WO2022029999A1 - Thermochemical conversion method and thermochemical conversion device - Google Patents

Abstract

Provided is a method allowing even solid fuels, which are difficult to pulverize, to be converted thermochemically in a satisfactory manner, allowing for an increase in the amount of heat generation from a flammable gas generated by gasification/thermal decomposition, and, moreover, allowing for a reduction in the size of a thermochemical conversion reaction oven. This invention is a method for supplying an oxidant to the interior of a thermochemical conversion reaction oven C to convert the solid fuel thermochemically, the method comprising an electron injection step of injecting a predetermined concentration of electrons into the oxidant supplied to the interior of the thermochemical conversion reaction oven C.

Description

Thermochemical conversion method and thermochemical conversion device

The present invention relates to a thermochemical conversion method and a thermochemical conversion device.

Conventionally, by reacting solid fuels such as coal, biomass, and waste with oxidizing agents (air, oxygen, oxygen-enriched air, etc.), thermochemical conversion such as combustion, gasification, and pyrolysis is performed. Various techniques have been proposed to generate energy such as electric power and heat, and to generate liquid fuel and gaseous fuel. For example, in recent years, a vertical waste incinerator that incinerates industrial waste (particularly medical waste) containing high calorific value substances and flame-retardant substances has been proposed (see Patent Documents 1 and 2). It is said that by adopting such a technique, dioxin can be thermally decomposed and incinerated ash can be sterilized, and the strength and heat resistance of the incinerator can be improved.

Japanese Unexamined Patent Publication No. 2004-301352 Japanese Unexamined Patent Publication No. 2005-69542

By the way, in order to promote the thermochemical conversion reaction of solid fuel, (1) the solid fuel is finely pulverized, (2) the thermochemical conversion reaction temperature is raised, and (3) the thermochemical conversion reaction of solid fuel is carried out. It was necessary to take measures such as lengthening the residence time in the furnace (combustion furnace, gasification furnace, thermal decomposition furnace, etc.). However, for (1), it may be difficult to finely grind solid fuel in the first place, and for (2), it is necessary to increase the supply amount of oxidant, especially during gasification and thermal decomposition, and as a result, it is necessary to increase the supply amount of the oxidizing agent. There is a problem that the calorific value of the generated combustible gas is reduced, and there is a problem that the thermochemical conversion reaction furnace needs to be increased in size for (3). Even if the conventional techniques described in Patent Documents 1 and 2 are adopted, these problems have not been solved, and an effective solution has been long-awaited.

The present invention has been made in view of such circumstances, and can satisfactorily thermochemically convert solid fuels that are difficult to be finely pulverized, and generate heat of combustible gas generated by gasification / pyrolysis. It is an object of the present invention to provide a method capable of increasing the amount and reducing the size of a thermochemical conversion reactor.

In order to achieve the above object, the thermochemical conversion method according to the present invention is a method of supplying an oxidizing agent into a thermochemical conversion reaction furnace to thermochemically convert a solid fuel, and is a thermochemical conversion method. It includes an electron injection step of injecting electrons of a predetermined concentration into an oxidizing agent supplied into the reaction furnace.

Further, the thermochemical conversion device according to the present invention is a device that supplies an oxidant into a thermochemical conversion reaction furnace to thermochemically convert a solid fuel, and supplies the solid fuel into the thermochemical conversion reaction furnace. It is provided with an electron injection means for injecting electrons of a predetermined concentration into the oxidizing agent to be produced.

When such a method and configuration are adopted, electrons of a predetermined concentration are injected into the oxidant supplied in the thermochemical conversion reaction furnace, so that the thermochemical conversion of the solid fuel can be promoted. That is, the electrons supplied into the thermochemical conversion reaction furnace together with the oxidizing agent collide with the oxidizing agent and the pyrolysis gas in the pyrolysis gas combustion / gasification region of the thermochemical conversion reaction furnace, so that they are secondary. As a result of the generation of electrons and the generation of ions and radicals, the combustion and gasification of the pyrolysis gas is promoted. Then, since the heat generated by the combustion / gasification of the pyrolysis gas is transferred to the combustion / gasification region of the pyrolysis residue, the combustion / gasification of the pyrolysis residue is promoted. As a result, the thermochemical conversion of the solid fuel can be promoted over the entire thermochemical conversion reaction reactor, and the calorific value of the combustible gas generated by gasification / pyrolysis can be increased. In addition, since the amount of solid fuel processed can be increased, the thermochemical conversion reactor can be downsized. Further, there is a problem that tar is generated during gasification and thermal decomposition of solid fuel, and the tar is condensed in the process of cooling the generated gas, which causes clogging of the wake equipment. Adopting the method and the thermochemical conversion device has the advantages that the decomposition of tar in the pyrolysis gas is promoted by the action of electrons, the tar becomes lighter and more difficult to condense, and the tar concentration also decreases.

In the thermochemical conversion method according to the present invention, based on at least one of the volume of the thermochemical conversion space in the thermochemical conversion reaction furnace, the type of solid fuel, and the thermochemical conversion reaction temperature, It can include an electron concentration setting step of setting the concentration of electrons injected into the oxidant. Further, in the thermochemical conversion apparatus according to the present invention, it is based on at least one of the volume of the thermochemical conversion space in the thermochemical conversion reaction furnace, the type of solid fuel, and the thermochemical conversion reaction temperature. Therefore, an electron concentration setting means for setting the concentration of electrons injected into the oxidizing agent can be provided.

When such a method and configuration are adopted, the oxidant is based on at least one of the volume of the thermochemical conversion space in the thermochemical conversion reaction furnace, the type of solid fuel, and the thermochemical conversion reaction temperature. The concentration of injected electrons can be set to the optimum value.

