JP2003213269A - High temperature carbonization installation and high temperature carbonization method - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a high temperature carbonization installation that can produce a carbonization product whose surface area is enlarged to increase a calorific value and which has high carbon fixation stability, can shorten a heating time in a carbonization oven to reduce a passing time in the carbonization oven, can be downsized, and hardly causes the trouble of tar adhesion to a piping system for guiding evaporated gases. <P>SOLUTION: The high temperature carbonization installation comprises a gas flow passage 4 through which the first exhaust gas (m) is exhausted from a gas-producing oven 1 for producing the first gas (m) from a material (a1) to be treated, or a gas flow passage 5 through which the second exhaust gas (j) is exhausted from a gas burning oven 2 for burning the material (a1) to produce the second gas (j), and a carbonization oven 6 formed to introduce a material (a2) to be carbonized thereinto and which is transmitted with heat from the exhaust gas (j) passing through the gas flow passage 5, and is formed to carbonize the material (a2) to be carbonized at a material (a2) peripheral temperature of ≥700°C due to the transmitted heat. <P>COPYRIGHT: (C)2003,JPO

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a high-temperature carbonization apparatus and a high-temperature carbonization method for carbonizing an object to be carbonized by an exhaust gas discharged from a gas generation furnace or a gas combustion furnace, and particularly to a high-temperature carbonization method. The present invention relates to a high-temperature carbonization apparatus and a high-temperature carbonization method for carbonization and carbonization.

[0002]

2. Description of the Related Art A conventional carbonization apparatus is equipped with a carbonization furnace having a screw conveyor for conveying wastes which are carbonization targets, and the carbonization furnace intersects at right angles with a gasification furnace for generating a gas of 600 ° C. or less. It was placed horizontally so that The dry distillation furnace, for example, takes in solid waste, conveys it through the inside of the dry distillation furnace with a screw conveyor, and uses the gas in the gasification furnace that comes into contact with the dry distillation furnace as a heat source to dry-distill the waste at a temperature of 600 ° C or lower. And carbonized. Wood vinegar was recovered from the volatile gas generated by carbonization of the waste.

[0003]

However, in the above carbonization apparatus, the surface area of the carbide is small, the calorific value is small, and the carbon fixation stability is low. Also, it is necessary to lengthen the heating by the carbonization furnace, lengthen the carbonization furnace,
The time required for the waste to pass through the carbonization furnace and to be heated has to be lengthened, which has been a cause of enlargement of the apparatus. In the piping system that introduces the volatile gas from the carbonizer outlet to the wood vinegar liquid recovery device, there was a case where the piping system was clogged due to the adhesion of the tar component generated by the carbonization of the waste.

Therefore, the present invention provides a carbonization apparatus and a carbonization method capable of increasing the surface area of carbides to increase the amount of heat generation and producing carbides having a high carbon fixation stability, and the heating time by a carbonization furnace. An object of the present invention is to provide a carbonization device and a carbonization method which can be shortened to downsize the device, and in which a trouble of adhesion of a tar component is unlikely to occur in a piping system for guiding a volatile gas.

[0005]

In order to achieve the above object, the high temperature carbonization apparatus 6 according to the invention according to claim 1 is an object to be treated as shown in, for example, FIG. 1, FIG. 2, FIG. 11 and FIG. The gas passage 5 through which the exhaust gas m discharged from the gas generation furnace 2 that generates the first gas m from a1 passes, or the object to be treated a1
A gas flow passage 305 through which the exhaust gas j discharged from the gas combustion furnace 303 that burns the gas to generate the second gas j; and the exhaust gas j into which the substance to be carbonized a2 is introduced and which passes through the gas flow passages 5 and 305 And a dry distillation furnace 37, 337 configured to transfer heat from the above; the transferred heat causes the ambient temperature of the object to be carbonized a2 to be 700 ° C. or higher, and the object to be carbonized a2
Is carbonized by carbonization. The combustion in the present invention includes partial combustion and complete combustion (the same applies hereinafter).

According to this structure, the transferred heat raises the ambient temperature of the object to be carbonized a2 to 700 ° C. or more, and carbonizes the object to be carbonized a2 by carbonization, so that the surface area of the carbonized material u in which the object to be carbonized a2 is carbonized becomes large. The calorific value increases, and the tar content is deposited and solidified on the carbide u, so that the carbon fixation stability increases. Further, since the heating time is shortened, the device can be downsized. In addition, since the tar content is deposited and solidified on the carbide u, the tar content in the volatile gas g generated from the material to be carbonized a2 is reduced by carbonization, and the problem of tar adhesion in the piping system leading the volatile gas g is reduced. Hard to occur.

Normally, the material to be carbonized a2 is heated in the dry distillation furnace 37 without directly contacting the exhaust gases m and j (external heating type). However, the gas generation furnace 2 is a fluidized bed gasification furnace, and for forming a fluidized bed, the fluidized gas that fluidizes the fluidized medium does not contain oxygen, such as steam (e.g.
It may contain 2%. ) Is used, when the generated gas generated in the fluidized bed gasification furnace is used as the exhaust gas m, the exhaust gas m is configured to enter the carbonization furnace 37, and the carbonized material a2 is directly discharged into the exhaust gas m. It is also possible to carbonize it by exposing it to. In this case, since the carbonized material a2 is directly exposed to the exhaust gas, the heat quantity of the exhaust gas can be efficiently used to
Can be carbonized.

The high-temperature carbonization device 6 is, for example, as shown in FIGS. 1 and 2, discharged from a gas generation furnace 2 for generating a gas from an object to be treated a1 and further introduced into a second gas combustion furnace 3 for partial combustion. Or a gas flow path 5 through which exhausted exhaust gas j completely burned and discharged; a carbonization object a2 is introduced into the inside, and heat is transferred from the exhaust gas j passing through the gas flow path 5 The furnace 37 may be included; the ambient temperature of the object to be carbonized a2 may be 700 ° C. or higher by the transferred heat, and the object to be carbonized a2 may be carbonized by carbonization.

A dry distillation furnace configured to transfer heat from the exhaust gas passing through the gas flow path includes a dry distillation furnace arranged in the gas flow path or a dry distillation furnace arranged so as to intersect with the gas flow path. A furnace, or a carbonization furnace arranged in contact with the gas flow path, or a carbonization furnace arranged in proximity to the gas flow path, or configured to be heated by a heat transfer medium heated by the gas flow path There is a dry distillation furnace.

High-temperature carbonization apparatus 6 according to the invention of claim 2
For example, as shown in FIGS. 1 and 2, the high-temperature exhaust gas m discharged from the gas generation furnace 2 that generates gas from the object to be processed a1 or the gas combustion furnace 3 that burns the object to be processed a1.
A dry distillation furnace 37 arranged so as to come into contact with the discharged high temperature exhaust gas j is provided; the exhaust gas m, j coming into contact with the dry distillation furnace 37 is a substance a to be carbonized introduced into the dry distillation furnace 37.
The ambient temperature of 2 is set to 700 ° C. or higher, and the object to be carbonized a2 is carbonized by carbonization.

