JP4756556B2 - Sludge carbonization equipment - Google Patents

Description

  The present invention relates to a sludge carbonization facility for carbonizing organic matter-containing sludge.

Wastewater containing organic matter discharged from homes and the like is generally treated by an activated sludge method or the like in a sewage treatment facility.
Sewage sludge containing excess organic matter is generated along with this wastewater treatment, but the amount of generated sewage sludge increases year by year as the amount of wastewater treatment increases, and disposal of such wastewater is a major problem.
When disposing of sewage sludge, the sewage sludge contains a large amount of water and cannot be disposed as it is, where it is concentrated and dehydrated for reduction, or incinerated or melted. Various treatments are currently being performed.

However, if sewage sludge is incinerated or melted, a large amount of energy is consumed, resulting in high processing costs.
Therefore, as one method of treating sewage sludge with low energy consumption, it has been proposed to carbonize sewage sludge by dry distillation treatment.
In this carbonization treatment, since the sewage sludge contains about 45% by mass of carbon in the substrate, the carbon in the sludge is not consumed like incineration and melting treatment, but the sludge is oxygen-free or low. By pyrolysis (carbonization) in an oxygen state, the carbon content remains, and is produced as a carbide (carbonized product) having a new composition.

Conventionally, this carbonization treatment agglomerates surplus sewage sludge generated in a sewage treatment facility by adding a polymer flocculant, etc., and then dehydrating it with a dehydrator to obtain a moisture content of about 75 to 85% (usually Is about 80%) dewatered sludge.
Thereafter, this dewatered sludge is put into the dryer, where it is dried to a moisture content of about 25 to 45% (usually about 40%).
In this drying treatment, the sludge is dried and granulated into a suitable particle size suitable for the subsequent carbonization treatment, for example, a dumpling-like particle having a size of about 10 mm.
The dried sludge thus obtained is put into a carbonization furnace, and this is subjected to dry distillation treatment in the carbonization furnace to obtain sludge as a carbonized product, which is discharged from the carbonization furnace.

FIG. 3 shows a specific configuration of a conventional carbonization treatment facility for performing this carbonization treatment.
In the figure, reference numeral 200 denotes a hot air generating furnace in which hot air serving as a heat source for drying the dewatered sludge is generated.
Reference numeral 201 denotes a receiving hopper, and dewatered sludge dehydrated to a moisture content of about 80% is first received by the receiving hopper 200.
The dewatered sludge accepted here is sent to a dryer 206 which also serves as a granulator by a quantitative supply device 204 and a transfer device 205 via a relay hopper 202, where a predetermined moisture content, specifically 40%, is sent. It is dried to a moisture content of about a degree and granulated into dumpling-like grains having a particle size of about 10 mm.

The dryer 206 has a stirring shaft 210 inside a rotary drum 208 as shown in FIG. Here, the stirring shaft 210 is provided at a position eccentric from the center of the rotary drum 208.
A plurality of stirring blades 212 extend radially from the stirring shaft 210.
On the other hand, a plurality of plate-like lifters 214 are provided on the inner peripheral surface of the rotating drum 208 at a predetermined interval in the circumferential direction so as to rotate integrally with the rotating drum 208.
As a result, the sludge (dehydrated sludge) inside the rotary drum 208 is lifted upward from the bottom by the lifter 214 as the rotary drum 208 rotates, and falls by its own weight near the top.
The sludge that has fallen is finely crushed by the high-speed rotation of the stirring blade 212 located on the lower side, and falls to the bottom side of the rotary drum 208.

The sludge inside the rotary drum 208 is subjected to such a stirring action and is exposed to the hot air introduced into the dryer 206 from the hot air generating furnace 200 in FIG. 3 to be dried, and the moisture gradually decreases.
The sludge is gradually sent in the axial direction while being granulated into an appropriate particle size inside the rotary drum 208 by the inclination gradient of the rotary drum 208 and further by the crushing by the stirring blade 212 and the scattering action at that time.
The dried sludge that has been dried and granulated by the dryer 206 in this way is then transported to the carbonization furnace 222 via the relay hopper 218 by the transport devices 216 and 220, where it has an appropriate particle size of about 10 mm. The granulated dried sludge having a moisture content of about 40% is carbonized by dry distillation.

  This carbonization furnace 222 is of the external heating type rotary kiln type, and this carbonization furnace 222 is provided with a cylindrical retort 226 as a dry distillation vessel inside the furnace body 224 as shown in FIG. The dried sludge that has been dried and granulated by the preceding dryer 206 is put into the retort 226 by a screw feeder (not shown).

