JP2007029869A - Treatment method of organic wastes - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a treatment method of organic wastes which can make a contained heavy metal harmless and can change the metal to a valuable material to effectively use it, by heating and carbonizing organic wastes to convert them to a carbonized residue and melting an obtained solid material to slag it. <P>SOLUTION: The treatment method of the organic wastes consists of a carbonization step, as the A step, for heating the organic wastes using a carbonization treatment apparatus 1A and a melt slagging step, as the B step, for introducing the carbonized residue obtained in the A step in a rotary combustion apparatus 6 to melt it by heating reduction, using a slagging treatment apparatus 1B, wherein the carbonization treatment apparatus 1A has a reforming furnace 1 having a water-content introduction pipe 16, a gas introduction pipe 14 and a gas discharging pipe 15, a pyrolysis furnace 2 which is mostly surrounded by the reforming furnace and has a plurality of gas drawing pipes 21 in its peripheral side, a supplying apparatus 51, to be connected, of the organic wastes and an discharging apparatus 52 at another end, and the slagging treatment apparatus 1B consists of the rotary combustion apparatus 6 with a reductive-gas supplying opening 61 and a melting chamber 8 connected to its bottom part. <P>COPYRIGHT: (C)2007,JPO&INPIT

Description

  The present invention relates to a method for treating organic waste, and more particularly to a method for treating organic waste in which organic waste is heated and distilled to form a molten slag.

Conventionally, landfill disposal or incineration landfill disposal by incineration has been performed as a method of treating organic waste such as garbage (raw garbage), municipal waste such as paper and fibers, waste wood, thinned wood, plastics, etc. Yes. However, since the allowable amount of landfill disposal sites is approaching the limit, it is desired to recycle organic waste and make the landfill disposal amount substantially zero. As one of such recycling methods, a method is known in which municipal waste is pulverized, carbonized by carbonization, and the resulting carbide (carbonization residue) is used as fuel.
Japanese Patent No. 2001-288474

  However, since the carbide obtained by the above processing method contains heavy metals, when used as a fuel, an electric dust collector or the like must be placed in the flue to collect and recover the heavy metals. It must be economical.

  The present invention has been made in view of the above circumstances, and its purpose is to contain organic waste by heating and distilling the organic waste and melting the obtained dry distillation residue to form slag. An object of the present invention is to provide a method for treating organic waste, which can detoxify heavy metals and convert organic waste into valuable substances for effective use.

  That is, the gist of the present invention includes a dry distillation step consisting of the following step A using organic waste as a raw material and a melt slag forming step consisting of the following B step using the dry distillation residue obtained in the step A as a raw material. It exists in the processing method of the organic waste characterized by this.

  In the step A, a reforming furnace having a water and / or steam moisture introduction pipe, a gas introduction pipe and a gas discharge pipe, and the majority of the reforming furnace is surrounded by a reforming furnace, and a plurality of gases are provided on the peripheral surface thereof. Use a carbonization treatment device equipped with a pyrolysis furnace with a vent pipe, an organic waste supply device connected to one end of the pyrolysis furnace, and a discharge device at the other end, and an organic system for the pyrolysis furnace Combustible gas and oxidant generated by heating and dry distillation in the pyrolysis furnace and ejected from the degassing pipe are mixed in the reforming furnace, and the combustible gas is at least partially burned to generate the pyrolysis furnace. It is a dry distillation process which heats.

  Step B is composed of a cylindrical rotating combustion device having at least one pair of reducing gas supply ports composed of two, and a melting chamber connected to the bottom of the rotating combustion device, and each of the reducing gases described above. Using a slagging treatment device that is arranged at intervals in the longitudinal direction of the swirl combustion device so that vortex flows in opposite directions to the swirl combustion device are generated at the supply port, the dry distillation residue obtained in step A is used. It is a molten slag forming step that is introduced into the revolving combustion device and melted by heat reduction.