According to this structure, the exhaust gas m, j contacting the carbonization furnace 37 sets the ambient temperature of the carbonized material a2 introduced into the carbonization furnace 37 to 700 ° C. or higher, and carbonizes the carbonized material a2 by carbonization. Therefore, the surface area of the carbide u obtained by carbonizing the object to be carbonized a2 increases, the amount of heat generated increases, and the tar content is deposited and solidified on the carbide u, so that the carbon fixation stability increases. Further, since the heating time is shortened, the device can be downsized. Further, since the tar component is deposited and solidified on the carbide u, the volatile gas g generated from the carbonized material a2 by carbonization.
The tar content in the inside is reduced, and the problem of tar content adhesion is less likely to occur in the piping system that guides the volatile gas g.

As shown in FIGS. 1 and 2, for example, the high-temperature carbonization apparatus 6 is discharged from a gas generation furnace 2 for generating a gas from an object to be treated a1 and is further introduced into a second gas combustion furnace 3 for partial combustion. Alternatively, a dry distillation furnace 37 arranged so as to come into contact with the exhausted hot exhaust gas j that has been completely burned is provided; the exhaust gas j that comes into contact with the dry distillation furnace 37 is a substance a2 to be carbonized introduced into the dry distillation furnace 37. The ambient temperature may be 700 ° C. or higher, and the carbonized material a2 may be carbonized by carbonization.

High-temperature carbonization apparatus 6 according to the third aspect of the invention
In the high temperature carbonization device 6 according to claim 1 or 2, for example, as shown in FIG. 2, a moisturizing device 46 for moisturizing the material to be carbonized a2 before carbonization is provided.

According to this structure, since the moisturizing device 46 is provided, the moisturizing device 46 moistens the material to be carbonized a2, and the activation effect of the moistening increases the surface area of the carbide u carbonized from the material to be carbonized a2. However, the composition of the generated volatile gas g can be improved and the molecular weight can be reduced. It should be noted that the dry distillation is a concept of heating a solid in a state where there is usually no liquid, but a concept including heating of the wetted object a2.

High temperature carbonization apparatus 6 according to the invention of claim 4
The high-temperature carbonization apparatus 6 according to any one of claims 1 to 3, is provided with two dry distillation furnaces 237A and 237A as shown in FIG. 6, for example. After being transported inside the 237A, the other dry distillation furnace 237
It is configured to be transported inside B.

With this structure, the carbonization furnace 237A,
Since two B are provided, the residence time in the furnace can be extended and the amount of the carbide u to be carbonized from the material to be carbonized a2 can be increased.

High-temperature carbonization apparatus 6 according to the invention of claim 5
In the high temperature carbonization apparatus 6 according to any one of claims 1 to 4, as shown in, for example, FIG. 1 and FIG.
A control device 17 for controlling the ambient temperature is provided; a waste heat boiler 10 for recovering heat from the exhaust gas j is arranged downstream of the dry distillation furnace 37 with respect to the flow of the exhaust gas j; The exhaust gas flow path 14 for guiding the discharged exhaust gas j to the upstream side of the dry distillation furnace 37 and mixing with the exhaust gas j on the upstream side of the dry distillation furnace 37 is arranged; The ambient temperature is controlled by controlling the gas flow rate.

According to this structure, since the control device 17 is provided, the control device 17 controls the ambient temperature of the carbonized material a2 in the carbonization furnace 37 by controlling the flow rate of the exhaust gas flowing through the exhaust gas passage 14. can do. It is desirable that the control device 17 controls the ambient temperature to be 700 to 1000 ° C, and more preferably 800 to 1000 ° C.

High temperature carbonization apparatus 6 according to the invention of claim 6
In the high temperature carbonization apparatus 6 according to any one of claims 1 to 5, for example, as shown in FIGS. 1 and 3,
The carburizing object a2 is provided with a carrying device 38 for carrying it through the inside of the carbonization furnace 37; the carrying device 38 is carrying the carburizing object a2.
It has a stirring section 81 for stirring 2.

According to this structure, the carrying device 38 is provided, and the carrying device 38 has the stirring section 81 for stirring the carburized object a2 being transferred. Therefore, the carburized object a2 carried by the carrier device 38 is stirred. The agglomerate a2 to be stirred is heated uniformly by the stirring by the portion 81, and a high-quality carbide u can be produced from the acarbide a2.

High-temperature carbonization apparatus 6 according to the invention of claim 7
The high temperature carbonization apparatus 6 according to any one of claims 1 to 6 is provided with a cooling device 41 for cooling the carbonized object a2 as shown in FIG. 2, for example.

According to this structure, since the cooling device 41 is provided, the carbonized object a2 (carbide u) can be cooled, and the temperature of the carbonized object a2 can be lowered to the atmospheric temperature, which is easy to handle. It can be the temperature.

High-temperature carbonization apparatus 6 according to the invention of claim 8
In the high temperature carbonization device 6 according to any one of claims 1 to 7, for example, as shown in FIG. 2, steam s for removing tar adhering in the carbonization furnace 37 is removed by the carbonization furnace 37.
A steam supply device 49 for supplying the

With this structure, the steam supply device 49
Since the steam supply device 49 is provided, the tar adhering in the dry distillation furnace 37 can be blown with steam s to remove the tar.

High temperature carbonization apparatus 6 according to the invention of claim 9
In the high-temperature carbonization apparatus 6 according to any one of claims 1 to 8, for example, as shown in FIG. 2, the wood vinegar liquid t contained in the volatile matter gas g generated in the carbonization furnace 37 is recovered. The recovery device 45 is further configured to recover the tar contained in the volatile matter gas g.

With this structure, the wood vinegar liquid t and the tar contained in the volatile gas g can be recovered.

In order to achieve the above object, a high temperature carbonization method according to a tenth aspect of the present invention, for example, as shown in FIG. 1, produces a first gas m from an object to be treated a1 and a first gas m.
And a combustion discharge step of burning the object a1 to generate the second gas j and discharging the second gas j as the exhaust gas j; An ambient temperature of the carbide a2 is set to 700 ° C. or higher, and a carbonization carbonization step of carbonizing and carbonizing the carbonized material a2 is provided.

The high-temperature carbonization method is, for example, as shown in FIG. 1, a generation and discharge step of generating a first gas from an object to be treated a1 and discharging the first gas m as an exhaust gas m; A second combustion discharging step of partially or completely burning the exhaust gas m generated to generate a second gas j and discharging the second gas j as the exhaust gas j; and the exhaust gas j discharged in the second combustion discharging step. The ambient temperature of the carbonized material a2 is set to 700 ° C. or higher, and the carbonized material a2 is carbonized by carbonization.
A dry distillation carbonization step may be provided. Further, the carbonized material a2 is
A moistening step of moistening before dry distillation may be provided.

The high temperature carbonization method according to the present invention according to claim 11 is the high temperature carbonization method according to claim 10, wherein, for example, as shown in FIG. 1, a moistening step of moisturizing the material to be carbonized a2 before carbonization is carried out. Prepare

[0030]

BEST MODE FOR CARRYING OUT THE INVENTION Embodiments of the present invention will be described below with reference to the drawings. In each drawing, the same or corresponding members are designated by the same reference numerals, and duplicate description will be omitted.

FIG. 1 is a gasification and melting system 1 to which a high temperature carbonization apparatus 6 according to a first embodiment of the present invention is attached.
It is a block diagram of.