The input dried sludge is first heated by the atmospheric heating inside the external heat chamber 230 by the auxiliary combustion burner (external heat chamber burner) 228 disposed inside the furnace body 224.
Then, the combustible gas contained in the dried sludge escapes into the atmosphere of the external heat chamber 230 through the blow pipe 232 provided in the retort 226, and after this combustible gas is ignited, the retort is caused by the combustion of the combustible gas. The sludge inside 226 is heated.
At this stage, the auxiliary burner 228 is stopped from burning.

As shown in FIG. 5, an exhaust gas treatment chamber 234 separated from the external heat chamber 230 is provided in the furnace body 224, and the exhaust gas from the external heat chamber 230 is guided here.
The exhaust gas treatment chamber 234 is provided with an exhaust gas treatment chamber burner 236, and unburned gas in the exhaust gas introduced into the exhaust gas treatment chamber 234 is subjected to secondary combustion in the exhaust gas treatment chamber burner 236. .

The sludge inside the retort 226 moves from the left end in the figure to the right in the figure along with the rotation of the retort 226 (the retort 226 has a slight gradient), and finally the carbonization residue (carbonized product) is retort. 226 is discharged from the right end outlet 238, that is, the carbonization furnace 222.
On the other hand, the exhaust gas discharged from the carbonization furnace 222 is discharged from the chimney to the atmosphere through a heat exchanger as shown in FIG.
This kind of sludge carbonization equipment is disclosed in, for example, Patent Document 1 and Patent Document 2 below.

  However, in the case of the conventional sludge carbonization treatment facility shown in FIG. 3, it is necessary to install a hot air generating furnace 200 for generating hot air for drying in the dryer 206, and the cost for the installation is low. In addition, the installation of the hot air generating furnace 200 inevitably increases the size of the equipment, and the generation of hot air in the hot air generating furnace 200 increases the running cost of the equipment.

  Further, the dryer 206 is a unit in which the entire amount of high water content sludge having a water content of about 80% is fed into the desiccant sludge, and this drier 206 is a dumpling-like particle having a size of about 10 mm. It also serves as a granulator for granulating, and combined with the small contact area between the dewatered sludge and hot air, it takes a long time (about 30 minutes) to dry. There is a problem of consuming a lot of energy, and this also increases the running cost of the equipment.

  In addition, the dryer 206 has a problem that the equipment cost increases due to a large and complicated structure having a rotating drum 208 and its driving device, a stirring blade 212 and its driving device, a lifter 214 and the like. There has been a problem that it is difficult to control the moisture content of the dried sludge discharged from 206 to a moisture content of about 40% suitable for carbonization in the subsequent carbonization furnace 222.

On the other hand, Patent Document 3 below discloses that the exhaust gas from the carbonization furnace 222 is guided to the dryer 206 and used as a heat source for drying in the dryer 206 instead of installing the hot air generator 200. .
According to the device disclosed in Patent Document 3, the installation of the hot air generating furnace 200 can be made unnecessary, and thus the equipment cost required for the hot air generating furnace 200 can be reduced. In addition, the running cost due to the generation of hot air in the hot air generation furnace 200 can be reduced.

  However, in the one disclosed in Patent Document 3, the above-described dryer 206 is used for drying the dewatered sludge. Therefore, the above problem caused by drying by the dryer 206, that is, a long time is required for drying. In the meantime, a large amount of heat energy is consumed, and the dryer 206 is large in size and complicated in structure, so that the equipment cost required for the dryer 206 is high. Further, when the dewatered sludge is dried by the dryer 206, the dry sludge is dried. The problem remains that it is difficult to control the water content of this material to a water content that is necessary and appropriate for carbonization in the carbonization furnace in the subsequent step.

JP-A-11-37644 Japanese Patent Laid-Open No. 11-33599 JP 11-37645 A

  With the background of such circumstances, the present invention can reduce the overall equipment including the dryer and reduce the equipment cost, increase the drying efficiency for the dewatered sludge and reduce the thermal energy required for drying, Another object of the present invention is to provide a sludge carbonization treatment facility capable of easily controlling the dry sludge to a desired appropriate moisture content.