In the thermochemical conversion method according to the present invention, oxidation is performed according to the flow rate measured in the oxidant flow rate measuring step for measuring the flow rate of the oxidant supplied in the thermochemical conversion reaction furnace and the oxidant flow rate measuring step. It can include an electron concentration control step of controlling the concentration of electrons injected into the agent. Further, in the thermochemical conversion apparatus according to the present invention, according to the oxidant flow rate measuring means for measuring the flow rate of the oxidant supplied into the thermochemical change reaction furnace and the flow rate measured by the oxidant flow rate measuring means. , An electron concentration controlling means for controlling the concentration of electrons injected into the oxidizing agent can be provided.

By adopting such a method and configuration, the concentration of electrons injected into the oxidant can be controlled according to the flow rate of the oxidant supplied into the thermochemical conversion reaction furnace, so that the flow rate of the oxidant fluctuates. Even so, the electron concentration can be maintained.

In the thermochemical conversion method according to the present invention, the thermochemical conversion reaction furnace is provided with an oxidant inlet that receives an oxidant from the outside, and in the electron injection step, the oxidant immediately before flowing into the oxidant inlet is provided. Can be injected with electrons. Further, the thermochemical conversion apparatus according to the present invention includes an oxidant flow generating means for generating an oxidant flow, and an oxidant supply pipe for connecting the oxidant flow generating means and the thermochemical conversion reaction furnace. The thermochemical conversion reaction reactor has an oxidant inlet that receives an oxidant supply from the outside, and the oxidant is used as an electron injection means so as to inject electrons into the oxidant immediately before flowing into the oxidant inlet. It can be installed in the supply pipe.

When such a method and configuration are adopted, electrons are injected into the oxidant immediately before flowing into the oxidant inlet of the thermochemical conversion reaction furnace, so that the electron concentration until the electrons flow into the thermochemical conversion reaction furnace The decrease can be suppressed as much as possible. It is also possible to install an electron injection means in the oxidizing agent flow generating means.

In the thermochemical conversion method according to the present invention, the oxidant supplied into the thermochemical conversion reaction furnace is heated by the apparent heat recovered from the combustion gas discharged from the thermochemical conversion reaction furnace or the flammable gas. An oxidant heating step can be included. Further, in the thermochemical conversion apparatus according to the present invention, the oxidizing agent supplied into the thermochemical conversion reaction furnace by the sensible heat recovered from the combustion gas discharged from the thermochemical conversion reaction furnace or the combustible gas is used. An oxidant heating means for heating can be provided.

By adopting such a method and configuration, the oxidant supplied into the thermochemical conversion reaction furnace can be heated by the sensible heat recovered from the combustion gas discharged from the thermochemical conversion reaction furnace or the flammable gas. Therefore, the energy utilization efficiency can be improved.

In the electron injection step of the thermochemical conversion method according to the present invention, electrons having a concentration of 500 / cc or more can be injected into the oxidizing agent. Further, in the thermochemical conversion apparatus according to the present invention, an electron injection means for injecting electrons having a concentration of 500 cells / cc or more into an oxidizing agent can be adopted.

By adopting such a method and configuration, it is possible to further promote the thermochemical conversion of the solid fuel in the thermochemical conversion reaction furnace by setting the concentration of electrons injected into the oxidant to 500 / cc or more. can.

According to the present invention, even a solid fuel that is difficult to be finely pulverized can be satisfactorily thermochemically converted, the calorific value of the combustible gas generated by gasification / pyrolysis is increased, and the amount of tar contained is increased. It is possible to provide a method that enables miniaturization of the thermochemical conversion reactor.

It is a block diagram of the thermochemical conversion apparatus which concerns on 1st Embodiment of this invention. It is a flowchart for demonstrating the thermochemical conversion method using the thermochemical conversion apparatus which concerns on 1st Embodiment of this invention. It is a block diagram of the thermochemical conversion apparatus which concerns on 2nd Embodiment of this invention. It is a block diagram of the thermochemical conversion apparatus which concerns on 3rd Embodiment of this invention. It is a block diagram of the thermochemical conversion apparatus which concerns on 4th Embodiment of this invention. It is a block diagram of the thermochemical conversion apparatus which concerns on 5th Embodiment of this invention. It is a time chart which shows the production rate of carbon dioxide at the time of solid fuel pyrolysis in Example 1 and Comparative Example 1 of this invention. It is a time chart which shows the production rate of carbon monoxide at the time of solid fuel pyrolysis in Example 1 and Comparative Example 1 of this invention. It is a time chart which shows the production rate of methane at the time of solid fuel pyrolysis in Example 1 and Comparative Example 1 of this invention. It is a time chart which shows the hydrogen production rate at the time of solid fuel pyrolysis in Example 1 and Comparative Example 1 of this invention. It is a time chart which shows the production rate of carbon dioxide at the time of solid fuel pyrolysis in Example 2 and Comparative Example 2 of this invention. 6 is a bar chart showing the average production rate of each produced gas ((A) is carbon dioxide, (B) is hydrogen and ethylene) when the concentration of electrons to be injected is changed in Examples 2 to 6 of the present invention.

Hereinafter, each embodiment of the present invention will be described with reference to the drawings.

<First Embodiment>
First, the configuration of the thermochemical conversion device 1 according to the first embodiment of the present invention will be described with reference to FIG. The thermochemical conversion apparatus 1 according to the present embodiment is an apparatus for supplying an oxidizing agent into the thermochemical conversion reaction furnace C to thermochemically convert a solid fuel, and as shown in FIG. 1, oxidation. It is provided with an agent supply machine 10, an oxidant supply pipe 20, a flow meter 30, an oxidant preheater 40, an electron generator 50, an electron concentration measuring device 60, a control unit 70, and the like. Here, the thermochemical conversion reaction reactor C is a furnace having a space for thermochemically converting solid fuel, and is, for example, a combustion furnace, a gasification furnace, a pyrolysis furnace, or the like.