The gasification and melting system 1 combusts the fluidized bed gasification furnace 2 as a gas production furnace for producing the produced gas m as the first gas or as the exhaust gas, and the produced gas m to combust the second gas. As exhaust gas (combustion gas)
A swirling melting furnace 3 as a gas combustion furnace for generating j, and a first product gas m guided from the fluidized bed gasification furnace 2 to the swirling melting furnace 3.
The duct 4, the radiant boiler 7, the high temperature air superheater 8, the second duct 5 as a gas flow path for guiding the exhaust gas j discharged from the high temperature air superheater 8, and the high temperature provided in the second duct 5. Carbonization device 6, waste heat boiler 10, bag filter 12 for collecting ash h in exhaust gas j, third duct 9 connecting high temperature carbonization device 6 and waste heat boiler 10, and waste heat boiler 10. A fourth duct 11 connecting the bag filter 12 and a fifth duct 13 connecting the bag filter 12 and a suction blower (not shown)
A bypass line 14 as an exhaust gas flow path connecting the fifth duct 13 and the second duct 5, and a bypass line 14
A bypass blower 15 (which is driven by a drive motor (not shown)) provided therein is included.

The fluidized bed gasification furnace 2 is equipped with a screw feeder 21 for supplying the general waste a1 as an object to be processed into the furnace.
Equipped with. In the fluidized bed gasification furnace 2, a fluidized bed of silica sand c is formed on the air dispersion plate 2A by the air b sent to the furnace bottom 22. The general waste a1 is 450 to 650.
By falling into the fluidized bed of silica sand c kept at ℃,
The heated silica sand c and the air b are brought into contact with each other to be rapidly pyrolyzed and gasified to form a product gas m, tar and solid carbon.
Solid carbon is finely pulverized by vigorous agitation of the fluidized bed. Air b on the freeboard 2B of the fluidized bed gasifier 2
Is blown in, and tar and solid carbon are gasified at 650 to 850 ° C. An incombustible discharge port 23 is formed in the furnace bottom 22. Silica sand c and incombustible substance d are discharged from the incombustible substance discharge port 23, and then classified by a classifying device (not shown). Although the incombustibles d include metals such as iron, copper, and aluminum, since they are in a reducing atmosphere in the furnace, they can be recovered in an unoxidized and clean state.

The produced gas m, which has exited from the outlet 24 of the fluidized bed gasification furnace 2 together with the finely divided solid carbon, passes through the first duct 4 and enters from the inlet 25 of the swirl melting furnace 3 to the swirl melting furnace 3. Supplied. The generated gas m is in the primary combustion chamber 3A,
1200 while mixing with preheated air b in swirl flow
Burns at a high temperature of ~ 1500 ° C at high speed. Combustion is inclined 2
Completed in the next combustion chamber 3B. The total amount of ash in solid carbon becomes slag mist due to the high temperature. Most of the slag mist is captured by the molten slag in the furnace wall of the primary combustion chamber 3A by the action of the centrifugal force of the swirling flow. The molten slag sg flowing down the furnace wall enters the secondary combustion chamber 3B and is then discharged from the slag separating section bottom 3C.

A radiant boiler 7 (medium to be heated is steam) is provided vertically above the vertical portion 3D on the downstream side of the slag separating portion bottom portion 3C of the swirl melting furnace 3, and heat is exchanged with the exhaust gas j. It A high temperature air superheater 8 for heating the air b to a high temperature is provided above the radiant boiler 7, and heat is exchanged with the exhaust gas j.

The exhaust gas j exiting from the outlet portion 8A of the high temperature air superheater 8 passes through the second duct 5, and while passing through the second duct 5, the flow direction is changed from the horizontal direction to the vertical downward direction,
Furthermore, the flow direction is changed to the horizontal direction, and the high-temperature carbonization device 6 provided in the horizontal portion 5B of the second duct 5 intersects and contacts. A raw material a2 as a material to be carbonized is supplied to the high temperature carbonization device 6. The exhaust gas j heats the high temperature carbonization device 6,
The ambient temperature of the raw material a2 is 700 ° C. or higher, preferably 800
That is, the temperature of the carbonization gas k which is the gas in the high temperature carbonization apparatus 6 is raised to 700 ° C. or higher, preferably 80 ° C. or higher.
Raise to above 0 ° C. The carbonization gas k is used in the high temperature carbonization device 6
It is a gas that comes into direct contact with the raw material a2 therein to dry-distill and carbonize the raw material. By contacting with the carbonization gas k and heating it, the raw material a
2 becomes a carbide u and is discharged from the high temperature carbonization device 6.

The exhaust gas j that intersects with and comes into contact with the high temperature carbonization device 6 passes through the third duct 9 and passes through the waste heat boiler 10 (the medium to be heated is steam) provided on the downstream side of the high temperature carbonization device 6. The exhaust gas j exiting the waste heat boiler 10 is the waste heat boiler 1
It passes through a bag filter 12 provided on the downstream side of 0 for collecting dust in the exhaust gas j. The exhaust gas j exiting the bag filter 12 passes through the fifth duct 13, further passes through a suction blower (not shown), and further passes through a chimney (not shown) to be discharged to the atmosphere.

A part of the exhaust gas j passing through the fifth duct 13 before passing through the suction blower flows through the bypass line 14 connecting the fifth duct 13 and the vertical portion 5C of the second duct 5,
It is returned to the vertical portion 5C of the second duct 5 and mixes with the exhaust gas j flowing through the vertical portion 5C of the second duct 5. Horizontal part 5B
The temperature of the exhaust gas j is 700 to 100 for the dry distillation gas k.
It is desirable that the heating temperature is 0 ° C., preferably 800 to 1000 ° C.

A carbonization furnace 3 which will be described later and constitutes the high-temperature carbonization device 6.
7 (see FIG. 2), the temperature measuring device 16 for measuring the temperature of the carbonization gas k is provided in the carbonization furnace 37, the automatic control valve 18 is provided in the bypass line 14, and the control device 17 is not installed. It is provided in the illustrated control room. The control device 17 receives the temperature signal p from the temperature measuring device 16 and sends a start signal q for starting the bypass blower 15 to the bypass blower 15 (actually, a drive motor start control panel (not shown)) to start the bypass blower 15. Then, the opening signal r is set so that a predetermined amount of exhaust gas j flows through the automatic control valve 18.
To the automatic control valve 18, and the automatic control valve 18 moves to the horizontal portion 5B.
It is advisable to control the temperature of the exhaust gas j flowing through. In the present embodiment, the predetermined amount means that the exhaust gas j sent from the swirling and melting furnace 3 and the exhaust gas j returned through the bypass line 14 are mixed, and the exhaust gas j after mixing is
The dry distillation furnace 37 (see FIG. 2) is contacted, the heat is transferred from the exhaust gas j to the dry distillation furnace 37, and the temperature of the dry distillation gas k is 700 to 1
The amount is 000 ° C., preferably 800 to 1000 ° C. In this way, the temperature of the exhaust gas j when the temperature is not controlled exceeds 1000 ° C (the maximum temperature suitable for carbonization), or the temperature of the exhaust gas j may exceed 1000 ° C (the maximum temperature suitable for carbonization). The high temperature carbonization device 6 can be arranged in the.

FIG. 2 is a block diagram showing the structure of the high temperature carbonization apparatus 6. The configuration of the high temperature carbonization device 6 will be described with reference to the drawings.

