JP3561310B2 - Dry distillation type oiling equipment - Google Patents

Description

[0001]
[Industrial applications]
BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a dry distillation liquefaction apparatus for recovering oil by thermally decomposing high-molecular organic waste such as waste wires and cables and waste tires covered with rubber or plastic.
[0002]
[Prior art]
Conventionally, as this type of dry distillation type oil converting apparatus, the one shown in FIG. 5 is known, and the recovery of oil from high-molecular-weight organic waste is performed using such an apparatus. . Hereinafter, the conventional dry distillation type oil-forming apparatus will be described. This apparatus comprises a gas generating furnace 9 for generating a carbonized gas by thermally decomposing the above-mentioned polymer organic waste material, and a carbonized gas by cooling the generated carbonized gas. It basically comprises an oil recovery means 2 for separating and recovering the oil contained in the gas, and an exhaust gas processing means 4 for removing the remaining combustible components from which the oil has been recovered by performing a combustion process or the like to make the pollution-free. The gas generating furnace 1c is disclosed in JP-A-5-180425 and JP-A-62-17513, and the heat exchanger 22 in the oil recovery means 2 and the recovery method are described in JP-A-62-1431. Japanese Patent Publication No. 59-9010 discloses a secondary combustion method in the exhaust gas treatment means 4 described in Japanese Patent Application Publication No. Sho 59-14010 and Japanese Patent Application Laid-Open No. Sho 62-1432.
[0003]
The gas generating furnace 9 has a stepped inclined multi-stage structure in which the inside of the furnace is divided into an upper pyrolysis section 91 and a lower self-combustion section 92. The self-combustion section 92 includes a fuel tank. A combustion burner 93 for burning fuel from the fuel supply 93a and air supply means 94 for supplying air for combustion by a blower 94a are provided.
[0004]
The procedure for recovering oil by this conventional apparatus is as follows. First, a raw material is charged into a pyrolysis section 91 and a self-combustion section 92 in a furnace, and air is supplied from the outside by an air supply means 94 into the self-combustion section 92. The raw material in the self-combustion section 92 is burned by the combustion burner 93 while supplying the gas. Then, after the raw material starts burning, the combustion burner 93 is stopped, the supply of the air is continued, the raw material continues to self-combust, and the raw material of the thermal decomposition section 91 is pyrolyzed by the heat of combustion to dry distillation. Generate gas.
[0005]
Next, the dry distillation gas is led out to the oil recovery means 2 and cooled by passing through the heat exchangers 22, 23 and 24, and the oil separated into gas and liquid is recovered in the oil storage tanks 27 and 28. Then, in the exhaust gas treatment means 4, the low carbon component remaining in the dry distillation gas without being recovered as oil is completely burned in the secondary combustion chamber 41, and the combustion exhaust gas in the secondary combustion chamber 41 is used for smoke suppression. Through a heat exchanger 42, a smoke collection tower 43 for cleaning and dust collection, and a mist separator 44, thereby discharging the clean gas detoxified from the chimney 45 to the outside air.
[0006]
In short, the above-described conventional dry distillation type oil conversion apparatus ignites the raw material M by the combustion burner 93 while supplying air into the gas generating furnace 9 as shown in the principle diagram in FIG. The ignition by the combustion burner 93 is continued until the temperature of the generating furnace 9 reaches a predetermined temperature, for example, 400 ° C., and when the temperature reaches the predetermined temperature, the ignition by the combustion burner 93 is stopped. (For example, 10%) is continued, and the remaining raw material M is thermally decomposed by the heat of combustion accompanying the self-combustion to obtain a carbonized gas. The operation control of the gas generating furnace 9, that is, the control of the pyrolysis conditions, is performed by controlling the degree of self-combustion by controlling the amount of supplied air, and thereby controlling the temperature inside the gas generating furnace 9. ing.
[0007]
[Problems to be solved by the invention]
However, in the above-mentioned conventional dry distillation type oil converting apparatus, since heat for thermal decomposition is obtained by burning the raw material M itself, the burned raw material is used as a raw material for oil recovery. Therefore, there is an inconvenience that the oil conversion rate, which is the oil recovery rate for the raw material, is reduced (at most about 50%).