The oxidant supply machine 10 functions to generate an oxidant flow supplied to the thermochemical conversion reaction furnace C, and corresponds to the oxidant flow generation means in the present invention. The oxidant supply pipe 20 is a tube for connecting the oxidant supply machine 10 and the thermochemical conversion reaction furnace C to supply the oxidant produced by the oxidant supply machine 10 to the thermochemical conversion reaction furnace C. Is. The thermochemical conversion reaction reactor C has an oxidant inlet (not shown) that receives an oxidant supply from the outside, and the oxidant supply pipe 20 is connected to the oxidant inlet.

The flow meter 30 functions to measure the flow rate of the oxidant supplied into the thermochemical conversion reaction reactor C, and corresponds to the oxidant flow rate measuring means in the present invention. The flow rate of the oxidant measured by the flow meter 30 is sent to the control unit 70 and used for controlling the oxidant supply machine 10. Specifically, the control unit 70 controls the operation of the oxidant feeder 10 based on the flow rate measured by the flow meter 30, so as to supply the oxidant at a predetermined flow rate to the thermochemical conversion reaction furnace C. It has become.

The oxidant preheater 40 heats the oxidant supplied into the thermochemical conversion reactor C by the sensible heat recovered from the combustion gas discharged from the thermochemical conversion reactor C or the combustible gas. It functions and corresponds to the oxidizing agent heating means in the present invention. The operation of the oxidant preheater 40 is controlled by the control unit 70. Specifically, the control unit 70 is adapted to supply an oxidant having a temperature lower than the heat resistant temperature of the electron generator 50 by adjusting the temperature of the oxidant heated by the oxidant preheater 40. Even if the oxidant preheater 40 itself is provided with a heating device so that the oxidant can be heated without using the sensible heat recovered from the gas discharged from the thermochemical conversion reaction furnace C. good.

The electron generator 50 functions to inject electrons of a predetermined concentration into the oxidizing agent supplied into the thermochemical conversion reaction furnace C, and corresponds to the electron injecting means in the present invention. As the electron generator 50, for example, a method in which a high pulse voltage is applied to a negative electrode (electron generation terminal) sharpened in a needle shape to directly emit electrons into the air can be adopted. Then, the electron generation terminal of the electron generator 50 is inserted into the hole provided on the wall surface of the oxidant supply pipe 20, and a high voltage is applied to the electron generation terminal, whereby the oxidant circulating inside the oxidant supply pipe 20 is applied. Can be injected with electrons. At this time, it is generated by changing the number of electron generating terminals of the electron generator 50 or applying a voltage only to a part of the electron generating terminals (for example, only 50 out of 100 terminals). The electron concentration can be set to a predetermined concentration.

The operation of the electron generator 50 is controlled by the control unit 70. Specifically, the control unit 70 generates electrons having a concentration set based on various conditions in the electron generator 50, and injects electrons from the electron generator 50 into the oxidant supply pipe 20. Further, the control unit 70 controls the concentration of electrons injected into the oxidizing agent from the electron generator 50 according to the flow rate measured by the flow meter 30. The electron generator 50 in the present embodiment is configured to inject electrons having a concentration of 500 cells / cc or more into the oxidizing agent. In the present embodiment, the concentration of electrons generated by the electron generator 50 is such that the concentration of electrons in the oxidant immediately before flowing into the oxidant inlet of the thermochemical conversion reaction reactor C is 500 cells / cc or more. Is set relatively high (for example, about 50,000 / cc).

The electron concentration measuring device 60 functions to measure the concentration of electrons contained in the oxidizing agent flowing through the oxidizing agent supply pipe 20. The electron concentration measured by the electron concentration measuring device 60 is sent to the control unit 70 and used to control the operation of the oxidant feeder 10 and the electron generator 50. The structure of the electron concentration measuring instrument 60 is not particularly limited, and may be, for example, a structure that is preliminarily incorporated inside the oxidant supply pipe 20, and may be attached to the outside (removably) of the oxidant supply pipe 20. It may have a structure that can be used. When the latter structure is adopted, the oxidant can be extracted through the holes provided in the oxidant supply pipe 20 and the concentration of electrons contained in the extracted oxidant can be measured.

The control unit 70 integrates and controls various devices of this device. Specifically, the control unit 70 supplies the oxidant at a predetermined flow rate to the thermochemical conversion reaction furnace C by controlling the operation of the oxidant supply machine 10 based on the flow rate measured by the flow meter 30. Further, the control unit 70 supplies an oxidant having a temperature lower than the heat resistant temperature of the electron generator 50 by adjusting the temperature of the oxidant heated by the oxidant preheater 40. Further, the control unit 70 includes the volume of the thermochemical conversion space (combustion space, gasification space, pyrolysis space, etc.) in the thermochemical conversion reaction reactor C, the type of solid fuel, and the thermochemical conversion reaction temperature (combustion). The concentration of electrons injected into the oxidizing agent is set based on at least one of (temperature, gasification temperature, thermal decomposition temperature, etc.). That is, the control unit 70 functions as the electron concentration setting means in the present invention. Then, the control unit 70 generates electrons of a set concentration in the electron generator 50, and injects electrons from the electron generator 50 into the oxidant supply pipe 20. Further, the control unit 70 controls the concentration of electrons injected into the oxidant according to the flow rate measured by the flow meter 30. That is, the control unit 70 also functions as the electron concentration control means in the present invention.

Next, using the flowchart of FIG. 2, a thermochemical conversion method using the thermochemical conversion device 1 according to the present embodiment (a oxidant is supplied into the thermochemical conversion reaction reactor C to heat a solid fuel). Method of chemical conversion) will be described.

First, the control unit 70 of the thermochemical conversion device 1 has at least one of the volume of the thermochemical conversion space in the thermochemical conversion reaction reactor C, the type of solid fuel, and the thermochemical conversion reaction temperature. Based on the above, the concentration of electrons injected into the oxidizing agent is set (electron concentration setting step: S1). In the electron concentration setting step S1, the control unit 70 sets the optimum electron concentration based on various information input via an input unit (not shown), or various types stored in a storage unit (not shown). The control unit 70 can set the optimum electron concentration based on the information.