  ADVANTAGE OF THE INVENTION According to this invention, while making the heavy metal contained in an organic waste harmless, it can convert an organic waste into the precursor (slag) of a valuable substance, and can utilize it effectively. Further, the fuel for heating and carbonizing can be remarkably reduced, and the amount of heat energy required for melting the carbonization residue to form slag can be reduced.

  Hereinafter, the organic waste processing method according to the present invention will be described with reference to the drawings. FIG. 1 is a process diagram showing a method for treating organic waste according to the present invention. FIG. 2 is a partially broken side view showing components of the carbonization apparatus used in the process A (dry distillation process). FIG. 3 is a side view showing the structure of the main part of the pyrolysis furnace of the carbonization treatment apparatus of FIG. 2, and FIG. 4 shows the internal structure of the pyrolysis furnace of the carbonization treatment apparatus of FIG. It is sectional drawing shown by the cross section along the -B line.

  As shown in FIG. 1, the organic waste treatment method of the present invention includes a dry distillation step comprising the following step A using organic waste as a raw material, and a dry distillation residue obtained in the above step A as a raw material. This is a method including a melt slag forming step consisting of step B.

  First, the carbonization apparatus (1A) used at A process (dry distillation process) is demonstrated. As shown in FIG. 2, the carbonization treatment apparatus (1A) is provided with a water introduction pipe (16) for introducing water and / or steam, a gas introduction pipe (14), and a gas discharge pipe (15). It is mainly composed of a furnace (1) and a pyrolysis furnace (2) rotatably inserted into the reforming furnace (1) and provided with a plurality of degassing pipes (21) on its peripheral surface. An organic waste supply device (51) is connected to one end (the left end in FIG. 2) of the cracking furnace (2), and the other end (the right end in FIG. 2) of the pyrolysis furnace (2). ) Is provided with a discharge device (52) including a gate valve.

  The reforming furnace (1) is usually a fixed furnace installed on the foundation, and the gas introduction pipe (14) and the water introduction pipe (16) are located at the bottom on one end side of the reforming furnace (1). The gas discharge pipe (15) is connected in the vicinity and is connected to the upper part on the other end side of the reforming furnace (1). The reforming furnace (1) is installed in a state inclined about 1-2 degrees with respect to the horizontal level in order to incline the axis of the pyrolysis furnace (2).

  The pyrolysis furnace (2) is a rotary furnace having a structure similar to a general metal rotary kiln. The pyrolysis furnace (2) is rotatably inserted into both ends of the reforming furnace (1) via seal portions (1s) so that the gas inside the reforming furnace (1) does not leak to the outside. The both ends of the pyrolysis furnace (2) are rotatably supported by receiving a reinforcing ring (22) mounted on the outer periphery of these both ends with a support roller (42). On the other hand, an electric motor (3) is installed on the side of one end side of the reforming furnace (1), and a gear attached to the outer peripheral portion of the driving gear (32) of the electric motor (3) and one end of the pyrolysis furnace (2). (23) meshes, and the pyrolysis furnace (2) rotates in one direction at a speed of, for example, 0.3 to 10 rpm.

  Moreover, the open | released one end of the thermal decomposition furnace (2) is airtightly sealed by the hood (41) with which it mounted | worn through the seal part (41s) as a sliding member. Furthermore, the food | hood (41) is provided with the supply apparatus (51) for charging the organic waste crushed with the crusher, and such a supply apparatus (51) is a hopper (51h), for example. Consists of a provided screw conveyor. Therefore, the organic waste can be supplied to the rotating pyrolysis furnace (2) by introducing the organic waste into the hopper (51h).

  On the other hand, the other open end of the pyrolysis furnace (2) is hermetically sealed by a hood (43) mounted via a seal portion (43s) as a sliding member. Furthermore, the above-mentioned discharge device (52) for taking out the dry distillation residue is provided at the lower part of the hood (43). The discharge device (52) is configured by arranging a plurality of stages of gate valves having a shutter structure in the vertical direction. Therefore, by operating the discharge device (52) from the pyrolysis furnace (2), the obtained dry distillation residue can be taken out from the apparatus without causing the flammable gas generated in the pyrolysis furnace to leak out. I can do it.

