JP3272581B2 - Superheated steam production equipment using waste incineration heat - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to the production of superheated steam by incinerating municipal refuse or industrial waste, producing steam by the heat of the combustion exhaust gas, and using the steam in a power plant or the like. .

[0002]

2. Description of the Related Art Conventionally, fluidized bed incinerators are often used as incinerators for incinerating waste such as municipal solid waste, and such apparatuses are accommodated on a dispersion plate (for example, a perforated plate) in a fluidized bed incinerator. The fluidized medium is fluidized and heated by blowing air or incineration exhaust gas etc. from below the dispersion plate into the fluidized medium such as sand, and waste such as municipal solid waste is thrown into the fluidized bed thus formed. Burn. The combustion gas generated by the combustion reaches a boiler via a combustion gas outlet line, generates steam by thermal contact with hot water in the boiler, and uses the steam as a turbine drive source of a power plant or the like.

[0003]

The waste such as municipal solid waste contains a chlorine-containing organic compound such as PVC plastic, and the flammable component has a C1 content of about 0.2 to 0.1%.
Contains 5%. Chlorine contained in PVC plastic and the like mixed into waste such as municipal waste becomes HC1 by combustion (usually, HC1 contained in flue gas from municipal waste combustion).
(1 is about 500 to 1000 ppm), which acts on the tube of the steam generation boiler installed downstream of the incinerator to corrode it. In particular, when the tube surface temperature is about 350 ° C. or higher, high-temperature corrosion becomes remarkable as the temperature increases.

Therefore, conventionally, the tube surface temperature is 35
The temperature of the steam to be produced was limited to about 300 ° C. As a result, the power generation efficiency of the conventional refuse incineration is about 15% or less, and the power generation efficiency of a plant that can use boiler tube temperature of 500 to 600 ° C. using heavy oil or LNG containing almost no chlorine as fuel is used.
%, Which is significantly lower than the above, and its improvement has been strongly desired.

[0005] In view of such technical problems, the present inventors have filed an earlier application (application number: Japanese Patent Application No. 6-324843).
, In a fluidized bed as the incinerator, at a temperature of 300 to 700 ° C.
It has been found that a char mixture consisting of the uncracked residue from the fluidized bed and the fluidized medium results in a substantially chlorine-free uncracked residue. That is, it was found that substantially all chlorine contained in the waste was contained in the pyrolysis gas and was discharged to the pyrolysis gas outlet line.

[0006] Based on such knowledge, the incinerator side supplies waste to a space having a temperature of 300 ° C or higher to cause a pyrolysis reaction, and generates a pyrolysis gas generated by the reaction, undecomposed residues and A first fluidized bed (hereinafter referred to as a pyrolysis means) for separating a char mixture composed of a fluidized medium and an incombustible substance from each other, and a method for completely burning the undecomposed residue while blowing the char mixture upward by air or combustion exhaust gas. 2 fluidized beds (hereinafter referred to as char combustion means), while the first and second boilers are connected in series on the boiler side, and the heat of the pyrolysis gas is utilized in the lower stage boiler. About 400 ° C or less, specifically 30
Hot water or steam at about 0 ° C. is produced (hereinafter referred to as first steam producing means), and then the hot water or steam at about 300 ° C. is introduced into a second boiler to obtain combustion gas obtained from the char burning means. Has been proposed to produce superheated steam of about 500 ° C. or higher by the heat of the superheated steam (hereinafter referred to as second steam production means).

The present invention further develops such prior art and relates to the production of superheated steam capable of efficiently (in large quantities) producing high-temperature, high-pressure superheated steam while preventing high-temperature corrosion of the boiler tube due to chlorine. It is to provide an invention. Another object of the present invention is to provide an invention relating to the production of superheated steam capable of reducing chlorine more efficiently and obtaining high-temperature superheated steam as compared with the prior art.