Next, the control unit 70 operates the oxidant supply machine 10 to supply the oxidant to the thermochemical conversion reaction furnace C, and operates the oxidant supply machine 10 based on the flow rate measured by the flow meter 30. By controlling the above, a predetermined flow of oxidant is supplied to the thermochemical conversion reaction reactor C (oxidizer supply step: S2). The oxidant supply step S2 includes the oxidant flow rate measuring step in the present invention, and the flow rate measured by the flow meter 30 is used for controlling the electron concentration described later.

Next, the control unit 70 operates the oxidant preheater 40 and supplies it into the thermochemical conversion reaction furnace C by the apparent heat recovered from the combustion gas discharged from the thermochemical conversion reaction furnace C or the combustible gas. The oxidant to be heated is heated (oxidizer heating step: S3). At this time, the control unit 70 adjusts the temperature of the oxidant so that the temperature of the oxidant heated by the oxidant preheater 40 is lower than the heat resistant temperature of the electron generator 50.

Next, the control unit 70 operates the electron generator 50 to generate electrons of the concentration (predetermined concentration) set in the electron concentration setting step S1 in the electron generator 50, and the electron generator 50 is sent to the oxidant supply pipe 20. And electrons are injected (electron injection step: S4). In the electron injection step S4, the control unit 70 controls the concentration of electrons injected into the oxidant according to the flow rate of the oxidant measured by the flow meter 30 in the oxidant supply step S2. That is, the electron injection step S4 includes the electron concentration control step in the present invention. In the electron injection step S4, electrons having a concentration of 500 cells / cc or more are injected into the oxidizing agent.

Subsequently, the control unit 70 operates the electron concentration measuring device 60, measures the concentration of electrons contained in the oxidant flowing through the oxidant supply pipe 20, and monitors whether or not the measured concentration is within a predetermined range. (Electron concentration measurement step: S5). When the concentration measured in the electron concentration measuring step S5 is within a predetermined range, the control unit 70 continues electron injection without changing the electron concentration generated by the electron generator 50. On the other hand, when the concentration measured in the electron concentration measuring step S5 is out of the predetermined range, the control unit 70 uses the electron generator 50 so that the concentration measured by the electron concentration measuring device 60 is within the predetermined range. The concentration of generated electrons is changed (electron concentration adjusting step: S6).

After that, the control unit 70 determines the predetermined termination conditions (for example, the passage of a preset operating time, the weight of the solid fuel in the thermochemical conversion reaction reactor C is equal to or less than a predetermined threshold, and the thermochemical conversion reaction. When the temperature in the furnace C becomes equal to or lower than a predetermined threshold, etc.) is satisfied, the control of various devices is stopped, and the thermochemical conversion of the solid fuel is completed.

In the thermochemical conversion apparatus 1 according to the embodiment described above, since electrons of a predetermined concentration are injected into the oxidant supplied into the thermochemical conversion reaction reactor C, the thermochemical conversion of the solid fuel is promoted. be able to. That is, the electrons supplied into the thermochemical conversion reaction reactor C together with the oxidizing agent collide with the oxidizing agent and the pyrolysis gas in the pyrolysis gas combustion / gasification region of the thermochemical conversion reaction reactor C. Secondary electrons are generated, which generate ions and radicals, and as a result, the combustion and gasification of the pyrolysis gas is promoted. Then, since the heat generated by the combustion / gasification of the pyrolysis gas is transferred to the pyrolysis residue combustion / gasification region, the combustion / gasification of the pyrolysis residue is promoted. As a result, the thermochemical conversion of the solid fuel can be promoted over the entire thermochemical conversion reactor, and the calorific value of the combustible gas produced by gasification / pyrolysis can be increased. Further, since the amount of fuel processed can be increased, the thermochemical conversion reactor C can be miniaturized. Furthermore, tar is generated during gasification and thermal decomposition of solid fuel, and tar is condensed in the process of cooling the generated gas, which causes blockage of wake equipment. There is an advantage that the decomposition of tar in the pyrolysis gas is promoted by the action of the above, the tar becomes lighter and more difficult to condense, and the tar concentration also decreases.

Further, in the thermochemical conversion apparatus 1 according to the above-described embodiment, at least one of the volume of the thermochemical conversion space in the thermochemical conversion reaction reactor C, the type of solid fuel, and the thermochemical conversion reaction temperature. Based on any one of them, the concentration of electrons injected into the oxidant can be set to an optimum value.

Further, in the thermochemical conversion apparatus 1 according to the above-described embodiment, the flow meter 30 for measuring the flow rate of the oxidant supplied into the thermochemical conversion reaction reactor C and the flow rate measured by the flow meter 30 are used. Accordingly, a control unit 70 for controlling the concentration of electrons injected into the oxidant is provided, so that the oxidant is injected according to the flow rate of the oxidant supplied into the thermochemical conversion reaction reactor C. The electron concentration can be controlled. Therefore, the electron concentration can be maintained even if the flow rate of the oxidizing agent fluctuates.

Further, in the thermochemical conversion apparatus 1 according to the above-described embodiment, the inside of the thermochemical conversion reaction reactor C is generated by the apparent heat recovered from the combustion gas discharged from the thermochemical conversion reaction reactor C or the combustible gas. Since the oxidant supplied to the oxidant can be heated by the oxidant preheater 40, the energy utilization efficiency can be improved.

Further, in the thermochemical conversion apparatus 1 according to the above-described embodiment, the solid fuel in the thermochemical conversion reaction reactor C is set by setting the concentration of electrons to be injected into the oxidizing agent to 500 / cc or more. The thermochemical conversion of the fuel can be further promoted.

<Second embodiment>
Next, the configuration of the thermochemical conversion device 1A according to the second embodiment of the present invention will be described with reference to FIG. The thermochemical conversion device 1A according to the present embodiment is a modification of the configurations of the electron generator 50 and the electron concentration measuring device 60 of the thermochemical conversion device 1 according to the first embodiment. Since it is substantially the same as the first embodiment, different configurations will be mainly described, and common configurations will be designated by the same reference numerals and detailed description thereof will be omitted.