  Moreover, in order to take out the combustible gas which generate | occur | produced in the inside to the reforming furnace (1), many degassing pipes (21) are attached to the pyrolysis furnace (2). As shown in FIGS. 3 and 4, the gas vent pipe (21) is inserted from the peripheral surface portion of the pyrolysis furnace (2) to the position of the center line of the pyrolysis furnace. The vent pipes (21) are arranged at a constant pitch along the length direction of the pyrolysis furnace (2), and each adjacent vent pipe (21) is a center line of the pyrolysis furnace (2). Is used as a reference, the peripheral surface portions are extended in directions shifted by 90 ° from each other. That is, when viewed from one end side of the pyrolysis furnace (2), a large number of gas vent pipes (21) are extended from the center to the peripheral surface portion in a state of being sequentially shifted in a spiral shape. Furthermore, the open | released front-end | tip part of each degassing pipe | tube (21) located in the center part of pyrolysis furnace (2) is the other end side of pyrolysis furnace (2), ie, to-be-processed object (organic to be processed). It is bent toward the downstream side in the flow direction of the system waste).

  In the carbonization treatment apparatus (1A), as described above, a large number of gas vent pipes (21) are arranged substantially uniformly over the entire pyrolysis furnace (2), so that the pyrolysis furnace (2 ) Can be efficiently discharged to the reforming furnace (1), and the degassing pipe (21) extends to the center line of the pyrolysis furnace (2). A larger amount of organic waste can be treated in the cracking furnace (2). Moreover, because the tip of the gas vent pipe (21) is bent inside the pyrolysis furnace (2), the gas is released by solid components (organic waste and its dry distillation residue) inside the pyrolysis furnace (2). The blockage of the pipe (21) and the falling of the solid component into the reforming furnace (1) can be prevented. As the structure of the gas vent pipe (21), various structures such as a filter structure can be adopted as long as only the combustible gas generated in the pyrolysis furnace (2) can pass therethrough.

  Next, the slag-processing apparatus (1B) of the dry distillation residue used at B process is demonstrated. The slag processing device (1B) is connected to at least one set of two, for example, a substantially cylindrical rotating combustion device (6) having two reducing gas supply ports (62), and a bottom portion of the rotating combustion device. The cyclone melter (7) and a melting chamber (8) connected to the cyclone melter (7). The whirling combustion device (6) is a chamber for producing slag by melting dry distillation residue with a high-temperature reducing gas. Usually, the main body has, for example, a cylindrical shape with a part of an inverted frustum on the lower end side. It is formed and is provided with a dry distillation residue insertion port at its top.

  Each said reducing gas supply port (62) is normally attached to the upper part of the main body of a revolving combustion apparatus (6). These are located on the opposite sides of the center line of the main body of the swirl combustion device (6), for example, two parallel tangents, so that vortex flows in opposite directions are generated in the swirl combustion device (6). Are arranged at intervals approximately 1/4 to 1 times as large as the diameter of the main body of the swirling combustion device (6). As a result, a disadvantage in the case of unidirectional vortex flow, that is, a counter airflow is generated in the swirl combustion device (6) to form an ascending air current, and the dry distillation residue does not descend and adheres to the inner wall of the swirl combustion device (6). The disadvantage of blocking is eliminated. Each gas introduction pipe (62) is connected to a reducing gas supply line (61) for supplying a reducing gas.

  The melting chamber (8) connected to the cyclone melter (7) at the bottom of the swirling combustion device (6) is a processing vessel for generating uniform slag. An extraction port (81) for taking out molten slag is provided at the bottom of the melting chamber (8), and exhaust gas introduced from the rotating combustion device (6) is extracted at the upper part of the melting chamber (8). A gas exhaust pipe (82) is provided. The exhaust gas extracted from the gas exhaust pipe (82) can also be used as fuel for gas turbines, boilers, and the like.