  Thus, according to the first aspect, the dewatered sludge after the organic substance-containing sludge is dehydrated is dried by passing through a dryer, and the dried sludge is carbonized by passing through a carbonization furnace to carbonize the sludge as a carbonized product. In the treatment facility, the exhaust gas from the carbonization furnace is used as a heat source for drying, and the exhaust gas is supplied as hot air to the dryer, and as the dryer, the dehydrated sludge is dried on a part of the dehydrated sludge. Crush the mixture to which the powder is added, blow the hot air on the crushed material, transport the crushed material with the air current of the hot air and dry it to form the dry powder, and use an airflow dryer that discharges with the air current, (B) a first mixing means for mixing a part of the dewatered sludge and the dry powder to produce the mixture for supply to the dryer; and (b) the drying discharged from the dryer. A separator for separating powder from the air stream; A distribution means for dividing a part of the dry powder from the separator for supply to the dryer and a remaining part for supply to the carbonization furnace; and (d) for supply to the carbonization furnace. And a second mixing means for adding the remaining part of the dewatered sludge to the remaining part of the dried powder divided into the mixture and mixing it with the dried sludge for supply to the carbonization furnace, The dried sludge mixed by the two mixing means is carbonized by passing through the carbonization furnace.

  According to a second aspect of the present invention, in the first aspect, the separator is a cyclone separator.

Effects and effects of the invention

  As described above, the present invention supplies hot air of exhaust gas from the carbonization furnace to a dryer as a heat source for drying, and adds dry powder of dehydrated sludge generated in advance to a part of the dehydrated sludge as the dryer. The mixture is crushed, blown with hot air of exhaust gas from the carbonization furnace to the crushed material, transported crushed material with hot air current and dried to form dry powder, using an airflow dryer that discharges it with air current It was made like that.

  In this invention, further, the first mixing means for mixing the dried powder with a part of the dehydrated sludge to produce a mixture for supply to the dryer, and a separator for separating the dried powder from the dryer from the air stream; Distribution means for distributing a part of the dry powder from the separator for supply to the dryer and a part of the dry powder for supply to the carbonization furnace, and a remaining part of the dry powder for supply to the carbonization furnace. And a second mixing means for adding and mixing the remaining part of the dewatered sludge to the section to form dry sludge for supply to the carbonization furnace.

In short, in the sludge carbonization facility of the present invention, the entire amount of dehydrated sludge is not charged into the dryer, but a portion of the dehydrated sludge is charged into the dryer as a mixture together with the dry powder of dehydrated sludge that has been generated in advance.
Here, the moisture content of the dewatered sludge is about 80% as described above. On the other hand, the dry powder has a moisture content of about 10% to 20% (usually about 15% or less).

Therefore, the mixture put into the dryer has a lower water content than dehydrated sludge.
The mixing ratio of the dewatered sludge and the dry powder at this time is adjusted so that the water content of the mixture becomes a water content suitable for drying with a dryer.

The airflow dryer used in the present invention breaks the mixture, blows hot air (exhaust gas) from the carbonization furnace to the crushed material, and conveys the airflow. To discharge.
The time required for drying is in seconds, and it is possible to dry the mixture in a very short period of time.

The dried powder discharged from the dryer is separated from the airflow flowing out by the separator, and a part of it is divided again for supply to the dryer, and a part of the dehydrated sludge newly sent to the dryer. Are mixed together and re-supplied to the dryer.
That is, in this invention, the dried powder of the dewatered sludge can be circulated through the circulation path passing through the dryer and the separator. This circulation movement has the meaning of adjusting the moisture content so that the moisture content of the dewatered sludge charged into the dryer as described above becomes a moisture content suitable for drying.

The remaining part of the dry powder from the separator is supplied to the carbonization furnace for the original carbonization treatment.
However, if the dewatered sludge is supplied as a dry powder to the carbonization furnace, the carbonization process in the carbonization furnace cannot be performed satisfactorily.
Therefore, in the present invention, by mixing the remaining part of the dewatered sludge with the dry powder supplied to the carbonization furnace, the moisture content is adjusted to about 40% suitable for carbonization in the carbonization furnace, and The dried sludge is made into dumpling-like particles having a size of about 10 mm, which is suitable for treatment in a carbonization furnace.

That is, the moisture content and particle size of the dried sludge are adjusted to substantially the same properties as the dried sludge supplied from the conventional dryer to the carbonization furnace.
Then, this is passed through a carbonization furnace, where it is carbonized, and finally a carbonized product is obtained.