In the thermochemical conversion device 1A according to the present embodiment, as shown in FIG. 3, both the electron generator 50A and the electron concentration measuring device 60A are attached (removably) to the outside of the oxidant supply pipe 20. It is provided inside the housing H. The electrons generated by the electron generator 50A are mixed with the oxidant taken into the housing H and supplied to the inside of the oxidant supply pipe 20 through the holes provided in the oxidant supply pipe 20. The electron concentration measuring device 60A measures the concentration of electrons in the housing H.

The thermochemical conversion method (method of supplying an oxidizing agent into the thermochemical conversion reaction reactor C to thermochemically convert a solid fuel) using the thermochemical conversion apparatus 1A according to the present embodiment is first. Since it is the same as the thermochemical conversion method in the embodiment, detailed description thereof will be omitted.

When the thermochemical conversion device 1A according to the above-described embodiment is adopted, the same operation and effect as the thermochemical conversion device 1 according to the first embodiment can be obtained. Further, in the thermochemical conversion device 1A according to the present embodiment, since both the electron generator 50A and the electron concentration measuring device 60A are provided inside the common housing H, they are generated by the electron generator 50A. The electron concentration immediately after the electron concentration (before being supplied to the oxidizing agent supply tube 20) can be measured by the electron concentration measuring device 60A. Also in this embodiment, the electrons generated by the electron generator 50A so that the concentration of electrons in the oxidant immediately before flowing into the oxidant inlet of the thermochemical conversion reaction reactor C is 500 / cc or more. The concentration of the above is set relatively high (for example, about 50,000 / cc).

<Third embodiment>
Next, the configuration of the thermochemical conversion device 1B according to the third embodiment of the present invention will be described with reference to FIG. The thermochemical conversion device 1B according to the present embodiment is obtained by changing the position of the housing H of the thermochemical conversion device 1A according to the second embodiment, and the other configurations are substantially the same as those of the second embodiment. Since they are the same, different configurations will be mainly described, and common configurations will be designated by the same reference numerals and detailed description thereof will be omitted.

In the thermochemical conversion device 1B according to the present embodiment, as shown in FIG. 4, both the electron generator 50B and the electron concentration measuring device 60B are attached (removably) to the outside of the oxidant supply pipe 20. It is provided inside the housing H. Similar to the second embodiment, the electrons generated by the electron generator 50B are mixed with the oxidant taken into the housing H, and the oxidant supply pipe 20 is passed through the hole provided in the oxidant supply pipe 20. Supplied inside. The electron concentration measuring device 60B measures the concentration of electrons in the housing H.

In the present embodiment, one side surface of the housing H accommodating the electron generator 50B and the electron concentration measuring device 60B is a specific portion of the side wall of the thermochemical conversion reaction furnace C (a portion provided with an oxidant intake). The other side surface of the housing H is connected to the oxidant supply pipe 20. Then, the electron-containing oxidizing agent flowing out from the oxidizing agent outlet provided on one side surface of the housing H is supplied to the thermochemical conversion reaction furnace C. That is, in the present embodiment, the oxidant supply pipe 20 is connected to the thermochemical conversion reaction furnace C via the housing H.

In the first and second embodiments, the oxidant supply pipe 20 is interposed between the electron generators 50 and 50A and the thermochemical conversion reaction furnace C, and the electron concentration decreases toward the downstream side. On the other hand, in the present embodiment, the electron generator 50B in the housing H arranged in the vicinity of the thermochemical conversion reaction furnace C immediately before flowing into the oxidant intake of the thermochemical conversion reaction furnace C. Electrons can be injected into the oxidant.

The thermochemical conversion method (method of supplying an oxidizing agent into the thermochemical conversion reaction reactor C to thermochemically convert a solid fuel) using the thermochemical conversion apparatus 1B according to the present embodiment is first. Since it is the same as the thermochemical conversion method in the second embodiment, detailed description thereof will be omitted, but in the present embodiment, it flows into the oxidizing agent inlet of the thermochemical conversion reaction reactor C in the electron injection step. It is possible to inject electrons into the oxidant immediately before the chemical treatment.

When the thermochemical conversion device 1B according to the above-described embodiment is adopted, the same action and effect as those of the thermochemical conversion devices 1.1A according to the first and second embodiments can be obtained. Further, in the thermochemical conversion device 1B according to the present embodiment, since both the electron generator 50B and the electron concentration measuring device 60B are provided inside the common housing H, they are generated by the electron generator 50B. The concentration of electrons immediately after being made can be measured by the electron concentration measuring device 60B. Further, in the thermochemical conversion apparatus 1B according to the present embodiment, since the electrons are injected into the oxidant immediately before flowing into the oxidant intake of the thermochemical conversion reaction furnace C, the electrons are the thermochemical conversion reaction furnace. The decrease in electron concentration until it flows into C can be suppressed as much as possible.

<Fourth Embodiment>
Next, the configuration of the thermochemical conversion device 1C according to the fourth embodiment of the present invention will be described with reference to FIG. The thermochemical conversion device 1C according to the present embodiment has the positions of the flow meter 30, the electron generator 50, the electron concentration measuring device 60, etc. of the thermochemical conversion device 1 according to the first embodiment changed. Since the other configurations are substantially the same as those of the first embodiment, different configurations will be mainly described, and common configurations will be designated by the same reference numerals and detailed description thereof will be omitted.

In the thermochemical conversion device 1C according to the present embodiment, the electron generator 50C is set in the suction unit of the oxidant supply machine 10, and the oxidant flowing out from the oxidant supply machine 10 may contain electrons. You can do it. Further, in the present embodiment, the flow meter 30C is arranged on the downstream side of the oxidant preheater 40, and the electron concentration measuring instrument 60C is arranged near the thermochemical conversion reaction furnace C. Thereby, the flow rate of the oxidant in the vicinity of the middle stream of the oxidant supply pipe 20 can be measured, and the electron concentration of the oxidant immediately before flowing into the oxidant inlet of the thermochemical conversion reaction reactor C can be measured. Can be done.

