JP2007146130A - Method for producing solid fuel - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method for producing a solid fuel derived from an organic sludge, capable of suppressing inflammability in spite of having a high calorific value as the solid fuel and also without having excessive smell. <P>SOLUTION: This method for producing the solid fuel by carbonizing dried organic sludge by carbonizing equipment to make it as the solid fuel is provided by having a carbonizing process of carbonizing the dried organic sludge until becoming to have ≥1.0 and ≤1.8 ratio of the number of atoms of hydrogen to carbon (H/C), and bringing the dried sludge in contact with steam during the treatment in the carbonizing process. <P>COPYRIGHT: (C)2007,JPO&INPIT

Description

  The present invention relates to a solid fuel derived from organic sludge obtained by drying and sludgeting organic sludge, particularly sludge treated in a sewage treatment plant that burns with coal (hereinafter referred to as sewage sludge), human waste sludge. The present invention relates to a method for producing solid fuel derived from organic sludge such as livestock manure sludge and agricultural settlement drainage sludge, and a production facility for solid fuel.

Technology development related to effective use of organic sludge has been actively carried out in response to increasing environmental problems. Regarding the effective use of organic sludge, the technology to make carbonized sludge by further developing the use of green farmland and construction materials by composting has been developed.
In Patent Document 1, dry sewage sludge is granulated, carbonized at 300 to 600 ° C. for 4 to 22 minutes with a rotary kiln in an air shut-off atmosphere, and then immediately cooled, as a fuel substitute for boilers, cement kilns, etc. It is disclosed to use.
JP 2000-265186 A

The thing of patent document 1 has illustrated papermaking sludge, food sludge, and sewage sludge, and the said technique is made | formed as a uniform thing.
However, in the case of the prior art document 1, although the conditions are quite unclear, the atomic number ratio H / C is estimated from various numerical values listed as being 0.6 or less.
Moreover, in the thing of the prior patent document 1, it cannot be considered that high calorific value, suppression of ignitability, and suppression of odor can be achieved simultaneously.
Therefore, the main problem of the present invention is to provide a method for producing solid fuel derived from organic sludge and a facility for producing solid fuel that can suppress ignitability while having a high calorific value as a solid fuel and that does not have an excessive odor. It is to provide.

The present invention that has solved the above problems is as follows.
<Invention of Claim 1>
In the method for producing a solid fuel in which the dried organic sludge is carbonized by a carbonization facility, and this is used as a solid fuel,
Carbonizing the dried organic sludge until the atomic ratio H / C of hydrogen to carbon is 1.0 or more and 1.8 or less, and contacting with steam during the carbonization process A method for producing solid fuel derived from organic sludge.

(Function and effect)
When carbide is used as the solid fuel, the higher the calorific value, the better. As will be described in detail later, the calorific value greatly depends on the atomic ratio of hydrogen and carbon in the organic sludge, and rapidly decreases when the atomic ratio H / C is approximately 1.0 or less. To do. On the other hand, the present inventor has found that the ignition property of carbide depends on the atomic ratio H / C, and the atomic ratio H / C is in the range of 0.6 to 1.6, particularly 0.8 to less than 1.0. Found that it was highly ignitable. Furthermore, since the present invention is organic sludge, the odor also tends to remain for the carbide, and the residual odor is strong when the atomic ratio H / C is 1.0 or more. Therefore, there is no region that satisfies all of the high calorific value, low ignitability, and odor control.
However, in the present invention, the atomic ratio H / C of the hydrogen content and the carbon content in the organic sludge is 1.0 or more, and steam is blown into the carbonization facility. As described above, in the region where the atomic ratio H / C slightly exceeds 1.0 (the atomic ratio H / C is more than 1.0 to 1.6), the ignitability is not low. Further, when the atomic ratio H / C is 1.0 or more, the residual odor is strong.
On the other hand, when steam is blown in the carbonization facility according to the present invention, the ignitability can be suppressed, and the residual odor is reduced to an extent that does not become a problem. The reason why the ignition efficiency can be reduced by steam blowing is presumed that the easily oxidized components generated during carbonization are decomposed. It is estimated that the reason why the odor can be reduced is that the decomposition of the odor component in the dry organic sludge under the carbonization temperature condition is promoted by contact with steam. Thus, according to the present invention, the system satisfies all of the high calorific value, low ignitability, and odor suppression. It has been found that the upper limit of the atomic ratio H / C is preferably 1.8.
By the way, although the atomic ratio H / C of coal changes with production areas, it is less than 0.6-1.0, and an average is about 0.8. In this regard, although the conditions of the prior patent document are quite unclear, the atomic ratio H / C is estimated from various numerical values listed as being 0.6 or less. In this sense, the value of the atomic ratio H / C targeted by the present invention is quite high.

