amount of gaseous substance produced was 695 kg / h, which was slightly smaller than that of other invention examples, but showed a sufficiently high value. It is presumed that this is because the shape of the density modifier (a) is slightly elongated. The amount of recirculation of the flow medium (f) by the circulation flow path 16 was varied in the range of 0 to 1200 kg / h, but the result was hardly affected.

・ Comparative example 1
Similar to Invention Example 1, a gas obtained by adding water vapor to thermogas was used as a mixed gas (g) for thermal decomposition of organic substances. That is, the average composition of the thermogas used was H ₂ : 31 vol%, CO: 33 _{vol%, CO 2} : 30 vol%, H ₂ O: <1 _{vol%, N 2} : 6 vol%, and this thermo gas was used in the steam mixer. 108 Nm ³ / h was introduced, steam at a pressure of 10 kg / cm ² G was supplied as steam at 64 Nm ³ / h, and the temperature was raised to 430 ° C. with a preheater. The gas composition after steam mixing is H ₂ : 20 vol%, CO: 21 vol%, CO ₂ : 19 vol%, H ₂ O: 37 vol%, N ₂ : 4 vol%, and the flow rate is 172 Nm ³ / h (mass flow rate). It was 171 kg / h). This gas was used as a mixed gas (g) for thermal decomposition of organic substances, and a thermal decomposition treatment of waste plastic was carried out in the equipment configuration shown in FIG.

As the waste plastic, the same waste plastic as the waste plastic molded product shown in Table 2 was used. Therefore, no density adjusting agent was used for the waste plastic molded product. The molded product density of the waste plastic molded product was 0.975 g / cm ³ . Since silica sand (bulk density 1.1 g / cm ³ ) was used as the fluidized bed of the fluidized bed, the density ratio ρx / ρf during steady operation was 0.89.
The fluidized bed type reactor 1 is preheated to 600 ° C. by the heater 8 in advance, and the mixed gas is introduced into the reactor 1 and the waste plastic molded product is supplied at 880 kg / h to reach the planned reaction temperature. The temperature was raised to 620 ° C. After reaching 620 ° C., the thermal decomposition treatment of the waste plastic was continued for one day. The components of the produced gas reached a steady state about 2 hours after the start of the experiment.
During the experiment, the LHV of the produced gas and the amount of gaseous substances produced were measured.
In this comparative example, the average LHV of the produced gaseous substance was 7.2 Mcal / Nm ³ , which was 4.0 times higher than that of the thermogas (1.8 Mcal / Nm ^3). The amount of the gaseous substance produced was 556 kg / h, which was smaller than that of Invention Example 1.

・ Comparative example 2
Similar to Invention Example 2, steam was added to the gas generated from the converter of the steelworks to carry out a shift reaction, and the gas obtained by this was used as a mixed gas (g) for thermal decomposition of organic substances. For this reason, a branch pipe is provided in the linz-Donaw gas discharge pipe so that part of the linz-Donaw gas can be extracted through this branch pipe, and a flow control valve, steam mixer, etc. are located downstream of this branch pipe. A gas preheater and a shift reactor (cylindrical vertical type) filled with a Fe-Cr high-temperature shift catalyst were arranged.
The average composition of the _{linz-Donaw gas was H 2} : 1 vol%, CO: 65 vol%, CO ₂ : 15 vol%, H ₂ O: 1 vol%, N ₂ : 18 vol%. 70 Nm ³ / h the converter gas to steam mixer, after the steam pressure 10 kg / cm ² G was 101 nm ³ / h supplied as steam, was preheated to 320 ° C. at a gas preheater, into the shift reactor did. The shift reaction was an exothermic reaction and the shift reactor temperature rose to 430 ° C. The gas composition after the shift reaction was H ₂ : 26 vol%, CO: 0 vol%, CO ₂ : 30 vol%, H ₂ O: 35 vol%, N ₂ : 9 vol%, and the flow rate was 171 Nm ³ / h (mass flow rate). It was 171 kg / h). This gas was used as a mixed gas (g) for thermal decomposition of organic substances, and a thermal decomposition treatment of waste plastic was carried out in the equipment configuration shown in FIG. 4 (however, the equipment configuration in which the heater 8 was also used).