In this embodiment, since the electron generator 50C is arranged on the upstream side of the oxidant preheater 40, the heat resistant temperature of the electron generator 50C is not considered (that is, the heat resistant temperature of the electron generator 50C is set. The air can be heated by the oxidant preheater 40 (up to temperatures above).

The thermochemical conversion method (method of supplying an oxidizing agent into the thermochemical conversion reaction reactor C to thermochemically convert a solid fuel) using the thermochemical conversion device 1C according to the present embodiment is first. Since it is the same as the thermochemical conversion method in the embodiment, detailed description thereof will be omitted, but in the present embodiment, the electron injection step can be carried out at the same time as the oxidant supply step. Further, in the present embodiment, in the oxidant heating step, the air can be heated by the oxidant preheater 40 to a temperature exceeding the heat resistant temperature of the electron generator 50C.

When the thermochemical conversion device 1C according to the above-described embodiment is adopted, the same operation and effect as the thermochemical conversion device 1 according to the first embodiment can be obtained. Also in this embodiment, the electrons generated by the electron generator 50C so that the concentration of electrons in the oxidant immediately before flowing into the oxidant inlet of the thermochemical conversion reaction reactor C is 500 / cc or more. The concentration of the above is set relatively high (for example, about 50,000 / cc).

<Fifth Embodiment>
Next, the configuration of the thermochemical conversion device 1D according to the fifth embodiment of the present invention will be described with reference to FIG. The thermochemical conversion device 1D according to the present embodiment omits the electron concentration measuring device 60 and the like of the thermochemical conversion device 1 and the like according to the first embodiment, and the other configurations are the first embodiment. Since they are substantially the same as the above, different configurations will be mainly described, and common configurations will be designated by the same reference numerals and detailed description thereof will be omitted.

The thermochemical conversion device 1D according to the present embodiment does not include the electron concentration measuring device 60 or the like adopted in the first embodiment or the like. Therefore, in the thermochemical conversion method using the thermochemical conversion device 1D according to the present embodiment, the electron concentration measuring step carried out in the first embodiment and the like and the electron generation based on the measured electron concentration. The electron concentration adjusting step of feedback-controlling the vessel 50 is not performed.

Instead of performing feedback control based on the electron concentration, the control unit 70D in the present embodiment describes the elements described in the first embodiment (volume of thermochemical conversion space, type of solid fuel, thermochemical conversion reaction temperature). Or, the electron concentration is set based on the number of electrons generated per electron generator 50 (product standard value), etc., the set number of generated electrons is generated by the electron generator 50, and the oxidizer is generated from the electron generator 50. In addition to injecting electrons into the supply pipe 20, the concentration of electrons injected into the oxidant from the electron generator 50 is controlled according to the flow rate measured by the flow meter 30.

When the thermochemical conversion device 1D according to the above-described embodiment is adopted, the same operation and effect as the thermochemical conversion device 1 according to the first embodiment can be obtained. Also in this embodiment, the electrons generated by the electron generator 50 are generated so that the concentration of electrons in the oxidant immediately before flowing into the oxidant inlet of the thermochemical conversion reaction reactor C is 500 / cc or more. The concentration of the above is set relatively high (for example, about 50,000 / cc).

In each of the above embodiments, each step of the thermochemical conversion method (electron concentration setting step S1, oxidant supply step S2, oxidant heating step S3, electron injection step S4, electron concentration measuring step S5, electron concentration). Although an example in which the control unit 70 sends a control signal to operate various devices in the adjustment step S6) is shown, the user may operate and operate the various devices. That is, the thermochemical conversion method according to the present invention is not limited to the method automatically performed by a specific device, but also includes a method performed by a user's operation.

Here, each embodiment of the present invention will be described.

<Example 1>
As the thermochemical conversion apparatus in this embodiment, an apparatus having the same configuration as that of the first embodiment was adopted. A high-pressure blower (manufactured by Showa Denki Co., Ltd.) is used as the oxidant supply machine, a mass flow meter (manufactured by Azbil Co., Ltd.) is used as the flow meter, and a negative ion generation unit (manufactured by Andes Electric Co., Ltd.) is used as the electron generator. An air ion counter (manufactured by Andes Electric Co., Ltd.) was adopted as the concentration measuring instrument, and a processor (manufactured by Ecocle Japan Co., Ltd.) that integratedly controls these devices was adopted as the control unit. The negative ion generation unit (trade name: ITM-F301) can generate electrons having a concentration of 500,000 / cc or more. A ^1m3 reactor tester (manufactured by Ecocle Japan) is used as the thermochemical conversion reaction furnace, wood chips with a specific gravity of 0.18 are used as the solid fuel, and an inner diameter of 60 mm is used as the oxidant supply pipe. Adopted the steel pipe of. The distance from the negative ion generation unit to the 1 ^m3 furnace tester was 45 cm. The oxidant preheater was omitted.

In this embodiment, first, a high-pressure blower is operated by a processor, an oxidant (air) is supplied to a ¹ m3 furnace tester via a steel pipe, and the high-pressure blower is operated based on the flow rate measured by a mass flow meter. By controlling the above, an oxidant having a flow rate of 210 L / min was supplied to the 1 ^m3 furnace tester. Next, the negative ion generation unit was operated by the processor, and electrons having a predetermined concentration (500,000 / cc) or more were generated by the negative ion generation unit, and the electrons were injected into the steel pipe. In this embodiment, the negative ion generating unit is attached to the outer wall of the steel pipe, and the terminal of the negative ion generating unit is directly inserted into the hole provided in the outer wall of the steel pipe to inject electrons into the steel pipe. I made it. Next, the air ion counter is operated by the processor, the concentration of electrons contained in the oxidant flowing through the steel pipe is measured, and while monitoring whether the measured concentration is equal to or higher than a predetermined threshold (500 / cc). The solid fuel was gasified, and the control of various devices was stopped after the lapse of a preset operating time.