The high temperature carbonization device 6 includes a storage hopper 31 to which the raw material a2 is supplied, a cutting conveyor 32, a drive motor 33 for driving the cutting conveyor 32, a scraping machine 34, and a double damper 36. A carbonization furnace 37, a carbonization conveyor 38 as a transfer device, a drive motor 39 for driving the carbonization conveyor 38, a connecting chute 40, a cooling conveyor 41 as a cooling device, and a drive motor 42 for driving the cooling conveyor 41, It is configured to include a gate valve 43, a collection box 44, and a wood vinegar solution collection device 45 as a collection device.

The storage hopper 31 has an input port 51 with a lid into which the raw material a2 is charged, a hopper body 52 in which the raw material a2 is stored, and a discharge port 53. The raw material a2 charged from the charging port 51 is temporarily stored in the hopper body 52 and discharged from the discharging port 53.

The raw material a2 is preferably solid waste, and solid waste means waste such as municipal solid waste, or compression molding of this waste, waste wood of construction waste, and the waste. Crushed wood materials Waste materials generated during thinning of forests, Crushed waste materials Food processing wastes such as beer squeeze residue, but any waste material containing carbon, such as wood chips Including things that are not things. In addition to these, the general waste a1 (see FIG. 1) may be waste plastic, waste oil, waste tire, or the like.

The slicing conveyor 32 is a biaxial type (not shown in the drawing, uniaxial type) and is horizontally arranged, and has a supply port 54, a conveyor case 55, and a conveyor case 5.
It has a conveyor main body 56 housed inside 5, and a discharge port 57. The discharge port 53 of the storage hopper 31 is connected to the supply port 54, and the raw material discharged vertically downward from the discharge port 53 by its own weight of the raw material a2 is supplied to the cutout conveyor 32 from the supply port 54 and the conveyor main body 56. Is rotated, the sheet is conveyed horizontally in the conveyor case 55 from right to left in the figure, and is horizontally discharged from the discharge port 57. The conveyor main body 56 is rotationally driven by a drive motor 33 attached to the right end of the conveyor case 55 in the figure. The conveyor case 55 has a wetting nozzle 46 as a wetting device.
Is attached, mist-like water w1 is discharged from the wetting nozzle 46, and the raw material a2 being conveyed inside the conveyor case 55 is moistened.

The scraper 34 has a main body storage case 82, a supply port 68 and a discharge port 69 formed in the main body storage case 82, and a scraper main body 83 stored in the main body storage case 82. The supply port 68 is connected to the discharge port 57 of the cutting conveyor 32. The scraper main body 83 is connected to a moving device (not shown), and can be further rotated by a drive motor (not shown) about a rotation axis perpendicular to the plane of the drawing (in the X direction in the drawing). When a bridge (clogging) of the raw material a2 occurs at the discharge port 57 of the cutting conveyor 32, the scraper main body 83 is moved from the left side in the figure in the main body storage case 82 shown by the solid line to the right side shown by the broken line by the moving device. Moving. During the movement, the drive motor starts rotation, and the rotation causes the raw material a2 to drop off from the conveyor main body 56 and scraped. After that, the scraper main body 83 returns to the normal position on the left side in the drawing by the moving device.

FIG. 3 shows a detailed view of the scraper body 83.
The scraper main body 83 is configured to include a hollow shaft 84 and a spiral portion 85 attached to the outer peripheral portion of the hollow shaft 84. The spiral part 85 is composed of two left-handed left spiral parts 85A and B, which are mounted 180 degrees apart from each other,
It is composed of two right-handed right spiral parts 85C and 85D which are attached so as to be offset from each other. The left spiral parts 85A and B are
The right spiral portions 85C and 85D are arranged on the right side in the figure, and are arranged on the left side in the figure. Central part 83A of scraping machine main body 83
Then, the left spiral portion 85A and the right spiral portion 85D are connected, and the left spiral portion 85B and the right spiral portion 85D are connected. The scraper main body 83 approaches the raw material a2 bridged while rotating, and the spiral part 85
When the raw material a2 collides with the raw material a2, the raw material a2 falls off from the conveyor main body 56 and is scraped off.

Returning to FIG. 2, the description will be continued. Double damper 36
Is a damper 36A and a damper 3 arranged vertically above and below.
Each of the dampers 36A, 36B has a damper main body 86A, B which is rotated by 90 ° from the horizontal position in the closed state to the vertically downward position in the open state. When the damper main body 86A is opened, the raw material discharged vertically downward into the damper 36A from the discharge port 69 of the scraper 34 due to the weight of the raw material is discharged after the damper main body 86A is closed. Is opened, it is discharged vertically downward into the damper 36B. The damper bodies 86A and 86B are opened / closed by a driving device (not shown).

The dry distillation furnace 37 is arranged horizontally and has a supply port 6
7, a discharge port 58, and a cylindrical horizontal distillation type dry distillation furnace case 59
Have. The carbonization furnace case 59 accommodates the carbonization conveyor 38 inside, and a drive motor 39 is attached to the right end 59B in the figure. The raw material a2 discharged from the damper 36B is
It passes through the supply port 67 vertically downward by its own weight, and is horizontally conveyed from right to left in the figure by the rotation of the carbonization conveyor 38. The raw material a2 traverses the second duct 5 while being conveyed to the carbonization conveyor 38, and the exhaust gas j flowing through the second duct 5 heats the dry distillation gas k in the dry distillation furnace case 59. The dry distillation gas k carbonizes and carbonizes the raw material a2, and the raw material a2 becomes a carbide u. The carbide u is discharged from the discharge port 58 downward in the vertical direction by its own weight. In the portion of the dry distillation furnace case 59 outside the fifth duct 13, the temperature of the dry distillation gas k inside the dry distillation furnace case 59 (the ambient temperature of the raw material a2).
A temperature measuring device 16 for measuring is attached.

The dry distillation furnace 37 is equipped with a steam nozzle 49 as a steam supply device, and the steam s is discharged from the steam nozzle 49. The steam nozzle 49 is used in the carbonization furnace case 5.
3 on top 59A, 1 on left edge 59C, side 59D
8 are attached to. The steam nozzle 49 is partially
The remaining part is arranged outside the second duct 5 inside the second duct 5.

FIG. 4 shows the structure of the carbonization conveyor 38. The carbonization conveyor 38 has a spiral structure, and the conveyor pitch of the spiral part may be the same, but it is preferably configured so as to become narrower in the carbide transport direction (from right to left in the figure). Therefore, in the figure, the first pitch is P ₁ ,
Assuming that the second pitch is P ₂ , the n-1th pitch is P _{n- 1} and the nth pitch is P _n , P ₁ > P ₂
> ... P _n-1 > P _n holds. First pitch P ₁
Can be obtained by measuring in the axial direction from the outermost portion of the rightmost end (tip of the spiral portion) to the portion where the outer circumferential portion shifts 360 degrees around the axis in the figure, and the second pitch P ₂ is Similarly, it can be obtained by measuring in the axial direction from the end point of the first pitch P _{1 to} the portion where the outer peripheral portion shifts 360 degrees around the axis. The third and subsequent pitches can be similarly measured.