  Next, the process method of this invention including the A process (dry distillation process) using said carbonization apparatus (1A) and the B process (melting slag conversion process) using the slag processing apparatus (1B) is demonstrated.

  First, A process (dry distillation process) is demonstrated. Process A is a process of decomposing organic waste into dry distillation residue and combustible gas. In such a process, the carbonization apparatus (1A) is used, and organic waste is supplied to the thermal cracking furnace (2) for heating and dry distillation. And the combustible gas produced | generated in the pyrolysis furnace (2) is injected in a reforming furnace (1) from the degassing pipe | tube (21) provided in the surrounding surface of the pyrolysis furnace (2). The ejected combustible gas is mixed with the oxidant supplied from the gas introduction pipe (14) in the reforming furnace (1) to at least partially burn the combustible gas, and is supplied from the moisture introduction pipe (16). Mixing with fresh water and / or steam causes a water gasification reaction to lighten and reform the combustible gas. And a pyrolysis furnace (2) is heated by the at least partial combustion of the above-mentioned combustible gas, and organic waste is heat-distilled. The aforementioned “at least partial combustion” includes complete combustion of combustible gas.

  In the present invention, the oxygen concentration in the reforming furnace (1) is usually controlled to be 12% by volume or less when performing the heating and dry distillation. The above-described method for controlling the oxygen concentration in the reforming furnace (1) to 12% by volume or less adjusts the amount of oxidant supplied from the oxidant introduction pipe (14) to the reforming furnace (1). Therefore, the oxygen concentration in the reforming furnace (1) is usually 12% by volume or less, preferably 8% by volume or less. If the oxygen concentration in the reforming furnace (1) exceeds 12% by volume, a large-volume gasification furnace is required, which is not economical.

  In order to suppress the generation of dioxins in the reforming furnace (1), it is necessary to completely burn the combustible gas. Therefore, if the amount of oxidant supplied to the reforming furnace (1) is increased and the combustible gas is completely burned, the generation of dioxins can be suppressed. However, since the amount of flammable gas generated is large, the amount of oxidant supplied is also large. As a result, a large-volume pyrolysis furnace and reforming furnace are required, which is not economical.

  Therefore, in the reforming furnace (1), the amount of combustible gas required to supply the amount of heat necessary for heating and dry distillation of the organic waste in the pyrolysis furnace (2) is burned. The remaining combustible gas is discharged from the gas discharge pipe (15) without being burned, and is processed in the following manner. For example, (i) a method of using as a reducing gas supplied to the rotating combustion apparatus in step B, (ii) a method of complete combustion in a combustion furnace (not shown) newly provided in a subsequent step, or (iii) There is a method of using it as a fuel after lightening or reforming with a reformer (not shown).

  The amount of water and / or steam supplied into the reforming furnace (1) is usually 0.4 to 5 times by weight with respect to the amount of organic components in the organic waste (absolutely dry state). When the amount of water and / or steam is less than 0.4 times by weight, the pyrolysis furnace (2) is excessively heated, and it is difficult to control the dry distillation operation. When the amount of water and / or steam exceeds 5 times by weight, it is difficult to lighten and reform the combustible gas.

  The supplied water and / or steam causes a water gas reaction of the combustible gas in the reforming furnace (1), and the combustible gas is lightened and reformed. Further, since the combustible gas is diluted with steam in the reforming furnace (1), polymerization and tarification of the combustible gas are suppressed. And tar content and coke are gasified by the lightening of combustible gas, and the coking progress speed of the reformer (1) inner surface is controlled.

  Furthermore, even if the composition and properties of organic waste vary, the amount of water gas reaction and the amount of heat generated can be easily increased by increasing or decreasing the amount of water and / or steam supplied to the reforming furnace (1). Since it can be adjusted, it is possible to stabilize the dry distillation operation without running out of control. As a result, the organic waste is not discharged from the pyrolysis furnace (2) with insufficient heating and dry distillation, and the pyrolysis furnace (2) is not excessively heated.