In this example, the production rates (mg / sec) of carbon dioxide (CO ₂ ), carbon monoxide (CO), methane (CH ₄ ), and hydrogen (H ₂ ) produced by gasification of solid fuel were measured. However, the time history as shown by the curve A was obtained in each of FIGS. 7 to 10. The temperature inside the 1 ^m3 furnace tester in this example was 900 ° C. at the bottom of the furnace.

<Example 2>
As the thermochemical conversion apparatus in this embodiment, an apparatus having the same configuration as that in the first embodiment is adopted, and as the thermochemical conversion reactor, a 1 L small reactor (hereinafter referred to as “small reactor”) is adopted. It was adopted. Cellulose having a volume of 20 cm ³ was used as the solid fuel, and a steel pipe having an inner diameter of 16 mm was used as the oxidant supply pipe. The distance from the negative ion generation unit to the small reactor was 5 cm.

In this embodiment, first, an oxidant (air) is supplied from a high-pressure cylinder to a small reactor via a steel pipe, and the flow rate is adjusted by a needle valve based on the flow rate measured by a mass flow meter. An oxidant of 0.028 mL / min was supplied to the small reactor. Next, the negative ion generation unit was operated by the processor, and electrons having a predetermined concentration (500,000 / cc) or more were generated by the negative ion generation unit, and the electrons were injected into the steel pipe. Next, the air ion counter is operated by the processor, the concentration of electrons contained in the oxidant flowing through the steel pipe is measured, and while monitoring whether the measured concentration is equal to or higher than a predetermined threshold (500 / cc). The solid fuel was gasified, and the control of various devices was stopped after the lapse of a preset operating time.

In this example, when the production rate (mg / sec) of carbon dioxide (CO ₂ ) produced by the gasification of the solid fuel supplied to the small reactor was measured, the time as shown by the curve A in FIG. 11 was measured. The history was obtained. Further, in this embodiment, the average production rate of carbon dioxide (CO ₂ ), hydrogen (H ₂ ), and ethylene (C ₂ H ₄ ) produced by gasification of the solid fuel supplied to the small reactor is shown. As a result of calculation using a simulation model simulating the configuration of the example, gray (center) bar graphs of FIGS. 12A and 12B were obtained. The temperature inside the small reactor in this example was 500 ° C.

<Example 3>
In this example, using the same simulation model as in Example 2, the electron concentration in the oxidant was set to be an order of magnitude higher (5000 / cc) than in Example 2. In this example, the average production rates of carbon dioxide (CO ₂ ), hydrogen (H ₂ ), and ethylene (C ₂ H ₄ ) produced by gasification of solid fuel were calculated. A gray bar graph with hatching (second from the right) of B) was obtained. The temperature inside the small reactor in this example was 500 ° C.

<Example 4>
In this example, using the same simulation model as in Example 2, the electron concentration in the oxidant was set to be an order of magnitude higher (50,000 / cc) than in Example 3. In this embodiment, the average production rates of carbon dioxide (CO ₂ ), hydrogen (H ₂ ), and ethylene (C ₂ H ₄ ) produced by gasification of solid fuel were calculated. A black-painted (far right) bar graph of B) was obtained. The temperature inside the small reactor in this example was 500 ° C.

<Example 5>
In this example, the same simulation model as in Example 2 was used, and the electron concentration in the oxidizing agent was set to be lower than that in Example 2 (300 / cc). In this example, the average production rates of carbon dioxide (CO ₂ ), hydrogen (H ₂ ), and ethylene (C ₂ H ₄ ) produced by gasification of solid fuel were calculated. A white bar graph with hatching (second from the left) in B) was obtained. The temperature inside the small reactor in this example was 500 ° C.

<Example 6>
In this example, using the same simulation model as in Example 2, the electron concentration in the oxidant was set to be lower than that in Example 5 (100 cells / cc or more). In this embodiment, the average production rates of carbon dioxide (CO ₂ ), hydrogen (H ₂ ), and ethylene (C ₂ H ₄ ) produced by gasification of solid fuel were calculated. A blank (leftmost) bar graph of B) was obtained. The temperature inside the small reactor in this example was 500 ° C.

<Comparative Example 1>
Using the same equipment as in Example 1 except that the negative ion generation unit was omitted, the high-pressure blower was operated by the processor, the oxidant was supplied to the 1 m ³ furnace tester via the steel pipe, and the mass flow was increased. By controlling the operation of the high-pressure blower based on the flow rate measured by the meter ^, an oxidizer with a flow rate of 210 L / min is supplied to the 1 m3 furnace tester to gasify the solid fuel, and the elapsed operating time set in advance. The control of various devices was stopped. The production rates (mg / sec) of carbon dioxide (CO ₂ ), carbon monoxide (CO), methane (CH ₄ ), and hydrogen (H ₂ ) produced by gasification of solid fuel were measured. The time history as shown by the curve B was obtained in each of FIGS. 10. At this time, the temperature inside the 1 m ³ furnace tester was 900 ° C. at the bottom of the furnace.

<Comparative Example 2>
Using the same equipment as in Example 2 except that the negative ion generation unit was omitted, the oxidant was supplied from the high-pressure valve to the small reactor via the steel pipe, and based on the flow rate measured by the mass flow meter. By adjusting the flow rate with the needle valve, an oxidizer with a flow rate of 0.028 mL / min is supplied to the small reactor to gasify the solid fuel, and the control of various devices is stopped after the elapsed preset operating time. I let you. When the production rate (mg / sec) of carbon dioxide (CO ₂ ) produced by the gasification of the solid fuel was measured, the time history as shown by the curve B in FIG. 11 was obtained. At this time, the temperature inside the small reactor was 500 ° C.