<Invention of Claim 2>
The method for producing a solid fuel derived from organic sludge according to claim 1, wherein the solid fuel is a solid fuel combusted with coal.

(Function and effect)
Since the solid fuel obtained by the present invention has a high calorific value, it is particularly useful when co-firing with coal in a coal-fired power plant.

<Invention of Claim 3>
The carbonization facility has a carbonization facility having an input port through which the dried organic sludge is charged and a discharge port through which the carbonized carbon from which the dry organic sludge is carbonized, wherein the carbonization step is a dry organic process of the carbonization facility. The solid fuel derived from organic sludge according to claim 1 or 2, wherein carbonization proceeds from the inlet of the activated sludge toward the carbide outlet, and the steam is blown so as to face the direction of the carbonization process. Production method.

(Function and effect)
When steam is blown from the carbide discharge side, it comes into contact with a higher partial pressure of steam in the area where carbonization has progressed compared to when steam is blown from the dry organic sludge charging side. The effect of suppressing and reducing the residual odor is high.

<Invention of Claim 4>
The carbonization equipment is a screw-type carbonization equipment that is transported toward an exhaust port by an externally heated rotary kiln or an internal screw, and the steam and / or inert gas so as to face the advancing direction of the carbonization process from the exhaust port side. V / S is 0.01 to 5.0 m / sec when the steam and / or inert gas blowing air volume is Vm ³ / sec, and the inner air cross-sectional area of the carbonization facility is Sm ^2. The manufacturing method of the solid fuel derived from the organic sludge of Claim 3 blown in on conditions.

(Function and effect)
Since the present invention is intended for organic sludge, particularly sewage sludge, it is desired to reduce the residual odor peculiar to the sludge as much as possible. As the carbonization equipment, an external heating type rotary kiln or a screw type carbonization furnace can be suitably employed rather than a fluidized bed carbonization furnace. In this case, as will be described later, due to the structure of the equipment, a zone where heat cannot be sufficiently applied is generated particularly on the steam blowing side (carbide discharge side). It has been found that if the dry distillation gas tends to stay on the blowing side (carbide discharge side), odor remains in the carbide. Therefore, when steam and / or inert gas is blown under the above conditions, the odor is reduced as shown in the examples described later.

<Invention of Claim 5>
The method for producing a solid fuel derived from organic sludge according to any one of claims 1 to 4, further comprising a granulation step of granulating the dry organic sludge before the carbonization step.

(Function and effect)
By granulating the dried organic sludge, the specific surface area of the carbide is reduced and contact with oxygen is reduced as compared with the case where no granulation is performed, so that the ignitability is suppressed. Moreover, handling property improves by granulation and a bulk density also increases.

<Invention of Claim 6>
In a solid fuel production facility that carbonizes dried organic sludge with a carbonization facility and uses this as a solid fuel,
A facility for producing solid fuel derived from organic sludge, characterized by comprising steam contact means for contacting with steam during carbonization in the carbonization facility.

(Function and effect)
From the viewpoint of equipment, the same effect as in claim 1 is obtained.