[0008]
Further, in the above-described conventional apparatus, since the temperature control in the gas generating furnace 9 is performed by adjusting the supply amount of air, there is a disadvantage that it is difficult to stably maintain and control the thermal decomposition conditions. That is, the air supplied into the furnace may cause not only combustion of the raw material for the self-combustion but also combustion of the carbonized gas itself. In this case, fluctuations in the pyrolysis conditions are caused, and the control becomes difficult. A decrease in the carbonization gas causes a decrease in the oil conversion rate, and further, the quality of the oil component becomes unstable.
[0009]
The present invention has been made in view of such circumstances, and a purpose thereof is to improve the oil conversion rate and, in addition, to facilitate the operation control of a gas generating furnace.
[0010]
[Means for Solving the Problems]
In order to achieve the above object, the invention according to claim 1 comprises, as shown in FIG. 1, a carbonization furnace 1 that pyrolyzes a polymer material to generate a carbonization gas, and is connected to an upper portion of the carbonization furnace 1. An oil recovery means 2 for separating and recovering the oil by cooling the dry distillation gas; and a high-temperature gas which does not cause self-combustion of the polymer material even when the polymer material is brought into contact with the polymer material at a pyrolysis temperature. And a high-temperature gas generating means 3 for generating the gas. The high-temperature gas generating means 3 and the dry distillation furnace 1 are connected to each other such that only the high-temperature gas is blown into the dry distillation furnace 1 as a heat medium for thermally decomposing a polymer material.The high-temperature gas generating means 1 is provided separately from the carbonization gas burning means for generating a high-temperature gas from the combustion exhaust gas obtained by burning the remaining carbonization gas from which the oil has been recovered by the oil recovery means. Independent high-temperature gas generating means for independently generating high-temperature gas, and connecting the dry distillation gas burning means and the independent high-temperature gas generating means to the dry distillation furnace in the starting stage. And supply switching means for switching the high-temperature gas from the dry-distilled gas combustion means into the dry-distillation furnace in the steady-state operation stage, and the independent high-temperature gas generating means is constituted by a coke oven. .
[0011]
[Action]
With the above arrangement, in the first aspect of the present invention, the high-temperature gas generated by the high-temperature gas generating means is blown into the carbonization furnace, and the high-temperature gas causes thermal decomposition of the polymer material (raw material). Then, the dry distillation gas generated by the thermal decomposition is cooled by the oil recovery means, and the oil is separated and recovered. At the time of the thermal decomposition, even if the high-temperature gas comes into contact with the raw material, the raw material does not cause self-combustion. Compared to the case where the air is continuously supplied to the furnace and the heat for pyrolysis is obtained by the self-combustion of the raw material, the amount of the raw material to be self-combusted by the oilification target increases and the carbonization gas itself does not burn, so that The rate is improved.
[0012]
In addition, since the high-temperature gas blown into the carbonization furnace does not cause self-combustion of the raw material at the thermal decomposition temperature, the generation of the carbonized gas by the thermal decomposition is stabilized, and the oil is formed along with the stable oil recovery. In addition to improving the efficiency, the temperature of the furnace itself can be controlled by the heat of the high-temperature gas itself. This facilitates the maintenance of stable pyrolysis conditions.
[0013]
further, KiIn the operating stage, the supply switching means connects the independent high-temperature gas generation means to the carbonization furnace, and the high-temperature gas generated by the independent high-temperature gas generation means is blown into the carbonization furnace. Then, the inside of the dry distillation furnace is heated and heated by the high-temperature gas, and thermal decomposition of the raw material starts. In the steady operation stage where the pyrolysis gas is steadily generated by the pyrolysis, the carbonization gas combustion means is connected to the carbonization furnace by the supply switching means, and oil is recovered from the carbonization gas by the oil recovery means. The remaining carbonized gas after burning is burned in the carbonized gas combustion means, and the combustion exhaust gas is blown into the carbonized furnace as a high-temperature gas. Then, thermal decomposition in the carbonization furnace is continued by the high-temperature gas from the carbonization gas burning means.