When the volatile matter is released in the carbonization step, the volume of the raw material a2, which is wood, becomes smaller by that amount, and when the conveyor pitch is the same, the raw material filling rate decreases toward the subsequent stage of the conveyor. However, by narrowing the conveyor pitch in the carbide transport direction, the raw material filling rate in the latter stage of the conveyor can be made comparable to that in the front stage of the conveyor,
Therefore, the raw material filling rate of the entire conveyor can be improved, and the processing amount of the raw material a2 can be increased. The pitch change ΔP (= P _n−1 −P _n ) is calculated by the following equation,
It can be defined as ΔP = a / (x + x ₀ ) + P ₀ . Here, a is a pitch reduction coefficient, x is a coefficient determined for each pitch change so that each of the second and subsequent pitches has an appropriate value, x ₀ is the first pitch (P ₁ ), and P is ₀ is a coefficient for correcting the final pitch.

As shown in the figure, a plate-shaped stirring paddle 81 as a stirring portion is attached to the spiral portion 38A of the carbonization conveyor 38. It is preferable that the number of the stirring paddles 81 is twice the number of turns of the spiral portion 38A, and the stirring paddles 81 are evenly arranged and attached. In the present embodiment, since the number of windings of the spiral portion 38A is 6, the number of stirring paddles 81 is 12. In the figure, the shaft portion connected to the drive motor 39 (see FIG. 2) at the right end of the spiral portion 38A is omitted (same in FIG. 5 described later).

As shown in FIG. 5, the structure of the stirring paddle 181 may be rod-shaped. The rod-shaped stirring paddle 181 may be arranged at a position that is 180 ° symmetrical when viewed from the side, and may have a structure that penetrates the spiral portion 138A. In the spiral-type carbonization conveyor 138 having a low rotation speed, when the plate-shaped stirring paddle is used, the raw material a2, which is wood, is lifted by the plate-shaped stirring paddle, and contact heat transfer with the wall surface of the carbonization conveyor 138 occurs. It may not happen. However, by making the stirring paddle into a rod shape, it is possible to prevent the raw material a2 from being lifted and improve the stirring effect of the raw material a2 without impeding wall surface heat transfer.

Returning to FIG. 2, the description of the structure of the high temperature carbonization apparatus 6 will be continued. The cooling conveyor 41 has a supply port 70, a conveyor case 60, a conveyor body 61 housed in the conveyor case 60, and a discharge port 62. Dry distillation furnace 3
The carbide u discharged from the discharge port 58 of
And the supply port 70 through the connecting chute 40 that connects the supply port 70
And is conveyed horizontally from right to left in the drawing by the rotation of the conveyor body 61, and is discharged vertically downward from the discharge port 62. Conveyor body 6
1 is rotationally driven by a drive motor 42 attached to the right end of the conveyor case 60 in the figure.

The shaft portion 61A of the conveyor body 61 is tubular, and a partition plate (not shown) is provided inside the shaft portion 61A.
A flow path that reciprocates inside A is formed. A cooling water supply pipe 64 and a cooling water return pipe 65 are connected to the left end of the shaft portion 61A in the figure via a connection component (not shown). Therefore, in the figure, the cooling water w2 supplied to the shaft portion 61A from the left end
However, the carbide u that flows through the flow path inside the shaft portion 61A and is transported inside the conveyor case 60 of the cooling conveyor 41 is cooled.

The gate valve 43 is provided at the discharge port 62 of the cooling conveyor 41. Further, a recovery box 44 is provided downstream of the gate valve 43, and by opening the gate valve 43, the cooled carbide u discharged from the discharge port 62 passes through the gate valve 43 and enters the recovery box 44. Be recovered.

The wood vinegar liquid recovery device 45 includes a volatile gas supply pipe 71, a volatile gas return pipe 72, a volatile gas cooling heat exchanger 73, a cooling water supply pipe 74, and a cooling water return pipe 75. Wood vinegar collection pipe 76 and wood vinegar collection container 77
It is configured to include and. The volatile matter gas supply pipe 71 is a gas outlet 63 provided at the upper left end of the carbonization furnace 37 in the figure.
It is connected to the. The volatile matter gas supply pipe 71 supplies the volatile matter gas g generated in the process in which the raw material a2 is heated and carbonized in the dry distillation furnace 37 to the volatile matter gas cooling heat exchanger 73. A tube 78 is provided inside the volatile gas cooling heat exchanger 73, the cooling water w2 supplied by the cooling water supply pipe 74 flows, and the cooling water return pipe 75 supplies it to a cooling water supply device (not shown). Will be returned.

The volatile matter gas supply pipe 71 is heated by a heater (not shown). The volatile matter gas g supplied to the volatile matter gas cooling heat exchanger 73 via the volatile matter gas supply pipe 71 comes into contact with the tube 78 and is cooled and condensed to become a wood vinegar liquid t, which is a volatile matter gas cooling heat exchange. It is stored at the bottom of the container 73. A wood vinegar solution recovery pipe 76 is connected to the bottom of the volatile matter gas cooling heat exchanger 73, and a sluice valve 79 provided on the wood vinegar solution recovery pipe 76 is closed to open to thereby remove the volatile gas cooling heat exchanger. The wood vinegar solution t stored in the bottom of 73 is recovered in the wood vinegar solution recovery container 77. Volatile gas supply pipe 7
Since No. 1 is heated by a heater (not shown), the wood vinegar liquid t is not condensed in the volatile gas supply pipe 71. In addition, the wood vinegar liquid t collected in the wood vinegar liquid collection container 77
Contains tar, but the wood vinegar liquid t and tar can be separated by a centrifugal separator (not shown).

Of the volatile matter gas g, the liquefied volatile matter gas g which has not been liquefied passes through the volatile matter gas return pipe 72 and is provided on the volatile matter gas return pipe 72.
The third duct 9 which is attracted to 0 and is located downstream of the carbonization furnace 37 and upstream of the bag filter 12 (see FIG. 1).
(See FIG. 1) or the primary combustion chamber 3A of the swirl melting furnace 3.
(See FIG. 1). Therefore, the volatile gas g generated in the carbonization process can be effectively used.

As shown in FIG. 6, the dry distillation furnace 237A and the dry distillation furnace 237B are connected to the horizontal portion 5 of the second duct 5 (see FIG. 1).
The raw material a2 which is provided in B and is heated by passing through the dry distillation furnace 237A.
However, it may pass through the dry distillation furnace 237B to be heated and carbonized. Particularly, in the case of the raw material a2 that needs to be heated and carbonized for a long time, the carbide u that is carbonized from the raw material a2
It is effective to have two stages of dry distillation furnaces in order to increase the amount of carbon dioxide.

Next, referring to FIG. 2, the operation of the high temperature carbonization apparatus 6 of the present embodiment will be described. The raw material a2 is charged into the storage hopper 31 from the charging port 51 with an open lid. The charged raw material a2 is discharged from the discharge port 53 by its own weight, passes through the supply port 54, and enters the right end of the cutout conveyor 32 in the figure. The raw material a2 that has entered the cutting conveyor 32 is conveyed by the rotation of the conveyor main body 56 and reaches the scraping machine 34.
The raw material a2 is wetted by the water w1 which is discharged in a mist form from the wet nozzle 46 while being conveyed by the cutting conveyor 32.