<Invention of Claim 7>
The carbonization facility has an inlet for supplying the dried organic sludge and an outlet for discharging the carbonized carbon of the dried organic sludge, and from the inlet of the dried organic sludge to the carbide outlet. The apparatus for producing solid fuel derived from organic sludge according to claim 6, further comprising steam contact means for blowing the steam so as to face the direction of carbonization.

(Function and effect)
From the viewpoint of equipment, the same effects as those of the third aspect can be achieved.

<Invention of Claim 8>
The production facility for solid fuel according to claim 6 or 7, further comprising a granulator for granulating the dried organic sludge in a preceding stage of the carbonization facility.

(Function and effect)
The same effects as those of the fifth aspect can be obtained from the viewpoint of equipment.

  According to the present invention, it is possible to produce an organic sludge-derived solid fuel that can suppress ignitability while having a high calorific value as a solid fuel and that does not have an excessive odor.

Hereinafter, the present invention will be described in detail based on specific examples.
<Basic knowledge>
As an example of organic sludge, when solid fuel obtained by drying and carbonizing sewage sludge is used as a substitute for fossil fuel, it is necessary to consider the energy consumed in the process of obtaining the fuel from the viewpoint of CO2 emissions. Necessary for solving.
That is, as shown in FIG. 1, electric power and fossil fuel (for example, kerosene) are consumed as energy required for drying and carbonization of sewage sludge. These can be expressed as CO2 emissions (1) associated with power consumption and CO2 emissions (2) associated with fossil fuel consumption. On the other hand, if the carbide | carbonized_material of a sewage sludge is used for an alternative fuel, the part will become the reduction amount (3) of CO2.
From the viewpoint of reducing CO2 emission, it is desirable that (1) + (2) <(3).
In the present invention, organic sludge is also used as an alternative fuel.

The inventor has tried many experiments. That is, for undigested sewage sludge from Sakai city sewage treatment plant, by changing the carbonization temperature and carbonization time, the hydrogen content and carbon content ratio H / C in the organic sludge was variously changed. When the calorific value was examined for these, the results shown in FIG. 2 were obtained.
According to the result of FIG. 2, the calorific value greatly depends on the atomic ratio of hydrogen and carbon, and decreases rapidly when the atomic ratio H / C is approximately 1.0 or less. On the other hand, when the atomic number ratio H / C is up to 1.8, the decrease in the calorific value is small.

  Moreover, when the ignition point temperature of the carbide | carbonized_material including the sewage sludge from other sewage treatment plants was investigated, the result shown in FIG. 3 was obtained. According to this result, the ignitability of the carbide depends on the atomic ratio H / C, and the atomic ratio H / C is in the range of 0.6 to 1.6, particularly 0.8 to less than 1.0. It turns out to be highly ignitable. Therefore, from the viewpoint of ignitability, the atomic ratio H / C is required to be 1.0 or more, more preferably 1.1 or more, and further preferably 1.4 considering the other characteristics. That's it.

  On the other hand, the present inventors have found that CO2 emissions can be reduced by using carbide of sewage sludge as an alternative fuel. However, in order to solve environmental problems, greenhouse gases other than CO2 are used. In addition, it is more important to make an assessment based on “total greenhouse gas emissions”. As the evaluation method, for example, it can be evaluated by the “Act on Promotion of Countermeasures against Global Warming” (hereinafter referred to as “Warming Law”) revised from April 1, 2006. According to the warm method, greenhouse gases other than CO2 include methane (CH4), dinitrogen monoxide (N2O), hydrofluorocarbons (HFC), perfluorocarbons, and sulfur hexafluoride (SF6). In addition, “total greenhouse gas emissions” refers to the emissions of the substance calculated by the method specified by the Cabinet Order for each substance that is a greenhouse gas, for each substance that is a greenhouse gas. Is the total amount obtained by multiplying by the coefficient specified by a Cabinet Order based on internationally recognized knowledge as a numerical value indicating the ratio of carbon dioxide to the extent that causes global warming. Article 2 of the law).