In the present invention, drying with a dryer can be performed within a very short time.
This effect prevents the dryer from having the function of a granulator that granulates into a particle size suitable for processing in a carbonization furnace, and has only a function for drying. Accordingly, in the dryer, the mixture having a lower water content than the dewatered sludge is finely crushed and dried until it becomes a fine dry powder by spraying with hot air and transporting air with hot air.

  Therefore, in the present invention, drying by a dryer can be performed with high efficiency in an extremely short time compared to the conventional case, and the required heat energy in the dryer is greatly increased in addition to using exhaust gas from the carbonization furnace as a heat source. Can save you money.

On the other hand, in the present invention, what was made into dry powder in this way was then mixed again with dewatered sludge, and it was made into dry sludge with an appropriate moisture content and appropriate size for supply to the carbonization furnace, Supply to carbonization furnace.
Therefore, although the dehydrated sludge is once dried powder, it can be carbonized well in the subsequent carbonization step.

In the present invention, the cost for the installation can be reduced by omitting the hot air generating furnace, and the entire equipment can be downsized by omitting the installation of the hot air generating furnace.
In addition, the required heat energy for drying in the dryer can be reduced, and the running cost can be increased compared to the conventional case.

  In addition, the dryer used in the present invention has a simple structure and can be reduced in size, and this also makes it possible to reduce the size and cost of the entire facility.

  Furthermore, in the present invention, when dry powder and dewatered sludge are mixed to form dry sludge for supply to the carbonization furnace, the moisture content of the dry sludge can be easily adjusted to an appropriate water content by simply changing the mixing ratio. Can be adjusted to the rate.

  In the present invention, a cyclone separator can be used as the separator (claim 2). In this case, the dry powder can be easily and efficiently separated and recovered from the airflow flowing out from the dryer.

Next, embodiments of the present invention will be described in detail with reference to the drawings.
In FIG. 1, reference numeral 10 denotes an externally heated rotary kiln type carbonization furnace whose structure and function are the same as those shown in FIG. 5.
That is, the carbonization furnace 10 has a cylindrical retort 14 as a dry distillation vessel inside the furnace body 12, and the water content is adjusted to about 40% inside the left end side of the retort 14 in the figure. Dry sludge is charged.
The input dried sludge is first heated by atmospheric heating inside the external heat chamber 18 by the auxiliary burner 16 disposed inside the furnace body 12.
Then, the combustible gas contained in the dried sludge escapes into the atmosphere of the external heat chamber 18 through the blow pipe 20 provided in the retort 14, and after this combustible gas is ignited, the retort is caused by the combustion of the combustible gas. The sludge inside 14 is heated.
At this stage, the auxiliary burner 16 is stopped from burning.

An exhaust gas treatment chamber 24 partitioned from the external heat chamber 18 is provided inside the furnace body 12, and exhaust gas from the external heat chamber 18 is led here.
An exhaust gas treatment chamber burner 26 is provided in the exhaust gas treatment chamber 24, and unburned gas in the exhaust gas introduced into the exhaust gas treatment chamber 24 is subjected to secondary combustion in the exhaust gas treatment chamber burner 26.

The exhaust gas in the exhaust gas treatment chamber 24 is subsequently discharged from the exhaust port 28.
In this embodiment, the exhaust gas from the carbonization furnace 10 discharged from the exhaust port 28 is supplied as a heat source (hot air) for drying to a later-described dryer 54 through the exhaust gas supply path 30.

  On the other hand, the sludge in the retort 14 moves from the left end in the figure to the right in the figure along with the rotation of the retort 14 (the retort 14 has a slight gradient), and finally a dry distillation residue (carbonized product) is formed. The retort 14 is discharged from the rightmost outlet in the drawing, that is, from the carbonization furnace 10.

Reference numeral 32 denotes a receiving hopper, and dewatered sludge dehydrated to a moisture content of about 80% is first received by the receiving hopper 200.
A part of the dewatered sludge accepted here (about 85% of the whole in this case) is sent to the mixer (first mixer) 40 through the relay hopper 34 by the quantitative supply device 36 and the transport device 38.

The mixer 40 is also supplied with dry powder obtained by previously drying dewatered sludge from a cyclone separator 72 described later.
A part of the dewatered sludge supplied to the mixer 40 and a part of the dried powder supplied from the cyclone separator 72 are mixed with each other by the mixer 40.