As the waste plastic, the same waste plastic as the waste plastic molded product shown in Table 2 was used. Therefore, no density adjusting agent was used for the waste plastic molded product. The molded product density of the waste plastic molded product was 0.975 g / cm ³ . Since silica sand (bulk density 1.1 g / cm ³ ) was used as the fluidized bed of the fluidized bed, the density ratio ρx / ρf during steady operation was 0.89.
The fluidized bed type reactor 1 is preheated to 600 ° C. by the heater 8 in advance, and the mixed gas (g) is introduced into the reactor 1 and the waste plastic molded product is supplied at 880 kg / h to carry out the planned reaction. The temperature was raised to 620 ° C., which is the temperature. After reaching 620 ° C., the thermal decomposition treatment of the waste plastic was continued for one day. The components of the produced gas reached a steady state about 2 hours after the start of the experiment.
During the experiment, the LHV of the produced gas and the amount of gaseous substances produced were measured.
In this comparative example, the average LHV of the produced gaseous substance was 5.7 Mcal / Nm ³ , which was 2.9 times higher than that of the linz-Donaw gas (2.0 Mcal / Nm ^3). The amount of the gaseous substance produced was 568 kg / h, which was smaller than that of Invention Example 2.

The results of Invention Examples 1 to 4 and Comparative Examples 1 and 2 described above are shown in Table 4.

1 Reactor 2 Flow layer 3 Dispersion plate 4 Air box 5 Gas supply pipe 6 Supply pipe 7 Quantitative cutting device 8 Heater 9 Gas extraction pipe 10 Gas cleaning device 11 Storage tank 12 Quantitative cutting device 13 Supply pipe 14 Discharge pipe 15 Emissions Control device 16 Circulation pipeline 17 Circulation amount control device 18 Heating device 19 Dying 20 Rolling roller 21 Cutter 160 Flow medium outlet 161 Flow medium inlet 190 Die hole

Claims (8)

In a fluidized bed type reactor in which a mixed gas (g) containing at least hydrogen and carbon dioxide is introduced as a fluidized gas and a fluidized bed is formed by a powdery and granular fluidized medium (f), an organic substance is mixed with the gas (g). ), Which is a method of thermal decomposition.
In performing thermal decomposition of an organic substance by supplying an organic substance molded product (x) obtained by compression molding an organic substance into granules or lumps from the upper part of a reactor.
The organic substance molded body (x) is obtained by adding a density adjusting agent (a) to an organic substance and compression molding.
An organic substance characterized in that the molded body density ρx of the organic substance molded body (x) and the bulk density ρf of the fluidized medium (f) satisfy ρx / ρf = 0.99 to 1.10 during steady operation. Pyrolysis method. When an organic substance molded product (x) obtained by adding a non-volatile density modifier (a) to an organic substance and compression molding is supplied to a reactor to thermally decompose the organic substance.
During steady operation, a part of the fluid medium (f) in the reactor (however, a fluid medium partially composed of the density modifier (a)) is extracted and discharged to the outside of the system, and a new fluid medium for the fluid medium is used. The method for thermally decomposing an organic substance according to claim 1 , wherein the powders and granules are supplied to the reactor. A part of the fluid medium (f) in the reactor was extracted to the outside of the reactor, and a part of the extracted fluid medium (f) was discharged to the outside of the system, and the fluid medium (f) that was not discharged to the outside of the system. The method for thermally decomposing an organic substance according to claim 2 , wherein the mixture is refluxed to a reactor. The method for thermally decomposing an organic substance according to claim 2 or 3 , wherein the bulk density ρf of the flow medium (f) is calculated by the following equation (1).
ρf = {ρa × (Wp × A) + ρm × Wout-ρm × (Wp × A)} / Wout… (1)
However, ρf: bulk density of fluid medium (f) (g / cm ³ )
ρa: Bulk density of density modifier (a) (g / cm ³ )
Wp: Supply rate (kg / h) of the organic substance molded product (x) into the reactor
A: Mass fraction (-) of the density modifier (a) in the organic substance molded product (x)
Wout: Emission of the flow medium (f) in the reactor to the outside of the system (kg / h)
ρm: Bulk density of new powders and granules for the fluid medium supplied to the reactor (g / cm ³ ) When the aspect ratio of the density adjuster (a) is [maximum width in the direction orthogonal to the major axis / major axis], the average aspect ratio of the density adjuster (a) is 1 to 3.5. The method for thermally decomposing an organic substance according to any one of claims 1 to 4. When the average maximum width of the organic substance molded body (x) in the direction orthogonal to its major axis is D and the average major axis of the density adjusting agent (a) is d, D / d is 3 to 300. The method for thermally decomposing an organic substance according to any one of claims 1 to 5. The method for thermally decomposing an organic substance according to any one of claims 1 to 6 , wherein the organic substance contains at least one selected from plastic and biomass. Claims 1 to 7 , wherein the organic substance molded product (x) is obtained by adding a density adjusting agent (a) to an organic substance, mixing the mixture, and compression molding the organic substance into columns using an extrusion molding machine. The method for thermally decomposing an organic substance according to any one.

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