[0014]
【Example】
Less than, RealAn embodiment will be described with reference to the drawings.
<First embodiment>
Figure 2,1 shows a gas distillation furnace as a carbonization furnace 1 (see FIG. 1), and reference numeral 2 denotes an oil recovery means for separating and recovering oil from a carbonization gas generated in the gas generation furnace 1a. Numeral 3a denotes a dry distillation gas burning means as the high temperature gas generating means 3 (see FIG. 1), and numeral 4 denotes an exhaust gas processing means.
[0015]
-Configuration of gas generating furnace 1a-
The gas generating furnace 1a basically includes a vertical cylindrical raw material introduction section 10, a gas generation chamber 11 for generating a dry distillation gas, a residue combustion chamber 12, and a residue recovery section 13. From the gas generating chamber 11 to the residue combustion chamber 12 and the residue recovery section 13 with the raw material introduction section 10 as the top, each bottom face is stepped and has a downward slope, so that the whole is configured as an inclined multi-stage. That is, in the gas generating furnace 1a of the first embodiment, the entirety of the self-combustion unit 92 and the pyrolysis unit 91 for generating the carbonized gas of the conventional apparatus (see FIG. 5) is used as the gas generation chamber 11. .
[0016]
A bucket conveyor 14 for supplying a raw material is connected to the top of the raw material introduction unit 10, and a pair of open / close plates each having a pair of open / close plates that are opposed to each other in a substantially V-shaped arrangement are connected inside. Dampers 15a, 15b, 15c are provided at predetermined vertical intervals. The raw material conveyed by the bucket conveyor 14 is supplied from the top onto the upper opening / closing damper 15a in a closed state. The three opening / closing dampers 15a, 15b, and 15c are configured to open only the upper opening / closing damper 15a after the raw material is charged into the closed upper opening / closing damper 15a, and to move the upper opening / closing damper 15b to the closed intermediate opening / closing damper 15b. The raw material was dropped, and then, after the upper opening / closing damper 15a was closed, only the intermediate opening / closing damper 15b was opened to drop the raw material onto the closed lower opening / closing damper 15c. By sequentially opening only the opening and closing dampers, the invasion of outside air is prevented as much as possible, and the raw material is charged into the gas generating chamber 11 in a state where the raw material is preheated and dried.
[0017]
In the gas generation chamber 11, the raw material introduction section 10 is partitioned by opening and closing dampers 15a, 15b, and 15c, and the residue combustion chamber 12 is partitioned by opening and closing gates 16a. A combustion burner 17 is provided below the gas generating chamber 11, and a downstream end of a high-temperature gas outlet pipe 32 described later is connected to the combustion burner 17. The upstream end of the carbonization gas outlet pipe 20 is connected to the uppermost part of the gas generating chamber 11 and below the lower opening / closing gate 15c via an opening / closing valve (not shown). In the gas generating chamber 11, the raw material charged therein is heated and heated by the combustion burner 17 at the time of start-up and by the high-temperature gas blown by the high-temperature gas outlet pipe 32 at the time of steady operation, and is pyrolyzed by pyrolysis. While the gas is generated, the generated carbonized gas is led out to the oil recovery means 2 by the carbonized gas outlet pipe 20.
[0018]
The residue combustion chamber 12 can be hermetically sealed by an opening / closing gate 16a on the gas generation chamber 11 side and an opening / closing gate 16b on the residue recovery section 13 side, and the above-mentioned pyrolyzed residue is introduced into the outside air. It is designed to burn underneath. Further, the residue collecting section 13 is provided with a cooling water tank 13a and a collecting conveyor (not shown), and the residue after combustion in the residue combustion chamber 12 is cooled and collected in the cooling water tank 13a. I have. An exhaust gas outlet pipe (not shown) is connected to the residue combustion chamber 12, and the exhaust gas outlet pipe supplies the combustion exhaust gas to the secondary combustion chamber 41 of the exhaust gas processing means 4.
[0019]
In FIG. 2, reference numerals 18a, 18b and 18c denote pushers, respectively. The pushers 18a and 18b agitate the raw material in the gas generation chamber 11 and push out the residue into the residue combustion chamber 12, and the pusher 18c functions as the residue combustion chamber 12. Stirring of the residue inside and pushing out of the residue after combustion to the residue recovery unit 13 are performed.