  The mixer 40 is composed of a paddle mixer, and a pair of rotating shafts 44 and 46 (see FIG. 2B) are provided inside the casing 42, and mixing blades 48 and 50 are radially fixed respectively. The rotating shafts 44 and 46 rotate in opposite directions to mix the dewatered sludge and the dry powder so as to knead at the overlapping portions of the mixing blades 48 and 50, and further rotate the rotating shafts 44 and 46. In contrast, the mixing blades 48 and 50 each having an inclined shape are fed in the axial direction by the feeding action, and in the process, the mixing of the dewatered sludge and the dry powder proceeds.

Here, the rotating shafts 44 and 46 rotate at unequal speed. Accordingly, there is a difference in peripheral speed between the mixing blades 48 and 50, and the dewatered sludge and the dry powder are kneaded and mixed with high efficiency based on the difference in peripheral speed.
And the mixture of the fully mixed dehydrated sludge and the dry powder is discharged from the outlet at the axial end. The discharged mixture is supplied into the dryer 54 by the feeder 52.

The dryer 54 is an air-flow dryer, and has a casing 56 that has a vertically long cylindrical shape.
A crushing portion 58 is provided inside and below the casing 56 as shown in FIG.
The crushing part 58 has a pair of rotating shafts 60 and 62 and crushing blades 64 and 66 fixed radially, respectively. By rotating these at high speed, the feeder 52 has an inside of the casing 56 of the dryer 54. The above-mentioned mixture supplied to the container, that is, the mixture of dewatered sludge and dry powder is finely crushed.

The casing 56 is also provided with a blowing port 68, and exhaust gas from the carbonization path 12 is blown into the casing 56 from the blowing port 68 as hot air (the temperature of the hot air is about 300 ° C. here).
The hot air blown in is blown vigorously against the crushed material of the mixture of dehydrated sludge and dry powder, and the crushed material is conveyed upward in the casing 56 by the upward airflow of hot air, and in the process, the dried air is dried. Is done.

The crushed particles of the mixture conveyed inside the casing 56 together with the hot air flow become dry powder at the rising end thereof, are discharged to the outside together with the air flow from the discharge port 70, and are supplied to the cyclone separator 72.
The temperature of the airflow (exhaust gas) discharged at this time is about 100 ° C. here.

In the present embodiment, the time required for drying by the dryer 54 is about 1 second.
The particle size of the dry powder is in the range of 75 to 590 μm, and the average particle size is 350 μm. However, this is the particle size after sieving, and the sieve has a minimum opening of 75 μm and a maximum of 590 μm.

This dryer 54 can transport powder particles having a size of up to 800 μm when the hot air flow rate is 20 m ³ / min (corresponding to a flow rate of 3.5 m / second at the discharge port 70 of the dryer 54) (however, Assuming that specific gravity is 1).

The cyclone separator 72 allows the dry powder to flow into the inside along with the air stream, and separates the dry powder from the air stream by centrifugal force based on rotation.
Then, the separated dry powder is dropped downward in the figure, and a part thereof is supplied to the mixer 40 again.

This dry powder has a low moisture content of about 15% or less while the moisture content of the dehydrated sludge is about 80%, and the dry powder is mixed with the dehydrated sludge. Thus, the water content of the mixture is set to a low water content suitable for drying in the dryer 54.
The water content in the mixture at this time can be easily adjusted by the mixing ratio of the dewatered sludge and the dry powder.

In this embodiment, only a part of the dry powder separated by the cyclone 72 is supplied to the dryer 54, and the remaining part is used for the carbonization treatment by the carbonization furnace 10 as a mixer (second mixer) 42. Supplied to.
That is, the dry powder from the cyclone separator 72 is distributed to the dryer 54 side and the carbonization furnace 10 side.

The distribution is performed by a distribution damper 75 provided on the dry powder supply path.
Accordingly, here, the distribution damper 75 constitutes distribution means for distributing the dry powder from the cyclone separator 72 to the dryer 54 side and the carbonization furnace 10 side.

Further, the remaining part of the dewatered sludge in the receiving hopper 32 (here, about 15% of the whole) is supplied to the mixer 78 by bypassing the dryer 54 by the transport device 79.
The mixer 78 is also composed of a paddle mixer, and its structure is basically the same as that of the mixer 40, and includes a pair of rotating shafts 44 and 46 and mixing blades 48 and 50 fixed thereto. The dry powder is mixed with the dewatered sludge that has been transported by the transport device 79 by their rotation.