<Discussion>
As is clear from the above results, in each example in which electrons were injected into the oxidant for thermochemical conversion of solid fuel, carbon dioxide (CO ₂ ) and carbon monoxide (CO) were higher than in each comparative example. , Methane (CH ₄ ) and hydrogen (H ₂ ) were significantly increased (FIGS. 7 to 11). Further, when the electron concentration injected into the oxidant is increased to 500 / cc or more, the average production rate of each produced gas (carbon dioxide (CO ₂ ), hydrogen (H ₂ ), ethylene (C ₂ H ₄ )) becomes higher. It was revealed that the increase was remarkable (Fig. 12).

The present invention is not limited to each of the above embodiments, and those embodiments to which a person skilled in the art has appropriately modified the design are also included in the scope of the present invention as long as they have the features of the present invention. To. That is, each element provided in each of the above embodiments, its arrangement, material, condition, shape, size, and the like are not limited to those exemplified, and can be appropriately changed. Further, the elements included in each of the above embodiments can be combined as much as technically possible, and the combination thereof is also included in the scope of the present invention as long as the features of the present invention are included.

1.1A, 1B, 1C, 1D ... Thermochemical conversion device 10 ... Oxidizing agent feeder (oxidizing agent flow generating means)
20 ... Oxidizing agent supply pipe 30 / 30C ... Flow meter (Oxidizing agent flow measuring means)
40 ... Oxidizing agent preheater (oxidizing agent heating means)
50 ・ 50A ・ 50B ・ 50C ... Electron generator (electron injection means)
70 / 70D ... Control unit (electron concentration setting means, electron concentration control means)
S1 ... Electron concentration setting process S2 ... Oxidizing agent supply process (Oxidizing agent flow rate measurement process)
S3 ... Oxidizing agent heating process S4 ... Electron injection process (electron concentration control process)
C ... Thermochemical conversion reactor

Claims (14)

1. Thermochemical conversion A method of thermochemically converting solid fuel by supplying an oxidizer into the reactor.
   A thermochemical conversion method comprising an electron injection step of injecting electrons of a predetermined concentration into an oxidizing agent supplied into the thermochemical conversion reaction furnace.
2. The concentration of electrons injected into the oxidant is determined based on at least one of the volume of the thermochemical conversion space in the thermochemical conversion reaction furnace, the type of solid fuel, and the thermochemical conversion reaction temperature. The thermochemical conversion method according to claim 1, which comprises a step of setting an electron concentration to be set.
3. An oxidant flow rate measuring step for measuring the flow rate of the oxidant supplied into the thermochemical conversion reaction furnace, and a step of measuring the oxidant flow rate.
   An electron concentration control step that controls the concentration of electrons injected into the oxidant according to the flow rate measured in the oxidant flow measurement step, and an electron concentration control step.
   The thermochemical conversion method according to claim 1 or 2, wherein the method comprises.
4. The thermochemical conversion reactor is equipped with an oxidant inlet that receives an oxidant supply from the outside.
   The thermochemical conversion method according to any one of claims 1 to 3, wherein in the electron injection step, electrons are injected into the oxidant immediately before flowing into the oxidant inlet.
5. The claim comprises an oxidant heating step of heating the oxidant supplied into the thermochemical conversion reaction furnace by the sensible heat recovered from the combustion gas discharged from the thermochemical conversion reaction furnace or the flammable gas. The thermochemical conversion method according to any one of 1 to 4.
6. The thermochemical conversion method according to any one of claims 1 to 5, wherein in the electron injection step, electrons having a concentration of 500 cells / c or more are injected into an oxidizing agent.
7. Thermochemical conversion A device that thermochemically converts solid fuel by supplying an oxidizer into the reactor.
   A thermochemical conversion apparatus comprising an electron injection means for injecting electrons of a predetermined concentration into an oxidizing agent supplied into the thermochemical conversion reaction furnace.
8. The concentration of electrons injected into the oxidant is determined based on at least one of the volume of the thermochemical conversion space in the thermochemical conversion reaction furnace, the type of solid fuel, and the thermochemical conversion reaction temperature. The thermochemical conversion apparatus according to claim 7, further comprising an electron concentration setting means for setting.
9. An oxidant flow rate measuring means for measuring the flow rate of the oxidant supplied into the thermochemical conversion reaction furnace, and an oxidant flow rate measuring means.
   An electron concentration control means for controlling the concentration of electrons injected into the oxidant according to the flow rate measured by the oxidant flow rate measuring means, and an electron concentration control means.
   7. The thermochemical conversion apparatus according to claim 7.
10. Oxidizing agent flow generating means to generate oxidizing agent flow and
    An oxidant supply pipe for connecting the oxidant flow generating means and the thermochemical conversion reaction furnace is provided.
    The thermochemical conversion device according to any one of claims 7 to 9, wherein the electron injection means is installed in the oxidizing agent supply pipe.
11. The thermochemical conversion reactor has an oxidant inlet that receives an oxidant supply from the outside.
    The thermochemical conversion device according to claim 10, wherein the electron injection means is installed in the oxidant supply pipe so as to inject electrons into the oxidant immediately before flowing into the oxidant inlet.
12. A means for generating an oxidant flow for generating an oxidant flow toward the thermochemical conversion reaction furnace is provided.
    The thermochemical conversion device according to any one of claims 7 to 9, wherein the electron injection means is installed in the oxidant flow generating means.
13. The claim comprises an oxidant heating means for heating the oxidant supplied into the thermochemical conversion reaction furnace by the sensible heat recovered from the combustion gas discharged from the thermochemical conversion reaction furnace or the flammable gas. The thermochemical conversion apparatus according to any one of 7 to 12.
14. The thermochemical conversion apparatus according to any one of claims 7 to 13, wherein the electron injection means injects electrons having a concentration of 500 cells / cc or more into an oxidizing agent.
    

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