When solid fuel is produced from sewage sludge, the amount of greenhouse gas other than N2O is negligible, so that practically only N2O may be used as a greenhouse gas other than CO2. Here, since the global warming potential of N2O is 310, the contribution due to greenhouse gases other than CO2 (4) ≈N2O generation amount × 310. Therefore, total greenhouse gas emissions = (1) + (2) + (4). To discuss environmental issues in accordance with the temperature law, (1) + (2) + (4) <( 3) is desirable.
Based on the above relationship, for example, when kerosene is used as a fossil fuel, the relationship between the atomic ratio H / C and the total greenhouse gas emission was examined, and the result shown in FIG. 15 was obtained. According to this result, from the viewpoint of reducing the total amount of greenhouse gas emissions, it can be seen that the atomic ratio H / C is more preferably 1.2 or more.

  Furthermore, it is well known that the odor of dried sewage sludge is strong, and there is a tendency for the odor to remain in the carbides, and the odor is reduced as the atomic ratio H / C decreases, but the atomic ratio H from the dried sludge is reduced. It is clear from the results of a number of human odor tests that the residual odor is particularly strong when / C is in the range of 1.0.

FIG. 3 is merely the result of the ignition point temperature of the carbide, but the following experiment was conducted in order to investigate the ignition properties during storage and transportation when solid fuel was used from a more practical viewpoint.
That is, as shown in FIG. 4, a cylindrical stainless steel container 2 having an inner diameter of 240 mm and a height of 240 mm is installed in a thermostat 1 having a volume of 216 liters (600 mm cube), and Teflon (trade name) is positioned 30 mm from the bottom. A dispersion plate 3 composed of a punching plate (hole diameter 1 mm, pitch 1.5 mm, thickness 0.5 mm) was provided, and the sample was charged with a predetermined oxygen concentration from an oxygen cylinder and a nitrogen cylinder in a state of 3.5 kg. Blowing gas is blown from the blowing passage 4 through the bottom wall in the cylindrical stainless steel container 2. In this experiment, air is used and blown at a flow rate of 100 ml per minute. The gas in the container is released to the atmosphere through the exhaust path 5. At that time, the exhaust gas is subjected to gas component analysis by gas chromatography (not shown).
At that time, 15mm height center from the bottom of the container, 70mm height from the bottom of the container (40mm height from the dispersion plate), 115mm height from the bottom of the container (85mm height from the dispersion plate) center, 115mm height from the bottom of the container (dispersion) Thermoelectrically on the center of the exhaust gas outlet, near the exhaust gas outlet, in the thermostatic chamber 1, and on the outer surface of the container (85 mm high from the dispersion plate). A pair is attached and temperature is measured continuously.

In the above form, when air blowing is continued for about 50 hours, there is a temperature measurement point that reaches the maximum temperature after approximately 18 to 25 hours at each temperature measurement point. Based on the maximum temperature at the temperature measurement point that reaches the maximum temperature, it is used as an indicator of ignition.
FIG. 5 shows the results obtained by examining the change in the atomic ratio H / C and the maximum temperature reached with or without the addition of steam under such test conditions.
It can be determined that the lower the maximum temperature is, the lower the ignitability, and the results shown in FIG. 5 indicate that the maximum temperature is lowered by the addition of steam and the ignitability can be suppressed. Further, FIG. 6 shows the result of examining the relationship with the outlet oxygen concentration in the gas analysis of the exhaust gas. It can be determined that the higher the outlet oxygen concentration is, the lower the ignitability is, and the results shown in FIG. 6 indicate that the addition of steam increases the outlet oxygen concentration and suppresses the ignitability.