[0008]

According to the first aspect of the present invention,
Pyrolysis that supplies waste to a space having a temperature of 300 ° C. or higher to cause a pyrolysis reaction, and separates a pyrolysis gas generated by the reaction, a non-decomposed residue, a char mixture composed of a fluidized medium, and a non-combustible material from each other. Means for completely burning the undecomposed residue while blowing the char mixture upward with air or flue gas; and burning the pyrolyzed gas with air or oxygen-enriched air at a temperature of 1
Ash melting means for generating a high temperature of 300 ° C. or more and introducing ash derived from the waste powder into the high temperature portion to melt the ash and decompose it into a combustion gas; A pyrolysis gas complete combustion means to be burned, a first steam production means for producing hot water or steam of about 400 ° C. or less by heat of the combustion gas obtained by the pyrolysis gas complete combustion means, A second steam producing means is provided, in which the hot water or the steam produced by the first steam producing means is superheated by the heat of the obtained combustion gas.

According to a second aspect of the present invention , a portion of the pyrolysis gas obtained by the pyrolysis means is branched and supplied to the inlet side of the pyrolysis means. .

According to this invention, in any of the above-mentioned claims, since the char mixture separated by the pyrolysis means contains substantially no chlorine, it is used as a superheat source of the second steam production means. Even if it is configured to obtain superheated steam of not less than ° C, high-temperature corrosion of equipment does not occur.

In addition, a pyrolysis gas containing chlorine is used as a heating source of the first steam producing means.
Since it is intended to manufacture hot water or steam at a temperature of 0 ° C. or less, specifically, about 300 to 350 ° C. or less, only a temperature lower than a high temperature corrosion temperature is heated. Absent.

Further, according to the first aspect of the present invention, in order to carry out the melting and separation of the ash, the ash or the like is not mixed into the pyrolysis gas introduced into the first steam producing means for a long period of time. And stable steam production becomes possible.

According to the second aspect of the present invention, a part of the pyrolysis gas obtained by the pyrolysis means is branched and supplied to the inlet side of the pyrolysis means.
Since a high temperature flammable gas of 0 ° C. to 400 ° C. can be circulated and supplied to the pyrolysis means, the pyrolysis gas is air or an inert gas such as N ₂ , CO ₂ , H ₂ O in combustion exhaust gas. Can be minimized, the heat generation per unit volume can be increased, and the combustion temperature required for ash melting can be easily increased to 1300 ° C.

In the third aspect of the present invention, the first
Alternatively, the steam heated by the second steam manufacturing means or a portion of the hot water or steam introduced into any of the manufacturing means may be appropriately introduced into the heat exchange means arranged on the high temperature side of the combustion means. It is a feature. That is, since the combustion means decomposes the undecomposed residue while blowing the char mixture upward by air or combustion exhaust gas, the combustion gas contains a high-temperature fluid medium.

Therefore, in the present invention, a heat exchange means is provided on the high temperature side of the char combustion means by utilizing the high temperature fluid medium, and is heated by the first or second steam production means. By performing heat exchange with the heated steam or a part of the hot water or the steam introduced into any of the above-mentioned production means, the following operation can be performed. That is, the first
By introducing warm water introduced into the steam producing means into the heat exchanging means so as to raise the temperature to some extent, the heat exchanging means
The temperature can be raised in three stages substantially in series with the first steam production means and the second steam production means, and a large amount of sufficiently heated superheated steam can be obtained.

Further, by introducing hot water or steam introduced into the second steam producing means together with the first steam producing means into the heat exchanging means in parallel, the heating amount of the second steam producing means is increased. And a large amount of superheated steam can be obtained. Furthermore, since the high temperature side of the char combustion means is heated to about 950 to 1300 ° C., the superheated steam after heating by the second steam production means is introduced into the heat exchange means, so that it is further heated. For example, 5
It is also possible to obtain a superheated steam of 00 to 600 ° C, and it is possible to obtain a sufficiently heated superheated steam.

Further, the provision of the heat exchange means on the high temperature side of the char combustion means is unnecessarily high at around 950 to 1300 ° C., and if it is passed through the outlet line as it is, the ordinary refractory material has no temperature. However, by dropping the temperature to 800 to 950 ° C., a normal refractory material can be used. Even if the temperature is lowered to 800 to 950 ° C. as described above, there is no problem in maintaining the steam temperature in the second steam producing means at 500 to 600 ° C.