[0020]
-Configuration of oil recovery means 2-
The oil recovery means 2 includes a carbon cyclone 21 for removing coal dust contained in the dry distillation gas led out through the dry distillation gas outlet pipe 20, and a first and a second cyclone 21 for cooling the dry distillation gas after removing the coal dust to separate and recover oil. The second and third heat exchangers 22, 23, and 24, the oil recovery when the heat cannot be recovered by the heat exchangers 22, 23, and 24, and the backflow of gas from the secondary combustion chamber 41 described later It comprises a bubbling tank 25 for prevention and a blower 26 for sucking and pressure-feeding the carbonization gas. The oil separated by passing through the first heat exchanger 22 is stored in the oil tank 27, while the oil separated by passing through the second and third heat exchangers 23 is stored in the oil tank 28. It is to be stored.
[0021]
The first to third heat exchangers 22, 23, and 24 are connected in order from the top of the carbon cyclone 21 to the downstream side, and the downstream side of the third heat exchanger 24 is connected to the gas inlet of the bubbling tank 25. Have been. The first bubbling tank 25 removes a water-soluble component contained in the carbonized gas by passing a carbonized gas introduced from a gas inlet into the liquid in a bubble state, and removes an oil component that has not been completely recovered. The gas is collected and the backflow of gas from the blower 26 is prevented. Then, the carbonization gas is sucked into the blower 26 from the gas outlet, and sent to one of the exhaust gas treatment unit 4 and the carbonization gas combustion unit 3a through the conduit 40 connected to the discharge side.
[0022]
-Configuration of carbonization gas combustion means 3a-
The carbonization gas burning means 3a generates a high-temperature gas in an oxygen-free state by burning the carbonization gas introduction pipe 30 for introducing the carbonization gas from the blower 26 and the carbonization gas introduced by the carbonization gas introduction pipe 30. The apparatus includes a carbonization gas combustion furnace 31 and a high-temperature gas outlet pipe 32 for blowing the high-temperature gas generated by the carbonization gas combustion furnace 31 into the gas generation chamber 11 of the gas generation furnace 1a.
[0023]
The carbonization gas introduction pipe 30 has an upstream end connected to an intermediate position of the conduit 40 and a downstream end connected to the carbonization gas combustion furnace 31. The first opening / closing valve 33 and the second A bubbling tank 34 is provided. Further, a return pipe 35 is attached to the dry distillation gas introduction pipe 30, and an upstream end of the return pipe 35 is located at a position between the first opening / closing valve 33 and the second bubbling tank 34 of the dry distillation gas introduction pipe 30. The downstream end is connected to the secondary combustion chamber 41 of the exhaust gas processing means 4 via a third bubbling tank 37. By controlling the opening and closing of the second on-off valve 36, the carbonized gas sent by the blower 26 is returned to the secondary combustion chamber 41 through the return pipe 35, and thereby, through the carbonized gas introduction pipe 30 when the carbonized gas is excessive. The amount of the carbonized gas introduced into the carbonized gas combustion furnace 31 is adjusted. The second or third bubbling tanks 34 and 37 are designed to further prevent the gas from flowing from the dry distillation gas combustion furnace 31 or the secondary combustion chamber 41 to further enhance safety.
[0024]
The dry distillation gas combustion furnace 31 has a downstream end of the dry distillation gas introduction pipe 30 and an upstream end of the high temperature gas discharge pipe 32 connected to each other. A combustion state by adjusting a flow detector of the introduced dry distillation gas, an air supply device for supplying air for combustion, and an air supply amount in the air supply device based on a detection value of the flow detection device. And a controller for controlling the The controller obtains a theoretical oxygen amount necessary for completely burning the amount of the carbonized gas detected by the flow rate detector, and based on the theoretical oxygen amount, the combustion of the carbonized gas becomes incomplete combustion. In this way, the amount of air supplied from the air supply device is controlled so that an amount of oxygen gas which is reduced by a predetermined amount from the theoretical amount of oxygen is supplied. Then, in the dry distillation gas combustion furnace 31, the exhaust gas as a high temperature gas having a predetermined temperature not containing oxygen gas is generated by completely consuming the supplied oxygen gas by burning the introduced dry distillation gas. Has become.