On the other hand, it is desirable to have a granulation step for granulating dry organic sludge before the carbonization step. In granulation, it is desirable that the particle size be 3 to 20 mm, particularly 4 to 15 mm. If the particle size is small, the effect of suppressing the ignitability is not sufficient, and the effect of improving the handling property is not sufficiently exhibited. If the particle size is excessively large, problems such as a long carbonization time remain. Furthermore, when granulating into cylindrical pellets, the effect of suppressing ignitability and the effect of improving handling properties are high, and it is found that φ4 to 8 mm × 5 to 20 mmL is optimal as the particle size in that case. ing.
Table 2 shows the maximum temperature achieved when the dried sludge is granulated into carbon pellets (φ5-6 mm × 5-12 mmL) and carbonized, and when carbonized without granulation. It can be seen that by granulating, the maximum temperature reached becomes low, and the ignitability can be suppressed.

An odor test was performed for the case where the steam ratio of H / C shown in FIGS. 5 and 6 was 1.58 and the case where no steam was added.
That is, after production, a certain amount of fuel is measured and stored in a container with a certain capacity, and then stored at room temperature for 1-2 days. The subject determined the odor of this sample by the “6-level odor intensity display method”. The number of subjects was 10 in order to prevent bias due to individual differences. Here, the odor intensity was rated according to the following criteria.
0: Odorless 1: Smell that can finally be detected 2: Weak scent that tells what smell it is 3: Smell that can be easily detected 4: Strong smell 5: Strong smell Three-stage evaluation was also conducted. ○: Acceptable odor △: Slightly unpleasant ×: Unpleasant results are shown in Table 1. For reference, dry sewage sludge itself was also evaluated.

  From the results shown in Table 1, the addition of steam also reduced the odor intensity, which was acceptable for most subjects. For reference, the odor reduction is significant in comparison with the results of dry sewage sludge.

<Other findings>
The atomic ratio H / C of the hydrogen content and the carbon content in the solid fuel correlates with the carbonization time used for carbonization and the carbonization temperature.
About carbonization of the sewage sludge in FIG. 7, it was shown that atomic ratio H / C changes with carbonization temperature and carbonization time.
FIG. 8 shows the correlation of the fuel ratio with respect to the atomic ratio H / C.
FIG. 9 shows various correlations with the carbonization temperature.
Other examples of organic sludge include human waste sludge and livestock manure sludge, but we know that there is no significant difference from the case of sewage sludge. It will be easy to see that there is no difference.

<Equipment example>
FIG. 10 shows a first example of manufacturing equipment. The dehydrated organic sludge 1 dehydrated by a belt press or the like is supplied to a dryer 10. The dryer 10 is dried by hot air from the first hot air furnace 12, and the dried sludge 2 is granulated by the granulator 26. As the granulator, a mixing granulator, a compression granulator, or the like can be applied, and an extrusion granulator is particularly suitable. The granulated dried sludge is supplied to a carbonization furnace 20 such as a rotary kiln. In the carbonization furnace 20, the combustion air is heated by the second heat exchanger 18, and this is blown with hot air heated under the fuel in the second hot air furnace 22 to perform carbonization. The carbonization furnace 20 has a configuration in which carbonization proceeds from a dry organic sludge inlet to a carbide outlet.

  The carbonized sludge is cooled and then used as a solid fuel. The granulation may be performed after carbonization, and rolling granulation and mixed granulation can be applied as the granulator, but compression granulation is preferable.

  The dry distillation gas generated in the carbonization furnace 20 is reburned by the reburning furnace 14 under the blowing of combustion air and fuel, and is used as a heating source of the hot air for drying in the dryer 10 in the first heat exchanger 16. The exhaust gas from the dryer 10 passes through the first heat exchanger 16, receives the heat of the exhaust gas from the reburning furnace 14, and is sent to the first hot stove 12. A part of the exhaust gas from the dryer 10 is guided to the dehumidifying tower 24, and after the humidity is reduced, it is injected so that the combustion efficiency in the reburning furnace 14 can be increased.