The mixer 78 has the following meaning.
That is, the dried powder after being dried by the dryer 54 is not suitable for carbonization in the carbonization furnace 10 as it is, and cannot be directly supplied to the carbonization furnace 10.

Therefore, in the mixer 78, dehydrated sludge having a water content of about 80% is added to the dried powder and mixed to form dry sludge composed of dumpling particles having a water content of about 40% and a size of about 10 mm. Then, the dried sludge after granulation is supplied to the carbonization furnace 10 by the transfer device 82 through the relay hopper 80.
Subsequent carbonization of dried sludge is as described above.

  The airflow (exhaust gas) separated from the dry powder by the cyclone separator 72 passes through the bag filter 84 by the exhausting action of the exhaust gas fan 86 and is collected there, and then deodorized (here, a catalyst deodorizer). 88 is discharged from the chimney 90 to the atmosphere.

The catalyst deodorizing device 88 is provided to remove the odor because the exhaust gas from the carbonization furnace 10 is accompanied by an odor.
In addition, in order to perform deodorization by catalyst deodorization efficiently, it is necessary to heat exhaust gas. The temperature of the exhaust gas discharged from the cyclone separator 72 is a low temperature that is less than 300 ° C., where it is heated to a temperature of about 300 ° C. and then deodorized by catalyst deodorization.

In the figure, reference numeral 92 denotes a kerosene tank for generating the heat source. The kerosene supplied from the kerosene tank 92 is burned, and the deodorizing device 88 heats the exhaust gas.
The kerosene in the kerosene tank 92 is also supplied for combustion in the carbonization furnace 10.

In the sludge carbonization equipment of this embodiment as described above, the cost for installation can be reduced by omitting the hot air generating furnace, and the entire equipment can be downsized by omitting the installation of the hot air generating furnace.
Further, the heat energy required for drying in the dryer 54 can be reduced, and the running cost can be increased more than before.

Further, the dryer 54 used in the present embodiment has a simple structure and is downsized, and this can also realize downsizing and cost reduction of the entire equipment.
Furthermore, in this embodiment, when dry powder and dewatered sludge are mixed to form dry sludge for supply to the carbonization furnace 10, the moisture content of the dry sludge can be adjusted to an appropriate level by simply changing the mixing ratio. The water content can be adjusted.

  In this embodiment, the cyclone separator 72 is used for separating the dry powder, and the dry powder can be easily and efficiently separated and recovered from the airflow flowing out from the dryer 54.

  Although the embodiment of the present invention has been described in detail above, this is merely an example, and the present invention can be configured in various forms without departing from the spirit of the present invention.

It is the figure which showed the carbonization processing equipment of the sludge of one Embodiment of this invention. It is an enlarged view of the dryer in FIG. 1, and its peripheral part, and the enlarged view of the principal part of the mixer in FIG. It is a figure which shows an example of the conventional carbonization processing equipment of sludge. It is a figure which shows the structure of the dryer in FIG. It is a figure which shows the carbonization furnace in FIG.

Explanation of symbols

10 Carbonization furnace 40 Mixer (first mixing means)
54 Dryer 72 Cyclone Separator 74,76 Rotary Valve 78 Mixer (Second Mixing Unit)

Claims (2)

The dehydrated sludge after dehydrating the organic substance-containing sludge is dried by passing it through a drier, and the dried sludge is passed through a carbonization furnace and carbonized to produce carbonized products. As a heat source for drying, the exhaust gas is supplied to the dryer as hot air, and as the dryer, a mixture obtained by adding dry powder of the dehydrated sludge to a part of the dehydrated sludge is crushed into a crushed material. Using an airflow dryer that blows the hot air, conveys the crushed material by the airflow of the hot air, and dries it to form the dry powder, which is discharged with the airflow
(A) a first mixing means for mixing a part of the dewatered sludge and the dry powder to produce the mixture for supply to the dryer;
(B) a separator for separating the dried powder discharged from the dryer from the air stream;
(C) Distributing means for separating a part of the dry powder from the separator for supplying to the dryer and a remaining part for supplying to the carbonization furnace.
(D) adding the remaining part of the dehydrated sludge to the remaining part of the dry powder divided for supply to the carbonization furnace and mixing it to form dry sludge for supply to the carbonization furnace. And a mixing means, and the dried sludge mixed by the second mixing means is carbonized through the carbonization furnace.   2. The sludge carbonization facility according to claim 1, wherein the separator is a cyclone separator.

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