[0025]
The high-temperature gas outlet pipe 32 blows a predetermined amount of combustion exhaust gas generated in the dry distillation gas combustion furnace 31 into the gas generation chamber 11 of the gas generation furnace 1a.
[0026]
-Configuration of exhaust gas treatment means 4-
The exhaust gas processing means 4 includes a secondary combustion chamber 41 to which the downstream end of the above-described conduit 40 is connected, and a smoke-exhausting heat exchanger 42 for cooling combustion exhaust gas generated by combustion in the secondary combustion chamber 41. And a smoke cleaning tower 43 for cleaning and collecting the exhaust gas after cooling, a mist separator 44, and a chimney 45 for discharging clean gas to the outside air.
[0027]
The secondary combustion chamber 41 burns the carbonized gas introduced through the conduit 40 under the supply of air, whereby the low-carbon gas remaining in the carbonized gas that is not recovered by the oil recovery means 2 because it is a gas at normal temperature is recovered. Several components are completely burned.
[0028]
-Procedures for oilification treatment according to the first embodiment-
The procedure of the oiling treatment according to the first embodiment having the above configuration will be described below.
[0029]
First, as a raw material, natural rubber, synthetic rubber such as ethylene-propylene rubber, chloroprene rubber, or an olefin-based plastic material such as polyethylene or polypropylene, or polyvinyl chloride or the like is placed in the gas generating chamber 11 of the gas generating furnace 1a. Polymer materials to be oiled, such as plastic materials containing halogen, specifically, rubber or plastic coated electric wires, rubber or plastic coated cables, or high molecular organic waste materials such as tires with these materials are appropriately The length and size are filled through the raw material introduction unit 10, and the preparation is completed.
[0030]
Next, in the start-up stage, the inside of the gas generating chamber 11 is heated and heated by the combustion burner 17 to burn the raw material at the bottom of the gas generating chamber 11 with separately supplied air. To generate carbonization gas. The dry distillation gas is led out from the dry distillation gas outlet pipe 20, the oil is recovered by the oil recovery means 2, and then introduced into the dry distillation gas combustion furnace 31 via the dry distillation gas introduction pipe 30.
[0031]
Then, when a steady operation stage occurs in which the carbonized gas starts to be generated and the carbonized gas is introduced into the carbonized gas combustion furnace 31, the heating by the combustion burner 17 is stopped, and thereafter, the air to the gas generation chamber 11 is supplied to the gas generation chamber 11. The combustion exhaust gas of a predetermined temperature (for example, 800 to 900 ° C.) obtained by burning the carbonization gas in the carbonization gas combustion furnace 31 is cut off in the gas generation chamber 11 through the high-temperature gas outlet pipe 32. The raw material in the gas generating chamber 11 is thermally decomposed in an oxygen-free state by the combustion exhaust gas to continuously generate the carbonized gas. In this steady operation stage, since the combustion exhaust gas to be blown does not contain oxygen gas, the self-combustion of the raw material in the starting stage is stopped, and thereafter, all the raw material charged into the gas generating chamber 11 is carbonized gas. It is subject to thermal decomposition for production. If the amount of the carbonization gas generated by the continuation of the steady operation increases and the introduction into the carbonization gas combustion furnace 31 becomes excessive, the second on-off valve 36 is opened and a part of the carbonization gas is secondary-reacted through the return pipe 35. The gas is led to the combustion chamber 41, and the carbonized gas introduced in the secondary combustion chamber 41 is burned. Then, the combustion exhaust gas is converted into a clean gas by passing through the smoke-exchanging heat exchanger 42, the smoke washing tower 43, and the mist separator 44, and the clean gas is discharged from the chimney 45 to the atmosphere.