According to a fourth aspect of the present invention, there is provided a separator connected to the outlet side of the combustion means for separating the combustion gas and the fluid medium from the combustion means. The heated steam or a part of the hot water or steam introduced into any one of the production means is appropriately introduced to the fluid medium outlet side of the separation means, and heated by thermal contact with the fluid medium. Is what you do.

According to this invention, since the separation means for separating the combustion gas and the fluid medium is provided at the outlet side of the char combustion means, in other words, the high temperature fluid medium of about 800 to 950 ° C. is heated. By returning to the decomposition means and the char combustion means, it becomes easy to form a fluidized bed at a desired temperature and to control the temperature.

In the present invention, a heat exchange means is arranged on the fluid medium outlet side of the separation means, and is introduced into the steam heated by the first or second steam production means or any of the production means. By heating a portion of the hot water or steam by appropriate thermal contact with the fluidized medium, the same effect as in the first aspect of the invention can be achieved.

In this case, heat exchange means (hereinafter referred to as first heat exchange means) is provided on the high-temperature side of the char combustion means, and heat exchange means (hereinafter referred to as second heat exchange means) is also provided on the fluid medium outlet side of the separation means. May be arranged. Also, the first heat exchange means
By arranging the first steam producing means, the second steam producing means, and the second heat exchanging means, it is possible to substantially increase the temperature in four stages in series, and to obtain an extremely high sufficiently heated superheated steam. I can do it.

Further, as shown in the embodiment described later, by arranging (1 heat exchange means and first steam production means in parallel) -second steam production means-second heat exchange means in series, The temperature can be raised in three stages in parallel / series, and a large amount of sufficiently heated superheated steam can be obtained. Also the first
Either the heat exchange means or the second heat exchange means may be selectively used. It is preferable to use a superheater or a boiler as the heat exchange means.

[0023]

Embodiments of the present invention will be described below with reference to the drawings. However, the dimensions, materials, shapes, relative arrangements, and the like of the components described in this embodiment are not intended to limit the scope of the present invention unless otherwise specified, and are merely illustrative examples. It's just FIG.
1 shows a superheated steam production apparatus utilizing the heat of incineration of waste according to an embodiment of the present invention. Fluid medium and waste such as municipal solid waste are supplied from a waste supply line 4 and a sand circulation line 5, and the temperature is controlled by air or flue gas supplied from air or flue gas inlet line 6. A fluidized bed space of 300 ° C. or higher is generated to cause a pyrolysis reaction of the waste, and the pyrolysis gas generated by the reaction is supplied to a pyrolysis gas outlet line 7. From the char mixture take-out line 9, incombustibles are separately taken out from the incombustibles take-out line 8.

The air or flue gas inlet line 6
The air or combustion exhaust gas supplied to the pyrolysis furnace 1 is
In order to perform the thermal decomposition efficiently in the range of 300 to 700 ° C, the oxygen content is low (about 3 to 5%) and the temperature is 100 to
It is preferable to use the combustion exhaust gas maintaining the temperature of 300 ° C., specifically, the combustion exhaust gas extracted from the outlet line 25 of the first boiler 24. The pyrolysis gas taken out from the pyrolysis gas outlet line 7 is introduced into the first boiler 24 through the ash melting furnace 31 and the pyrolysis gas combustion furnace 34.

That is, the ash melting furnace 31 swirls and separates the sand-mixed pyrolysis gas ash by swirling flow.
1, air or oxygen-enriched air is introduced together with the pyrolysis gas to form a high temperature of 1300 ° C. or more by the heat of combustion of the pyrolysis gas, the ash is melted by the heat, and the melted ash is melted. The slag is dropped into the water reservoir 32A through the ash outlet line 32 to generate a water-cooled slag of about several mm, and the slag is used as an aggregate for construction.