  FIG. 11 shows a second example of equipment, in which the dehumidifying tower 24 is not used, and the exhaust gas of the dryer 10 is reburned in the reburning furnace 14 and then the exhaust gas is returned to the dryer 10. It is. In the first heat exchanger 16, the combustion air is heated by the exhaust gas from the reburning furnace 14 and blown into the reburning furnace 14.

In the present invention, steam is added in any of the above examples.
As the steam addition conditions, a carbonization temperature of 250 to 350 ° C is desirable, and a temperature of 100 to 350 ° C is desirable from the viewpoint of preventing temperature decrease. The pressure may be appropriate, but atmospheric pressure to about 0.1 MPa is sufficient. The added flow rate is preferably 0.1 to 10 kg-water vapor per 1 kg of dried sludge. In addition, as shown in FIGS. 10 and 11, when the steam is blown from the carbide discharge side so as to face the direction of carbonization, the steam is blown from the dry organic sludge input side. Thus, in the region where carbonization has progressed, the contact is made in a state where the steam partial pressure is higher, so that the effect of suppressing ignitability and reducing the residual odor is high. Moreover, condensation of dry distillation gas can be aimed at by blowing inactive gas (for example, nitrogen gas) in addition to steam.

  These facilities are examples, and other forms can naturally be adopted. Moreover, there is no limitation on the type of the dryer 10 or the carbonization furnace 20. Incidentally, types of the carbonization furnace 20 include a rotary kiln, a screw type, a fluidized bed type, and the like. In the dryer 10, the outlet moisture is preferably 10 to 40%, particularly 15 to 25%.

  In addition, as carbonization conditions, the carbonization temperature is 250-350 degreeC from the result of FIGS. 7-9, and carbonization time 20-60 minutes is suitable.

As shown in FIG. 12, in the rotary kiln 20A, generally, hot air is blown into the outer cylinder 20a to give heat to the sludge in the inner cylinder. The region corresponding to the region supported by the non-heated portion (portion where heat cannot be sufficiently applied outside the installation range of the outer cylinder 20a) L. It was found that in the non-heated part L, dry distillation gas stays and odor remains in the carbonized sludge.
Therefore, when the steam and / or inert gas blowing rate is Vm3 / sec, the carbonization facility, in the example of FIG. 12, the inner space (internal space) cross-sectional area of the rotary kiln 20A is Sm2, V / S is 0.01-5. If it is blown at 0.03 to 3.0 m / sec under the condition of 0.0 m / sec, the strength of the odor remaining in the carbonized sludge can be reduced. Excessive blowing flow rate should be avoided to control the amount of entrained dust.
The rotary kiln 20A that can be suitably employed has an inner diameter of 0.1 to 4 m, an outer cylinder 20a length of 1 to 35 m, and a non-heated portion L length of 0.3 to 5 m.

  On the other hand, as shown in FIG. 13, a rotary kiln 20B can be used in which a non-heated portion L region is formed with a narrowed portion 20b whose diameter is gradually reduced from the end portion of the outer cylinder 20a and further formed with a small diameter portion 20c. In this embodiment, the blowing flow rate can be increased, and the retention of dry distillation gas hardly occurs, and the odor residue can be suppressed. The horizontal projection length of the narrowed portion 20b can be 0 to 2 m, and the length of the small diameter portion 20c can be 0.5 to 5 m (the length of the narrowed portion 20b is 0 m, the entire non-heated portion L region has a small diameter It means that it is a part 20c.) Further, the inner diameter of the small diameter portion 20c is 0.1 m or more due to the structure of the discharge mechanism.

  The screw type carbonization furnace 20C of FIG. 14 can also be used. Reference numeral 20d denotes a screw conveyor. The screw-type carbonization furnace 20C that can be suitably used has an inner diameter of 0.1 to 1 m, a heating part 20e length of 1 to 20 m, and a non-heating part L length of 0.3 to 3 m.