[0032]
-Operation and effect of the first embodiment-
In the above-mentioned steady operation state, since the combustion exhaust gas as the high-temperature gas blown into the gas generation chamber 11 does not contain oxygen gas, the self-combustion of the raw material at the start-up stage is stopped. The entire amount of the raw material to be filled is subjected to the thermal decomposition for producing the carbonization gas, that is, the oil. For this reason, compared to the conventional case where the air is continuously supplied to the furnace to continuously obtain the heat for the pyrolysis and the raw material is continuously self-burned, the number of objects to be liquefied can be increased by the amount of the non-self-burning, The conversion ratio can be improved.
[0033]
In addition, the control of the furnace temperature for the thermal decomposition can be reliably performed by adjusting the temperature and the amount of the combustion exhaust gas to be blown, and compared with the conventional case where the furnace temperature is controlled by adjusting the supply air amount. The control of the thermal decomposition conditions can be easily performed, whereby the stable thermal decomposition conditions can be maintained. Further, since the inside of the gas generation chamber 11 is reliably brought into an oxygen-free state by the blown combustion exhaust gas, the generation of the dry distillation gas by the thermal decomposition is stabilized, and the oil conversion rate is improved with the stabilization of the oil recovery. be able to.
[0034]
In addition, since the high-temperature gas blown into the gas generating chamber 11 is generated by burning the dry distillation gas after oil recovery in the dry distillation gas combustion furnace 31, the combustion exhaust gas does not contain oxygen gas, or In addition, it is possible to easily and reliably obtain a high-temperature gas in a state of being reduced to an extremely small amount, and it is possible to effectively use the carbonized gas after the oil recovery which has been conventionally discarded.
<Second embodiment>
-Configuration of the second embodiment-
Figure 3,2 shows a dry distillation type oil converting apparatus according to a second embodiment. In the second embodiment, the high-temperature gas generating means 3 (see FIG. 1) is composed of a dry distillation gas burning means 3a for a steady operation stage and an independent high-temperature gas generating means 3b for a start-up stage, and these are switching means. The switching valve 38 is used to switch according to the operation stage. Therefore, the gas generating furnace 1b according to the second embodiment is configured by omitting the combustion burner 17 for starting, like the gas generating furnace 1a according to the first embodiment.
[0035]
The carbonization gas combustion means 3a includes a carbonization gas introduction pipe 30, a carbonization gas combustion furnace 31, and a high-temperature gas discharge pipe 32 having the same configuration as that of the first embodiment. The switching valve 38 is interposed at an intermediate position between the two.
[0036]
The independent hot gas generating means 3b is,LeaksIn the furnaceConsists of coal, cokeTheAs a fuel, a high-temperature gas containing no oxygen gas at high temperature is generated by a combustion exhaust gas composed of carbon dioxide (CO2), carbon monoxide (CO), nitrogen (N2) and the like obtained by burning them. I have. The downstream end of the high-temperature gas outlet pipe 39 connected to the independent high-temperature gas generating means 3b is connected to the switching valve 38.
[0037]
The switching valve 38 is configured to be capable of switching between a starting side and a steady side by using, for example, a three-way switching valve or the like. By switching the switching valve 38 to the starting side, only the high-temperature gas outlet pipe 39 and the gas generating chamber 11 are communicated with each other. Only the generation chamber 11 is communicated with each other.
[0038]
Since other configurations of the dry distillation type oil-forming apparatus are the same as those of the first embodiment, the same members are denoted by the same reference numerals and description thereof will be omitted.
[0039]
-Operation and effect of the second embodiment-
In the case of the second embodiment having the above-described configuration, first, in the starting stage, the switching valve 38 is set to the starting side, and the independent high-temperature gas generating means 3b is communicated with the gas generating chamber 11. A high temperature gas (for example, 800 to 900 ° C.) is blown into the gas generation chamber 11. The inside of the gas generation chamber 11 is heated and heated by the high-temperature gas, and when the temperature reaches a predetermined temperature (for example, approximately 400 ° C.), the thermal decomposition of the raw material starts, and a carbonization gas is generated. Then, the carbonized gas is introduced into the carbonized gas combustion furnace 31 through the carbonized gas introduction pipe 30 after the oil content is recovered by the oil recovery means 2.