Since the scraper main body 83 of the scraper 34 is normally located at the left side position shown by the solid line in the figure, the raw material a2 drops and passes through the scraper 34 as it is. When the raw material a2 is clogged in the cutout conveyor 32, the scraper main body 83 rotates and moves toward the clogged raw material a2 to the position shown by the broken line in the figure, and the clogging of the raw material a2 is cleared. afterwards,
The scraper main body 83 moves to the original position.

The raw material a2 leaving the scraping machine 34 passes through the double damper 36. When passing through the double damper 36, the raw material a2 is discharged from the damper 3 after the damper 36A is closed to open.
After passing 6A, the damper 36A is closed and the damper 36
After B is closed to open, it passes through the damper 36B. Since the damper 36A and the damper 36B do not open at the same time, the dry distillation furnace 37 passes through the double damper 36 and the storage hopper 3
The amount of the volatile gas g leaked from 1 to the atmosphere is very small.

Raw material a entering the carbonization furnace 37 through the supply port 67
2 is conveyed by the rotation of the carbonization conveyor 38, and while being conveyed by the carbonization conveyor 38, the stirring paddle 8
1 (see FIG. 3). During this period, the exhaust gas j having a high temperature heats the dry distillation gas k, the dry distillation gas k reaches a temperature of 700 to 1000 ° C., preferably 800 to 1000 ° C., and the raw material a2 is heated by the dry distillation gas k to be carbonized to form a carbide u. Becomes The raw material a2 generates a volatile gas g while being heated and carbonized. Further dry distillation furnace 37
In the inside, while the raw material a2 is carbonized to form the carbide u, the steam s is discharged from the steam nozzle 49 and the carbide u is activated. By activating, the surface area of the carbide u can be increased, the composition of the generated volatile gas g can be improved, and the molecular weight can be reduced.

Further, with a dry distillation gas at a temperature of 700 ° C. or higher,
Since the carbonization is carried out by dry distillation, the tar content is deposited and solidified on the carbide, and the generation of tar is reduced as compared with the conventional dry distillation furnace. However, it is inevitable that the tar generated inside the dry distillation furnace 37 adheres. Steam s emitted from the steam nozzle 49
Depending on the inside of the carbonization furnace case 59, the carbonization conveyor 38
The tar adhering to the spiral portion 38A and so on is removed.
By doing so, the occurrence of tar troubles can be reduced. Further, since the tar is removed by the steam s, reforming of the removed tar, that is, CO and H ₂
Can be converted to. Converted CO and H
_{The second} duct 9 is attracted to the volatile gas attracting fan 80 through the wood vinegar recovery device 45, and is located downstream of the carbonization furnace 37 and upstream of the bag filter 12 (see FIG. 1) (see FIG. 1). Or the primary combustion chamber 3 of the swirl melting furnace 3.
It is returned to A (see FIG. 1) and is effectively used.

The carbide u exits the dry distillation furnace 37 from the discharge port 58, passes through the connecting chute 40, enters the cooling conveyor 41 from the supply port 70, and during transportation, the shaft portion 6 of the conveyor body 61.
It is cooled by 1A to lower the temperature, and exits the cooling conveyor 41 from the discharge port 62. Carbide u exiting the cooling conveyor 41
Passes through the opened gate valve 43 and enters the recovery box 44 for recovery.

The volatile matter gas g is supplied from the dry distillation furnace 37 to the volatile matter gas cooling heat exchanger 73 through the volatile matter gas supply pipe 71, and is cooled by the volatile matter gas cooling heat exchanger 73 to become wood vinegar liquid t to become volatile matter. It is stored at the bottom of the gas cooling heat exchanger 73. The wood vinegar solution t stored at the bottom of the volatile gas cooling heat exchanger 73 is recovered in the wood vinegar solution recovery container 77 by opening the gate valve 79.

The temperature control of the exhaust gas j will be described with reference to FIG. When the melting temperature of the swirling melting furnace 3 rises, the temperature of the exhaust gas leaving the swirling melting furnace 3 rises, for example, exceeds 1000 ° C. in the horizontal portion 5B, and the temperature of the carbonization gas k is reduced to 1
The temperature may be higher than 000 ° C. In this case, the control device 17 issues a start signal q to start the bypass blower 15 attached to the bypass line 14. Further control device 1
7 issues an opening signal r to the automatic control valve 18 to open the automatic control valve 18. Therefore, the exhaust gas j having a low temperature flowing downstream of the waste heat boiler 10 is returned to the vertical portion 5B through the bypass line 14 and mixed with the exhaust gas j having a high temperature to lower the temperature of the exhaust gas j toward the carbonization furnace 37, The temperature of the dry distillation gas k can be lowered to 1000 ° C. or lower.

In the carbonization in the high temperature carbonization apparatus 6 of this embodiment, the temperature of the exhaust gas j discharged from the swirling melting furnace 3 is sufficiently high, and the temperature of the dry distillation gas k in the dry distillation furnace 37 heated by the exhaust gas j is high. 700 ° C to 1000 ° C, preferably 800
The high-temperature carbonization device 6 is installed at a temperature range of ℃ ~ 1000 ℃,
Since the sensible heat of the exhaust gas j is used as the heat source for carbonizing the raw material a2, the following effects are obtained. That is, surface area, calorific value,
It is possible to obtain a carbide u with improved quality such as carbon fixation stability. Further, the heating time for carbonization can be shortened, and the device can be downsized. Tar can be precipitated and solidified on the carbide to improve the yield of the carbide. Further, since the concentration of hydrogen and hydrocarbon in the volatile matter gas g generated in the carbonization process becomes high, the volatile matter gas g can be effectively used.

As shown in FIG. 7, wood heated at a high temperature of 700 to 1000 ° C. first becomes a melt (melt), and the melt (melt) is primarily decomposed to produce gas (gas), tar ( It is decomposed into liquid or vapor) and char (solid). Next, the tar is secondarily decomposed into decomposed gas (gas) and char (solid). Tar is precipitated and solidified on the carbide by secondary decomposition.

As shown in FIG. 8, when a wood chip as a raw material touches a high temperature wall, the touched portion becomes a melt (melt) and the wood slides on the high temperature wall, so that the wood chip smoothly moves on the high temperature wall. Moving.

When the carbonization temperature is 600 ° C. or lower, when the carbonization temperature is raised in this range, the liquid is produced from the melt during the primary decomposition of the melt after the formation of the melt.
Although gas and solid (char) are generated, liquid and gas are more dominant than solid (char). Furthermore, in the secondary decomposition, the change from liquid / vapor (mainly tar content) to gas and solid (char) is performed, but the change to gas is promoted by the change to solid (char). . Therefore, the carbide yield is lowered by the high temperature. In the range of 600 ° C. or lower, the conversion of the melt generated by the primary decomposition into the liquid or the gas proceeds more predominantly in the higher temperature region than the conversion into the solid (char), and the adoption of a high carbonization temperature is theoretically adopted. It is disadvantageous for carbide formation.