The pyrolysis gas from which the ash has been removed is introduced into the pyrolysis gas combustion furnace through an outlet line 33, and is completely burned by air supplied from an air supply line. To the first boiler 24.

Reference numeral 10 denotes a char combustion furnace consisting of a tower type fluidized bed furnace. The char mixture supplied from the char mixture take-out line 9 on the dispersion plate 11 disposed at the bottom and the fluidized sand circulated from the sand circulation line 19 Is stored. Further, air is further supplied from the air supply line 12 below the dispersion plate 11 from the air supply line 13 in the middle region of the char combustion furnace 10, and the undecomposed residue is burned.
A water-cooled wall boiler 36 or a super heater for generating a combustion gas of about 0 ° C. and introducing boiler water from a branch line 26 ′ in an upper region of the char combustion furnace 10 is provided.
Unnecessarily high combustion gas of about 50 to 1300 ° C
The temperature is lowered to 00 to 950 ° C., and a part of the boiler water supplied to the first boiler 24 is heated. The heating temperature of the boiler water is about 300 ° C.

As described above, the combustion gas temperature is set to 800 to 9
Even if the temperature is lowered to 50 ° C., there is no problem in maintaining the steam temperature in the second boiler 20 at 500 to 600 ° C. Small incombustibles that are not burned in the combustion furnace 10 are taken out from an incombustibles take-out line 14.

Then, the combustion gas of the sand mixture heated to a high temperature as described above is supplied to
It is introduced into a solid separation device such as a cyclone 16 where fluidized sand and combustion gas are separated, and the combustion gas is supplied to a gas outlet line 1.
7 to the second boiler 20. The fluidized sand is taken out from a sand outlet line 18 and supplied to a combustion furnace 10 from a sand circulation line 19 and to the pyrolysis furnace 1 from a sand circulation line 5, respectively.

Reference numeral 20 denotes a second boiler and reference numeral 24 denotes a first boiler. In the first boiler 24, the pyrolysis gas taken out from the pyrolysis gas outlet line 7 is reburned by the air taken in from the air inlet line 21. The boiler water introduced into the first boiler 24 together with the combustion exhaust gas discharged from the second boiler gas outlet and taken in from the boiler water inlet 26 is heated to 300 ° C.
The steam is heated back and forth, and steam is supplied to the second boiler 20 from the first boiler steam outlet 27.

In the second boiler 20, the steam extracted from the first boiler steam outlet line 27 of the first boiler 24 and the branch steam line 27 'heated by the water-cooled wall boiler 36 are used.
Through the combustion gas supplied through the combustion gas line 17,
A superheated steam of about 600 ° C. is produced and taken out from the second boiler steam outlet 28.

Next, the operation of the above embodiment will be described in detail.
Chlorine-containing organic compounds such as PVC plastics are mixed in the waste such as municipal waste supplied to the pyrolysis furnace 1, and the combustibles contain about 0.2 to 0.5% as C1. . Then, municipal solid waste from the waste supply line 4 and high-temperature circulating sand from the sand circulation line 5 are supplied to the pyrolysis furnace 1, respectively, and air or combustion exhaust gas is supplied from the lower air or combustion exhaust gas inlet line 6 to flow. By treating at a temperature of 300 to 700 ° C. in the fluidized bed in which the sand 2 is fluidized, an undecomposed residue substantially free of chlorine is obtained from the char mixture removal line 9. That is, substantially all of the chlorine contained in the waste is contained in the pyrolysis gas and discharged to the pyrolysis gas outlet line 7. The large-sized incombustibles separated by the thermal decomposition reaction in the thermal decomposition furnace 1 are taken out of the furnace through an incombustibles take-out line 8.

The pyrolysis gas extracted from the pyrolysis outlet line 7 of the pyrolysis furnace 1 by the pyrolysis furnace 1 contains low calorie gas, oil, tar and HC1, which are converted into an ash melting furnace. After complete combustion in the first boiler gas inlet 23 and the first boiler 2 together with the combustion exhaust gas from the second boiler gas outlet line 22
4

Accordingly, it is possible to stably produce steam over a long period of time without incorporation of ash or the like into the combustion gas of the pyrolysis gas introduced into the first boiler 24. The temperature of the pyrolysis gas introduced into the
Since the temperature can be set as high as about 900 ° C. (about 950 ° C. at the maximum), a large amount of steam at about 300 ° C. produced by the boiler can be produced.