  The amount of water and / or steam supplied to the reforming furnace (1) is controlled by a control system (not shown) that maintains the outer surface temperature of the pyrolysis furnace (2) within a predetermined temperature range. This operation stabilization control uses heat generation due to partial combustion of combustible gas and endotherm (including evaporation and heating) due to water gas reaction with water and / or steam from steam. is there. The operation can be stabilized not only by adjusting the supply amount of water and / or steam, but also by adjusting the supply amount of the oxidizing agent and the supply amount of organic waste to the reforming furnace (1).

  The temperature in the reforming furnace (1) is usually 600 to 750 ° C, preferably 600 to 650 ° C. The pressure in the reforming furnace (1) is set so that the heavy combustible gas generated in the pyrolysis furnace (2) can be ejected to the reforming furnace (1). Is kept slightly lower than the gas pressure.

  The heating and distillation of the organic waste in the pyrolysis furnace (2) is usually performed in an air shut-off state. Therefore, the oxygen concentration in the pyrolysis furnace (2) is usually 0% by volume. However, when oxygen is contained in the organic waste as a raw material, it may be present as oxygen gas in the combustible gas in the pyrolysis furnace (2) due to thermal decomposition during heating and dry distillation. And when the temperature in a pyrolysis furnace (2) is higher than the ignition temperature of combustible gas, the produced | generated oxygen gas can burn the combustible gas for the oxygen equivalent (partial combustion).

  Therefore, the oxygen concentration in the pyrolysis furnace (2) is usually 1% by volume or less, preferably 0.1% by volume or less, more preferably 0% by volume. When the oxygen concentration exceeds 1% by volume, it is difficult to heat and distill the organic waste, and it is difficult to suppress the generation of dioxins.

  The temperature in a pyrolysis furnace (2) is 500-600 degreeC normally, Preferably it is 550-600 degreeC.

  Due to the partial combustion in the pyrolysis furnace (2), tar and coke adhered to the inner surface of the pyrolysis furnace (2) are also burned. Note that the amount of heat transmitted from the outside of the pyrolysis furnace (2) is reduced by the amount of heat generated by partial combustion in the pyrolysis furnace (2), although it is small. Therefore, the temperature of the pyrolysis furnace (2) is kept low, the burden on it (heat resistance of the material) is reduced, and it becomes possible to use a material with low heat resistance. In addition, the combustible gas is diluted with the steam and other gases generated by the partial combustion described above and / or reacts with the steam to water gas, thereby suppressing the generation of tar and coke in the pyrolysis furnace (2). At the same time, the coking progress speed is suppressed, and the continuous operation period can be extended.

  According to the present invention, the heat necessary for gasifying the organic waste in the pyrolysis furnace (2) is sufficiently covered by at least partial combustion of the combustible gas in the reforming furnace (1). Refined and expensive fuel is almost unnecessary.

  The produced dry distillation residue is discharged from the carbonization apparatus (1A) through the discharge apparatus (51) connected to the other end of the pyrolysis furnace (2).

  Examples of organic wastes to be processed by the carbonization apparatus (1A) of the present invention include garbage (raw garbage), municipal waste such as papers and fibers, waste wood, thinned wood, plastics, and car shredder dust. (ASR: Automobile Shredder Residue), waste electrical appliances, waste OA equipment, waste such as sewage sludge.

  Examples of the oxidizing agent used in the carbonization apparatus (1A) of the present invention include oxygen gas or a gas containing oxygen, and specifically include air, oxygen, and oxygen-enriched air.

  The dry distillation residue obtained in the step A (dry distillation step) is a residue obtained by subjecting the above-mentioned object to be subjected to dry distillation treatment, and mainly contains elements such as C, Si, Ca, Mg, Al, and Fe.