[0040]
Next, in a steady operation stage in which the carbonization gas is generated steadily, the switching valve 38 is switched to the stationary side, and the carbonization gas combustion furnace 31 of the carbonization gas combustion means 3a is communicated with the gas generation chamber 11, and A high-temperature gas similar to the above is blown into the gas generation chamber 11 from the carbonization gas combustion furnace 31. Thereafter, the raw material is thermally decomposed by the high-temperature gas from the carbonization gas combustion furnace 31, and the generation of the carbonization gas is continued, and the recovery of the oil is continuously performed.
[0041]
Accordingly, in all the operation stages from the start-up stage to the steady operation stage, the entire amount of the raw material filled in the gas generation chamber 11 can be subjected to oil conversion, and the oil conversion rate is improved as compared with the case of the first embodiment. Can be achieved. For example, when natural rubber is used as a raw material, when the furnace temperature is in the range of 350 to 400 ° C., the oil conversion is 65%. When ethylene propylene (EP) rubber is used as the raw material, the furnace temperature is Is 470 to 520 ° C., the oil conversion is 70%. When resinous polyolefin is used as the raw material, the oil conversion is 550 to 600 ° C. The oiling rate can be greatly improved from the conventional oiling rate of about 50% so that the oiling rate is 63%. The value of the above oil conversion ratio is a result when a raw material consisting only of an organic portion that can be converted to oil is used. However, 30 to 70% by weight of an inorganic substance such as a copper conductor is contained as in a rubber-coated cable. Even if the raw material is used, it is necessary to inject extra high-temperature gas by the amount of heat for heating the inorganic substance, but the same oil conversion rate as above can be obtained.
[0042]
Further, the fuel in the independent high-temperature gas generating means 3b is recovered by the oil recovery means 2 by the operation up to the previous time, and the generated oil stored in the oil tanks 27 and 28 is used. In combination with the use of the carbonized gas, the carbonized gas generated in the gas generating furnace 1b can be more effectively used, and the energy balance can be improved.
<Other aspects>
Note that,UpThe present invention is not limited to the first and second embodiments, but includes various other modifications. That is, in the first embodiment, the amount of heat for pyrolysis is obtained from the combustion burner 17 in the start-up stage and from the carbonization gas combustion means 3a in the steady operation stage, respectively. Is obtained from the independent high-temperature gas generating means 3b in the start-up stage and from the carbonization gas combustion means 3a in the steady-state operation stage, but is not limited thereto. For example, in both the start-up stage and the steady-state operation stage, May be obtained by the high-temperature gas from the independent high-temperature gas generating means 3b. That is, as shown in FIG. 4, the independent high-temperature gas generating means 3 alone constitutes the high-temperature gas generating means 3, and the independent high-temperature gas generating means 3 is independent of the start-up stage and the steady-state operation stage. The thermal decomposition of the raw material in the gas generating chamber 11 may be performed only by the high-temperature gas blown from 3b.
[0043]
In the first and second embodiments, in the combustion control in the carbonization gas combustion furnace 31, the control of the amount of air from the air supply device is performed by the controller. However, the present invention is not limited to this. Alternatively, the amount of the oxygen gas supplied from the oxygen cylinder may be controlled.
[0044]
By connecting the combustion burner 17 and the oil tanks 27 and 28 in the first embodiment, the oil already stored in the oil tanks 27 and 28 by the previous operation is used as the fuel for the combustion burner 17. It may be. This makes it possible to effectively use the recovered oil and improve the energy balance.
[0045]
In the second embodiment, the switching valve is exemplified as the supply switching means. However, the present invention is not limited to this. For example, the dry distillation gas combustion furnace 31 and the independent high-temperature gas generating means 3b may be individually connected to the dry distillation furnace 1b via on-off valves. May be connected.
[0046]
In the first and second embodiments, the combustion in the carbonization gas combustion furnace 31 is controlled to an incomplete combustion state to obtain a high-temperature gas containing no oxygen gas or reduced as much as possible. For example, it is also possible to obtain a combustion exhaust gas containing no oxygen gas by controlling the above-mentioned combustion to a precise complete combustion state.