The gas at the first boiler gas inlet 23 is HC1
Is contained at about 500 to 1000 ppm, so that the flow rate of the boiler water is adjusted to keep the tube surface temperature of the first boiler 24 at about 350 ° C. or less, which is the same as the conventional one, thereby suppressing high-temperature corrosion. For this reason, high-temperature superheated steam cannot be obtained in the first boiler 24, but can be heated up to about 300 ° C., and if this is further heated in the second boiler 20, about 500 to 600 ° C.
High temperature superheated steam can be obtained.

In the pyrolysis furnace 1, the char mixture consisting of the char mixture sand taken out from the char mixture take-out line 9 and the undecomposed residue and containing substantially no chlorine is dispersed in the combustion furnace 10 from the air supply line 12 through a dispersion plate. Combustion by air supplied via 11. In this case, the amount of air supplied from the air supply line 12 is adjusted, and the non-decomposed residue is burned while blowing the fluidized sand upward. Further air may be supplied from the air supply line 13 for complete combustion. The temperature of the combustion furnace 10 rises due to a combustion exothermic reaction. This temperature value is determined by the calorific value of the undecomposed residue supplied from the char mixture take-out line 9, the amount of air in the air supply lines 12, 13 and the amount of fluidized sand in the sand circulation line 19 and the temperature. May become hot. Therefore, it is easy to make the mixed sand combustion gas 800 to 950 ° C. by exchanging heat with the boiler water introduced from the branch pipe 26 by the water-cooled wall boiler 36. Miniaturized incombustibles such as glass and cans are extracted from the incombustibles take-out line 14.

Exhaust gas generated in the combustion furnace 10 at a high temperature of 800 to 950 ° C. and containing substantially no chlorine passes through the sand / combustion gas outlet line 15 together with the fluidized sand, and the cyclone 1
The fluidized sand is taken out from the sand outlet line 18 and the exhaust gas is taken out from the gas outlet line 17 separately. And 800-taken out from the sand exit line 18
Part of the 950 ° C. high-temperature fluidized sand is returned to the pyrolysis furnace 1 through the sand circulation line 5 and is used to maintain the temperature inside the pyrolysis furnace 1 at a predetermined temperature. The remainder is returned to the combustion furnace 10 via the sand circulation line 19.

On the other hand, the high temperature exhaust gas of 800 to 950 ° C. taken out from the gas outlet line 17 of the cyclone 16 is introduced into the second boiler 20 by the second
It is used to further heat the steam produced by the boiler 24 to produce superheated steam. Since the exhaust gas passing through the gas outlet line 17 does not substantially contain chlorine, even if the surface temperature of the boiler tube of the second boiler 20 is set to 350 ° C. or higher, high-temperature corrosion is greatly reduced. Therefore, the steam temperature in the tube is set to about 500 to 600 ° C. and 100 kgf / cm.
^2, and a high-temperature superheated steam can be stably obtained from the second boiler steam outlet 28.