  Then, B process (melting slag formation process) is demonstrated. In the B process, the slag processing apparatus (1B) is used, and the dry distillation residue obtained in the A process is introduced into the revolving combustion apparatus (6) from the top, and is melted by being heated and reduced with a high-temperature reducing gas. It is a conversion process.

  The above-described high-temperature reducing gas is a gas for converting slag into dry distillation residue, and each reducing gas is passed through the reducing gas supply line (61) so as to form vortex flows in opposite directions in the swirling combustion device (6). It is injected from the introduction pipe (62) into the swirl combustion device (6). The dry distillation residue supplied from above is sufficiently agitated by the above-described vortex of the high-temperature reducing gas to be in a uniform suspended state, slags into contact with the high-temperature reducing gas, and melts while falling.

The temperature in the swirling combustion device (6) is usually 1350 to 1500 ° C. from the viewpoint of performing appropriate smelting reduction. When the temperature in the swirling combustion device (6) is lower than 1350 ° C., the dry distillation residue may not be slagged. On the other hand, when the temperature exceeds 1500, the contribution rate to slag formation of the dry distillation residue is small and uneconomical for the high temperature. The amount of the high-temperature reducing gas introduced into the rotating combustion device (6) is usually 0.2 to 1.2 Nm ³ / kg-dry distillation as the amount with respect to the dry distillation residue introduced into the rotating combustion device (6). It is a residue.

  The high-temperature reducing gas introduced from the reducing gas introduction pipe (62) is a gas containing hydrogen and / or carbon monoxide. As reducing gas, the combustible gas discharged | emitted from the gas exhaust pipe (15) of the carbonization apparatus (1A) in A process is used. Thereby, the amount of thermal energy required for slag formation can be reduced. When only the combustible gas discharged from the carbonization treatment device (1A) cannot cover the amount of reducing gas introduced into the revolving combustion device (6), it is a gas, liquid or solid fossil fuel, waste plastic, waste rubber. Gas produced by burning flammable waste such as ASR (also called Automobile Shredder Residue) can also be used.

  Next, the slag obtained by melting and reducing in the rotating combustion apparatus (6) is connected to the cyclone melter (7) via the cyclone melter (7) at the bottom of the rotating combustion apparatus (6). It is sent to (8), homogenized, and taken out from the outlet (81) at the bottom of the melting chamber (8). Further, the reduced exhaust gas fed from the rotating combustion device (6) is extracted from the upper space of the melting chamber (8) through the gas discharge pipe (82). The melting chamber (8) is maintained at a temperature at which the molten slag does not solidify, for example, usually 1400 to 1550 ° C. The molten slag (precious material precursor) taken out from the outlet (81) is cooled and pulverized to form a roadbed material that is a valuable material.

  EXAMPLES Hereinafter, although an Example demonstrates this invention still in detail, this invention is not limited to a following example, unless the summary is exceeded.

Example 1:
Process A (dry distillation process): First, a carbonization treatment apparatus (1A) shown in FIG. 1 was used to perform a dry distillation process of organic waste. That is, municipal waste as organic waste is supplied from the supply device (51) to the pyrolysis furnace (2), and steam is supplied from the moisture introduction pipe (16) and air from the gas introduction pipe (14). The mixture was supplied to (1) and subjected to heating and carbonization to produce a carbonization residue. Table 1 shows the operating conditions of the carbonization treatment apparatus (1A), Table 2 shows the composition of the exhaust gas from the gas discharge pipe (15), and Table 3 shows the composition of the dry distillation residue.

  The dust concentration, nitrogen oxide concentration, sulfur oxide concentration, hydrogen chloride concentration and dioxin concentration in Table 2 were measured by the following methods.

  The dust concentration was determined according to the method described in JIS Z 8808.8. The nitrogen oxide concentration was determined according to the method described in JIS K 0104.4.2. The sulfur oxide concentration was determined in accordance with the method described in JIS K0103.6.1. The hydrogen chloride concentration was determined according to the method described in JIS K 0107.6.2. The concentration of dioxins was determined according to the method described in the “Manual for Standard Measurement and Analysis of Dioxins in Waste Treatment” (Environmental Maintenance Division, Department of Health and Welfare, February 1997).