[0047]
【The invention's effect】
As described above, according to the dry distillation type oil conversion apparatus of the first aspect of the present invention, the polymer material does not self-burn even when it comes into contact with the polymer material during thermal decomposition. High-temperature gas generating means for generating high-temperature gas is provided, and the high-temperature gas generating means is connected to the carbonization furnace such that only the high-temperature gas is blown into the carbonization furnace as a heat medium for thermally decomposing the polymer material in the carbonization furnace. Therefore, the entire amount of the polymer material filled in the dry distillation furnace can be subjected to oilification by thermal decomposition. Therefore, compared to the conventional apparatus in which air is continuously supplied into the furnace and part of the polymer material is self-burned to obtain heat for pyrolysis, the polymer material to be self-burned is also oiled. It is possible to improve the oil conversion rate by expanding the oil conversion target. In addition, since the high-temperature gas blown into the carbonization furnace does not cause the raw material to self-combust at the thermal decomposition temperature, the generation of the carbonized gas by the thermal decomposition can be stabilized, and the oil recovery can be stabilized. In addition, the oil conversion rate can be further improved.
[0048]
In addition, since the temperature of the carbonization furnace can be controlled by the heat of the high-temperature gas itself, that is, the control of the thermal decomposition conditions can be performed, the thermal decomposition conditions can be adjusted by adjusting the combustion state by adjusting the conventional air supply amount. Compared with the case of the controlling device, the control of the thermal decomposition conditions can be performed easily and accurately, and the thermal decomposition conditions can be maintained in a stable state.
[0049]
further, KiIn the operation stage, the inside of the dry distillation furnace is heated by the high-temperature gas from the independent high-temperature gas generating means to start the thermal decomposition of the polymer material, and in the steady operation stage, the high-temperature gas from the dry distillation gas burning means causes the above-mentioned polymer material to decompose. Thermal decomposition can be continued. This allows the entire amount of the polymer material filled in the carbonization furnace to be liquefied during all operation stages from the start-up stage to the steady-state operation stage of the apparatus, thereby further improving the liquefaction rate. Can be planned.
[Brief description of the drawings]
FIG. 1 is a configuration diagram of the present invention.
FIG. 2No.It is a schematic structure figure showing one example.
FIG. 3 is a schematic configuration diagram showing a second embodiment.
FIG. 4 is a schematic configuration diagram showing another embodiment.
FIG. 5 is a schematic configuration diagram showing an example of a conventional device.
FIG. 6 is a diagram showing the basic configuration of a conventional device.
[Explanation of symbols]
1 carbonization furnace
1a, 1b Gas generating furnace (dry distillation furnace)
2 Oil recovery means
3 High-temperature gas generating means
3a Carbonized gas combustion means (high-temperature gas generation means)
3b Independent high-temperature gas generating means (high-temperature gas generating means)
38 Switching valve (supply switching means)

Claims (1)

A carbonization furnace that pyrolyzes the polymer material to generate carbonization gas,
Oil recovery means connected to the carbonization furnace and separating and recovering oil by cooling the carbonization gas;
A high-temperature gas generating means for generating a high-temperature gas that does not cause self-combustion of the polymer material even when the polymer material comes into contact with the material at a thermal decomposition temperature,
The high-temperature gas generating means and the dry distillation furnace are connected to each other so that only the high-temperature gas is blown into the dry distillation furnace as a heat medium for thermally decomposing the polymer material ,
The high-temperature gas generating means,
A dry distillation gas combustion means for generating a high-temperature gas from a combustion exhaust gas obtained by burning the remaining dry distillation gas from which oil has been recovered by the oil recovery means,
Independent high-temperature gas generation means provided separately from the carbonization gas combustion means and independently generating high-temperature gas,
The connection between the carbonized gas combustion means and the independent high-temperature gas generation means and the carbonization furnace is established by starting the high-temperature gas from the independent high-temperature gas generation means into the carbonization furnace at the start-up stage, and increasing the high-temperature gas from the carbonization gas combustion means during the steady operation stage. Supply switching means for switching the gas to be blown into the carbonization furnace,
The dry distillation type oil converting apparatus, wherein the independent high temperature gas generating means is constituted by a coke oven.

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