In order to maintain the temperature of the pyrolysis furnace 1 at a predetermined temperature of 300 ° C. or higher in the pyrolysis furnace 1, the amount of oxygen in the air or the flowing gas supplied from the combustion exhaust gas inlet line 6 is adjusted. It is preferable to adjust the flow rate of exhaust gas from one boiler 24 or to supply a part of the fluidized sand having a high temperature of about 800 to 950 ° C. taken out from the sand outlet line 18 from the cyclone 16 from the sand circulation line 5 as a heat source. .
For that purpose, in the combustion furnace 10, the unloaded residue is blown off the fluidized sand supplied from the char mixture take-out line 9 by setting the gas emptying speed (gas flow rate in the furnace / cross-sectional area of the furnace) to 3 to 6 m / s. And the fluid sand is cyclone 16
A high-speed circulating fluidized bed that is separated from the combustion gas and supplied to the pyrolysis furnace 1 and the combustion furnace 10 by circulation is suitable. In order to carry out the present invention more efficiently, the amount of the substantially chlorine-free char mixture taken out from the char mixture take-out line 9 is made as large as possible, preferably 40% or more of the combustible material in the raw material, and the combustion furnace 10 Increase the amount of heat generated by
It is desirable to increase the amount of heat recovered in the second boiler 20. As a result, a power generation efficiency of about 30% or more (about twice as much as the conventional one) can be obtained. Therefore, in this embodiment, chlorine in the garbage is substantially separated and removed, and the char recovery rate is 50%.
As a condition that can be achieved as described above, the temperature of the pyrolysis furnace 1 is set to 300 to
700 ° C., preferably 350 to 450 ° C.

Now, the sand exit line 1 from the cyclone 16
Since the fluidized sand taken out of 8 has a high temperature of about 800 to 950 ° C., if it is supplied to the pyrolysis furnace 1 from the sand circulation line 5 as it is, the temperature of the pyrolysis furnace 1 becomes 350 to
It may be difficult to maintain the temperature at 450 ° C. In such a case, as shown in FIG. 2, a superheater or other heat exchange means is arranged on the sand outlet line 18 side of the cyclone 16 and heat exchange is performed by superheated steam heated by the second boiler 20. The temperature of the fluidized sand can be reduced to around 500 to 800 ° C., and the shortage of the amount of heating of the second boiler 20 can be compensated.

In particular, the second boiler 20 is apt to suffer from heat shortage due to the introduction of the steam from the water-cooled wall boiler 36 together with the first boiler 24, but this embodiment can smoothly solve this problem.

FIG. 3 shows another embodiment of the present invention, in which a part of the pyrolysis gas obtained by the pyrolysis furnace is partially converted into an ash melting furnace 31.
In other words, the high-temperature combustible gas of 350 ° C. to 400 ° C. is supplied to the pyrolysis furnace 1 on the upstream side of the pyrolysis furnace through the branch line 7a to the inlet side below the dispersion plate 3 of the pyrolysis furnace.
The amount of heat generated per unit volume can be minimized by minimizing dilution of the pyrolysis gas with air or inert gas such as N ₂ , CO ₂ , H ₂ O, etc. in the combustion exhaust gas. And the combustion temperature required for melting the ash can be easily increased to 1300 ° C., and the temperature fluctuation can be suppressed to achieve stable thermal decomposition.

[0043]

As described above, according to the present invention, it is possible to prevent high temperature corrosion of a boiler tube by chlorine while preventing high temperature corrosion.
High-pressure superheated steam can be obtained efficiently. Further, according to the present invention, heat distribution and heat absorption can be performed more efficiently than in the prior application, and moreover, pyrolysis and char combustion can be performed more efficiently, and high-temperature superheated steam can be obtained. And so on.

[Brief description of the drawings]

FIG. 1 is a system diagram showing an apparatus for producing a superheated steam using incineration heat of waste according to an embodiment corresponding to the first and third aspects of the present invention.

FIG. 2 is a system diagram showing an apparatus for producing superheated steam using incineration heat of waste according to an embodiment corresponding to the fourth aspect of the present invention.

FIG. 3 is a system diagram showing an apparatus for producing superheated steam using the heat of incineration of waste according to an embodiment corresponding to the second aspect of the present invention.