  In addition, carbon of the carbonization residue in Table 3 was measured by a known industrial analysis method for coals and cokes, and other components were measured by a known X-ray analysis method.

Step B: The slagging treatment apparatus (1B) shown in FIG. That is, the dry distillation residue discharged from the discharge device (52) of the carbonization treatment device (1A) in step A was introduced from the top of the rotating combustion device (6) and melted and reduced with a high-temperature reducing gas. Next, the molten slag was homogenized in the melting chamber (8), cooled and pulverized to obtain slag (precursor of valuable material). The amount of dry distillation residue introduced was 25 kg / hr, the amount of hot reducing gas introduced was 8.0 Nm ³ / hr, and the amount of slag produced was 12 kg / hr. In addition, as a result of random sampling of the obtained slag and component analysis by X-ray, the fracture surface was homogeneous with almost no component variation in the sample. As a result, it was suitable as a precursor of roadbed material which is a valuable material. Table 4 shows the operating conditions of the smelting reduction treatment in the swirl combustion device (6) and the homogenization of the molten slag in the melting chamber (8).

Process drawing showing a method for treating organic waste according to the present invention Side view of a partially broken view showing components of a carbonization apparatus used in step A (dry distillation step) Side view showing the structure of the main part of the pyrolysis furnace of the carbonization apparatus of FIG. Sectional drawing which showed the internal structure of the thermal decomposition furnace of the carbonization apparatus of FIG. 2 with the cross section along the BB line orthogonal to a centerline

Explanation of symbols

DESCRIPTION OF SYMBOLS 1A: Carbonization processing apparatus 1B: Slag processing apparatus 1: Reforming furnace 14: Gas introduction pipe 15: Gas discharge pipe 16: Moisture introduction pipe 1s: Seal part 2: Pyrolysis furnace 21: Gas vent pipe 22: Reinforcement ring 23 : Gear 3: Electric motor 32; Drive gear 41: Hood 41 s: Sealing part 42: Support roller 43: Hood 43 s: Sealing part 51: Feeding device 51 h: Hopper 52: Discharging device 6: Rotating combustion device 61: Reducing gas supply line 62 : Reduction gas introduction pipe 7: Cyclone melter 8: Melting chamber 81: Extraction port 82: Gas discharge pipe

Claims (2)

An organic waste comprising a dry distillation step comprising the following step A using organic waste as a raw material, and a molten slag forming step comprising the following B step using the dry distillation residue obtained in the step A as a raw material Processing method.
Step A: a reforming furnace having a water and / or steam moisture introduction pipe, a gas introduction pipe, and a gas discharge pipe, and most of the reformer is surrounded by the reforming furnace, and a plurality of gas vents are formed on the peripheral surface thereof. Use a carbonization device equipped with a pyrolysis furnace with a pipe, connected to an organic waste supply device at one end of the pyrolysis furnace, and provided with a discharge device at the other end. The combustible gas generated by the heating dry distillation in the pyrolysis furnace and ejected from the degassing pipe is mixed in the reforming furnace, and at least a partial combustion of the combustible gas is performed. Heating dry distillation process B process: It is comprised from the cylindrical revolving combustion apparatus which has at least 1 set of 2 reducing gas supply ports which consists of two, and the melting chamber connected to the bottom part of the revolving combustion apparatus, Each reducing gas supply port is connected to the rotating combustion device. Then, using a slagging device disposed at intervals in the longitudinal direction of the rotating combustion device so as to generate vortex flows in opposite directions, the dry distillation residue obtained in step A is introduced into the rotating combustion device, Melting slag process that melts by heat reduction   The processing method according to claim 1, wherein the exhaust gas discharged from the reforming furnace is provided as a reducing gas to a revolving combustion apparatus.

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