However, if the dry distillation temperature is 700 ° C. or higher, preferably 800 ° C. or higher, the following effects are obtained. That is, when the carbonization temperature is 700 ° C. or higher, liquid, gas, and solid (char) are generated in the primary decomposition from the generated melt. The degree of predominance of gas generation becomes stronger than that in the high temperature region of 600 ° C. or lower. And liquid
In the secondary decomposition of tar that has become vapor, solid (char) is produced and gas is produced, but solid (char) is produced more predominantly than gas is produced. Therefore, the solidified product (charified product) of tar is deposited and solidified on the carbide, and the carbide yield is improved. The explanation that the solidification (charification) of tar, which is a liquid / vapor, leads to an increase in the yield of carbide is rational also in terms of the reaction mechanism. When the carbonization temperature is increased to over 700 ° C, the composition of the wood pyrolysis product gas becomes CO
CO ₂ increases and CO ₂ increases, but CO ₂ is mainly generated in the secondary decomposition of tar, which is a result of supporting the secondary decomposition of tar described above.

FIG. 9 is a gasification system 1 to which a high temperature carbonization apparatus 106 according to a second embodiment of the present invention is attached.
It is a block diagram of 01.

The gasification system 101 includes a fluidized bed gasification furnace 102 as a gas production furnace for producing a product gas m as a first gas or as an exhaust gas, and a high temperature carbonization described later from the fluidized bed gasification furnace 102. It is configured to include a sixth duct 105 as a gas flow path for guiding the generated gas m to the device 106, and a high temperature carbonization device 106 provided in the sixth duct 105. The configuration of the fluidized bed gasification furnace 102 is the same as that of the fluidized bed gasification furnace 2 described in the first embodiment, except for the differences described below, and the configuration of the high temperature carbonization device 106 is the first
It is the same as the high-temperature carbonization device 6 described in the above embodiment except for the differences described below. Therefore, the fluidized bed gasification furnace 102
With respect to the configuration of 1 and the configuration of the high-temperature carbonization device 106, explanations other than the differences described below will be omitted.

As shown in FIG. 9, a fluidized bed gasification furnace 102.
The generated gas m is discharged from. Further, the produced gas m comes into contact with a dry distillation furnace 137 (see FIG. 10) described later, and the dry distillation furnace 13
Exhaust gas m for heating 7. Further, in the present embodiment, the exhaust gas m enters the inside of the dry distillation furnace 137 as described later, and therefore is also the dry distillation gas in the dry distillation furnace 137.

The exhaust gas m discharged from the fluidized bed gasification furnace 102 flows in the sixth duct 105. Exhaust gas m
Is used in a combustion furnace (not shown) that contacts the dry distillation furnace 137 to heat the dry distillation furnace 137 and then burns the exhaust gas m. Therefore, the radiant boiler, the high temperature air heater, the waste heat boiler, the bag filter and the like are not installed in the sixth duct 105 through which the exhaust gas m flows. Further, a bypass line for returning the exhaust gas m on the downstream side of the high temperature carbonization device 106 to the upstream side of the high temperature carbonization device 106 is not provided.

In the second embodiment, steam s as a fluidizing gas for fluidizing the fluidized medium in the fluidized bed gasification furnace 102 is supplied from the bottom 122 of the fluidized bed gasification furnace 102. . In this case, the fluidized bed gasification furnace 102
Since the inside is almost completely reducing atmosphere, exhaust gas m
Is in direct contact with the raw material a2 as the material to be carbonized, the raw material a2
2 is thermally decomposed and carbonized, but the combustion of the raw material a2 occurs only partly.

The features of the structure of the high temperature carbonization apparatus 106 will be described with reference to FIG. The sixth duct 10 of the dry distillation furnace case 159 of the dry distillation furnace 137 constituting the high temperature carbonization device 106.
A plurality of through holes 166 are formed in the inner portion of the No. 5, and the exhaust gas m enters from the through holes 166 into the dry distillation furnace case 159 and directly contacts the raw material a2. The exhaust gas m is 700 ° C. to 1000 in the carbonization furnace 137.
It is supplied at a temperature of 0 ° C, preferably 800 ° C to 1000 ° C. Therefore, in the present embodiment, the sensible heat of the exhaust gas m is used as the heat source for carbonizing the raw material a2, and the same effect as in the first embodiment can be obtained.

Further, since the exhaust gas m is constructed so as to come into direct contact with the raw material a2 as a dry distillation gas, the temperature of the exhaust gas m becomes the ambient temperature of the raw material a2, and the calorific value of the exhaust gas m is increased by the carbonization of the raw material. Is used for. The volatile component gas g generated in the dry distillation furnace case 159 is absorbed by the through hole 166.
From the dry distillation furnace 137 to the wood vinegar solution recovery device 245 without flowing into the sixth duct 105 from the volatile matter gas attraction fan 2 provided on the downstream side of the wood vinegar solution recovery device 245.
80 has a sufficient suction volume.

FIG. 11 shows a combustion system 3 to which a high temperature carbonization device 306 according to a third embodiment of the present invention is attached.
It is a block diagram of 01.

The combustion system 301 includes a fluidized bed incinerator 303 and a fluidized bed incinerator 30 as a second gas or a gas combustion furnace for producing exhaust gas j which is a combustion gas.
A sixth duct 305 serving as a gas flow path for guiding the exhaust gas j from the No. 3 to a high temperature carbonization device 306 described later, and a sixth duct 305.
It is configured to include a high temperature carbonization device 306 provided therein. The configuration of the fluidized bed incinerator 303 is the same as the fluidized bed gasification furnace 102 (see FIG. 9) described in the first embodiment, except for the differences described below. The structure of the high temperature carbonization device 306 is arranged in the high temperature carbonization device 6 described in the first embodiment (see FIG. 2) and in the sixth duct through which the exhaust gas j exiting the fluidized bed incinerator 303 flows. It is the same except that. Therefore, the description of the structure of the fluidized bed combustion furnace 302 will be omitted, except for the differences from the fluidized bed gasification furnace 2 (see FIG. 1) described below.

Similar to the fluidized bed gasification furnace 2 (see FIG. 1),
Air b as fluidizing gas is fed into the fluidized bed combustion furnace 303 from the furnace bottom 322. However, the air b from the side wall 303A is further fed into the fluidized bed combustion furnace 303.
Therefore, a sufficient amount of air b is supplied to the fluidized bed combustion furnace 303 so that the fluidized bed combustion furnace 303 becomes an oxidizing atmosphere instead of a reducing atmosphere, and the general waste a1 as the input processing target is completely combusted to generate an exhaust gas j. To be done. The exhaust gas j is a carbonization furnace 3.
It is the exhaust gas j that contacts 37 (see FIG. 12) and heats the dry distillation furnace 337. The exhaust gas j discharged from the fluidized bed incinerator 303 flows in the sixth duct 305.

The exhaust gas j contacts the dry distillation furnace 337 to heat the dry distillation furnace 337, and then recovers heat from the exhaust gas j by a high temperature air heater (not shown) (heating air b), a waste heat boiler. , Sent to bug filters, etc. Unlike the first embodiment, no radiation boiler is attached in the sixth duct 305 through which the exhaust gas j flows. Further, the exhaust gas j on the downstream side of the high temperature carbonization device 306 is fed to the high temperature carbonization device 30.
No bypass line for returning to the upstream side of 6 is provided.

In the present embodiment, the sensible heat of the exhaust gas j is used as the heat source for carbonizing the raw material a2 as the material to be carbonized which is supplied to the carbonization furnace 337, and the ambient temperature of the raw material a2 is 700 ° C., more preferably 800 ° C. As a result of the above, the raw material a2 is subjected to carbonization and carbonization, and the same effect as that of the first embodiment can be obtained.