[Explanation of symbols]

DESCRIPTION OF SYMBOLS 1 Pyrolysis furnace (pyrolysis means) 2 Fluid medium, such as sand 7a Branch line 10 Combustion furnace (char combustion means) 11 Dispersion plate 16 Cyclone (separation means) 20 2nd boiler (2nd steam production means) 24 1st boiler (First steam production means) 31 Ash melting furnace 34 Pyrolysis gas combustion furnace 36 Water-cooled wall boiler (Heat exchange means arranged on the high temperature side of char combustion means) 129 Super heater (Flow of the separation means) Heat exchange means on the medium outlet side)

──────────────────────────────────────────────────の Continued on the front page (51) Int.Cl. ⁷ Identification code FI F23G 5/00 115 F23G 5/16 ZABE ZAB 5/30 ZABK 5/16 ZAB 5/32 ZAB 5/30 ZAB 5/46 ZABA 5 / 32 ZAB ZABB 5/46 ZAB 7/00 103A ZAB 7/00 103 F23J 1/00 ZABB ZAB F23C 11/02 ZAB F23J 1/00 ZAB 312 (72) Inventor Hirotoshi Horizoe Hirotoshi Kanazawa-ku, Kanazawa-ku, Yokohama-shi 1-8 Address 1 Yokohama Research Institute, Mitsubishi Heavy Industries, Ltd. (72) Susumu Nishikawa, Inventor 1-8-1, Koura, Kanazawa-ku, Yokohama-shi Yokohama Research Institute (72) Inventor Katsuhiko Kobayashi 1-8-1, Koura, Kanazawa-ku, Yokohama-shi Mitsubishi Heavy Industries, Ltd.Yokohama Research Laboratory (72) Inventor Yoshimasa Kawami 12 Nishikicho, Naka-ku, Yokohama-shi Mitsubishi Heavy Industries Inside Yokohama Works Co., Ltd. (72) Masaharu Kira 12, Nishikicho, Naka-ku, Yokohama-shi Inside Mitsubishi Heavy Industries, Ltd. Yokohama Works Co., Ltd. (56) References JP-A-5-346204 (JP, A) JP-A-58-95104 (JP) JP-A-52-117302 (JP, A) JP-A-1-252806 (JP, A) JP-A-7-35322 (JP, A) JP-A-5-141636 (JP, A) (58) Field surveyed (Int.Cl. ⁷ , DB name) F23G 5/027 F22B 1/18 F22G 1/16 F23C 10/00 F23C 10/20 F23G 5/00 115 F23G 5/16 F23G 5/30 F23G 5/32 F23G 5/46 ZAB F23G 7/00 103 F23J 1/00 ZAB

Claims (4)

(57) [Claims] 1. A waste material is supplied into a space having a temperature of 300 ° C. or more to cause a pyrolysis reaction, and a pyrolysis gas generated by the reaction, a char mixture composed of an undecomposed residue and a fluid medium, and an incombustible material are separated. A pyrolyzing means for separating each other, a burning means for completely burning the undecomposed residue while blowing the char mixture upward by air or flue gas, and burning the pyrolyzed gas with air or oxygen-enriched air at a temperature of 1300. Ash melting means for generating a high temperature of at least ℃ and introducing the ash derived from the waste powder into the high temperature portion to melt the ash and decompose it into a combustion gas; and supplying air to the combustion gas to complete combustion. A first steam for producing hot water or steam having a temperature of about 400 ° C. or less by using the heat of the combustion gas obtained by the complete pyrolysis gas combustion means; Disposal means for producing hot water or steam produced by the first steam producing means by means of heat of the combustion gas obtained by the combustion means and superheated steam. Superheated steam production equipment that uses the heat of incineration of materials. 2. A pre-Symbol claim 1, wherein the branched part of the pyrolysis gas obtained by thermal decomposition means utilizing incineration heat of waste and supplying the inlet side of the thermal decomposition section Superheated steam production equipment. 3. A method in which steam heated by the first or second steam producing means or a portion of hot water or steam introduced into any of the producing means is disposed on a high temperature side of the combustion means. exchange means superheated steam producing device using the incineration heat of claim 1 Symbol placement of waste, characterized in that said introducing appropriate. 4. A separating means connected to an outlet side of said combustion means for separating combustion gas and said fluid medium from said combustion means, wherein said steam heated by said first or second steam producing means or a portion of the hot water or steam is introduced into any of the production means, and introduced into the fluidized medium outlet side of suitable separating means, according to claim 1 Symbol mounting, characterized in that heated by thermal contact with the flowable medium Superheated steam production equipment using the heat of incineration of waste.