[0086]

As described above, according to the present invention, since the ambient temperature of the object to be carbonized is set to 700 ° C. or higher by the exhaust gas and the object to be carbonized is carbonized by carbonization, the surface area of the carbonized object becomes large. The calorific value increases, and the tar content is deposited on the carbide and solidifies, so that the carbon fixation stability increases. Further, since the heating time is shortened, the device can be downsized. Further, since the tar content is deposited and solidified on the carbide, the tar content in the volatile gas generated from the material to be carbonized is reduced by the carbonization, and the problem of tar adhesion in the piping system for guiding the volatile gas is less likely to occur.

[Brief description of drawings]

FIG. 1 is a sectional block diagram of a gasification and melting system using a high temperature carbonization apparatus according to a first embodiment of the present invention.

FIG. 2 is a sectional block diagram showing a configuration of a high temperature carbonization apparatus according to a first embodiment of the present invention.

FIG. 3 is a detailed view of a scraper main body of the scraper.

FIG. 4 is an explanatory view of a spiral portion of a carbonization conveyor of the high temperature carbonization apparatus of FIG.

5 is an explanatory view of another embodiment of the stirring paddle of the spiral portion of FIG.

FIG. 6 is a cross-sectional block diagram of a dry distillation furnace in the case of two stages.

FIG. 7 is a flow chart showing the contents of pyrolysis and carbonization of wood.

FIG. 8 is a schematic diagram showing thermal decomposition of wood.

FIG. 9 is a sectional block diagram of a gasification system using a high temperature carbonization apparatus according to a second embodiment of the present invention.

FIG. 10 is a sectional block diagram showing a configuration of a high temperature carbonization apparatus according to a second embodiment of the present invention.

FIG. 11 is a cross-sectional block diagram of a combustion system using a high temperature carbonization device according to a third embodiment of the present invention.

FIG. 12 is a sectional block diagram showing a configuration of a high temperature carbonization apparatus according to a third embodiment of the present invention.

[Explanation of symbols]

1 Gasification and melting system 2 Fluidized bed gasification furnace 3 Swirl melting furnace 5 Second duct 6 High temperature carbonization equipment 7 Radiant boiler 8 high temperature air superheater 10 Waste heat boiler 12 Bug filter 14 Bypass line 15 Bypass blower 16 Temperature measuring device 17 Control device 18 Automatic control valve 31 Storage hopper 32 cutting conveyor 34 scraper 36 double damper 37 Dry distillation furnace 38 Carbonization conveyor 41 Cooling conveyor 44 Collection Box 45 Wood vinegar liquid recovery device 46 Wet nozzle 49 steam nozzle 73 Volatile gas cooling heat exchanger 77 Wood Vinegar Collection Container 80 Volatile gas attraction fan 81 stirring paddle 101 gasification system 102 fluidized bed gasification furnace 106 high temperature carbonization equipment 137 carbonization furnace 166 through hole 237a, b Dry distillation furnace a1 General waste a2 raw material b air g Volatile gas j Exhaust gas m generated gas p Temperature signal q Start signal r Opening vibration t wood vinegar water w1 water w2 cooling water

─────────────────────────────────────────────────── ─── Continuation of front page (51) Int.Cl. ⁷ Identification code FI theme code (reference) C10B 53/02 C10C 5/00 C10C 5/00 F23G 5/00 115Z F23G 5/00 115 5/027 B 5 / 027 5/46 ZABA 5/46 ZAB B09B 3/00 303J (72) Inventor Kaori Sasaki 11-1 Haneda Asahimachi, Ota-ku, Tokyo Ebara Corporation (72) Inventor Satoshi Asano Haneda, Ota-ku, Tokyo 11-1 Asahimachi Ebara Corporation F-term (reference) 3K061 AA11 AB02 AC20 BA01 BA08 DA12 DA19 DB06 EA03 EB01 3K065 JA05 JA18 JA19 4D004 AA04 AA07 AA11 AA12 AA46 AC05 CA24 CA26 CA28 CB04 CB31 CB45 CC02 DA01 DA02 DA01 DA02 DA02 DA01 DA02 4H012 HA05 HB05 HB10 JA03 JA11 JA13

Claims (11)

[Claims] 1. A gas flow path through which exhaust gas discharged from a gas generation furnace that generates a first gas from a processing object passes, or a gas combustion furnace that burns a processing object to generate a second gas. A gas flow path through which the exhaust gas passes; and a carbonization furnace configured to introduce a substance to be carbonized therein and to transfer heat from the exhaust gas passing through the gas flow path; The ambient temperature of the object to be carbonized was 700 ° C. or higher, and the object to be carbonized was carbonized by carbonization.
High temperature carbonization equipment. 2. A high-temperature exhaust gas discharged from a gas-generating furnace that generates gas from the object to be processed or a high-temperature exhaust gas discharged from a gas combustion furnace that burns the object to be processed is disposed. The exhaust gas in contact with the carbonization furnace has an ambient temperature of 700 ° C. or higher introduced into the carbonization furnace and is configured to carbonize and carbonize the carbonization object. High temperature carbonization equipment 3. The high temperature carbonization apparatus according to claim 1 or 2, further comprising a moistening device for moistening the carbonized material before carbonization. 4. The two dry distillation furnaces are provided; the object to be carbonized is configured to be transported inside the dry distillation furnace on one side and then transported inside the dry distillation furnace on the other side.
To the high temperature carbonization apparatus according to claim 3. 5. A waste heat boiler for recovering heat from the exhaust gas is provided downstream of the dry distillation furnace with respect to the flow of the exhaust gas, the exhaust heat boiler being provided with a control device for controlling the ambient temperature; An exhaust gas flow passage is arranged for guiding the exhaust gas that has passed through the boiler to the upstream side of the dry distillation furnace and mixing the exhaust gas with the exhaust gas on the upstream side of the dry distillation furnace;
The high temperature carbonization apparatus according to claim 1, wherein the ambient temperature is controlled by controlling a flow rate of exhaust gas flowing through the exhaust gas passage. 6. A conveying device for conveying the object to be carbonized through the inside of the carbonization furnace; the conveying device having an agitating section for agitating the object to be carbonized during conveyance; The high temperature carbonization apparatus according to any one of 1. 7. The high-temperature carbonization apparatus according to claim 1, further comprising a cooling device that cools the carbonized material. 8. A steam supply device for supplying steam for removing tar adhering in the carbonization furnace to the carbonization furnace;
The high temperature carbonization apparatus according to claim 1. 9. A recovery device for recovering wood vinegar contained in volatile matter gas generated in the carbonization furnace; the recovery device is further configured to recover tar contained in the volatile matter gas. Any one of claims 1 to 8
High temperature carbonization equipment according to the item. 10. A generation / exhaust step of generating a first gas from an object to be processed and discharging the first gas as an exhaust gas, or burning the object to be processed to generate a second gas and discharging the second gas. A combustion discharge step of discharging as a gas; an ambient temperature of the object to be carbonized is 700 ° C. or higher by the exhaust gas,
A dry distillation carbonization step of carbonizing and carbonizing the object to be carbonized;
High temperature carbonization method. 11. The high temperature carbonization method according to claim 10, further comprising a moistening step of moistening the material to be carbonized before carbonization.