  Using the rotary kiln 20A of FIG. 12 (inner diameter is 0.35m, outer cylinder 20a length is 2.5m, non-heating part L length is 0.4m), steam and / or inert gas is blown, and The same odor test was performed. The results are shown in Table 3. The odor changes depending on the blowing conditions, and it can be seen that the residual odor is not a problem under the above conditions. Although Table 3 does not show the result of 0.01 m / sec, it has been found that residual odor does not cause a problem.

  The obtained solid fuel is particularly effective when co-firing with coal in a coal-fired power plant, but it can also be applied to boilers that use solid fuel as fuel.

It is explanatory drawing regarding the amount of CO2. It is a correlation diagram of atomic ratio H / C and calorific value. It is a correlation diagram of atomic number ratio H / C and ignition point temperature. It is a schematic diagram of a ignitability test device. It is a correlation diagram of atomic ratio H / C and the highest attained temperature. It is a correlation diagram of atomic number ratio H / C and exit oxygen concentration. It is a correlation diagram of atomic number ratio H / C, carbonization temperature, and carbonization time. It is a graph which shows the correlation of the fuel ratio with respect to atomic ratio H / C. It is a graph which shows the various correlation with carbonization temperature. It is a flow sheet of the 1st example of equipment. It is a flow sheet of the 2nd example of equipment. It is a schematic diagram of a rotary kiln. It is a schematic diagram of another rotary kiln. It is a schematic diagram of a screw type carbonization furnace. It is a graph which shows the relationship between atomic number ratio H / C and greenhouse gas total discharge.

Explanation of symbols

  DESCRIPTION OF SYMBOLS 1 ... Dehydrated organic sludge, 10 ... Dryer, 14 ... Recombustion furnace, 16 ... 1st heat exchanger, 20 ... Carbonization furnace, 22 ... 1st hot air furnace, 26 ... Granulator.

Claims (8)

In the method for producing a solid fuel in which the dried organic sludge is carbonized by a carbonization facility, and this is used as a solid fuel,
Carbonizing the dried organic sludge until the atomic ratio H / C of hydrogen to carbon is 1.0 or more and 1.8 or less, and contacting with steam during the carbonization process A method for producing solid fuel derived from organic sludge.   The method for producing a solid fuel derived from organic sludge according to claim 1, wherein the solid fuel is a solid fuel combusted with coal.   The carbonization facility has a carbonization facility having an input port through which the dried organic sludge is charged and a discharge port through which the carbonized carbon from which the dry organic sludge is carbonized, wherein the carbonization step is a dry organic process of the carbonization facility. The solid fuel derived from organic sludge according to claim 1 or 2, wherein carbonization proceeds from the inlet of the activated sludge toward the carbide outlet, and the steam is blown so as to face the direction of progress of the carbonization step. Manufacturing method. The carbonization equipment is a screw-type carbonization equipment that is transported toward an exhaust port by an externally heated rotary kiln or an internal screw, and the steam and / or inert gas so as to face the advancing direction of the carbonization process from the exhaust port side. V / S is 0.01 to 5.0 m / sec when the steam and / or inert gas blowing air volume is Vm ³ / sec, and the inner air cross-sectional area of the carbonization facility is Sm ^2. The manufacturing method of the solid fuel derived from the organic sludge of Claim 3 blown in on conditions.   The method for producing a solid fuel derived from organic sludge according to any one of claims 1 to 4, further comprising a granulation step of granulating the dry organic sludge before the carbonization step. In a solid fuel production facility that carbonizes dried organic sludge with a carbonization facility and uses this as a solid fuel,
A facility for producing solid fuel derived from organic sludge, characterized by comprising steam contact means for contacting with steam during carbonization in the carbonization facility.   The carbonization facility has an inlet for supplying the dried organic sludge and an outlet for discharging the carbonized carbon of the dried organic sludge, and from the inlet of the dried organic sludge to the carbide outlet. The apparatus for producing solid fuel derived from organic sludge according to claim 6, further comprising steam contact means for blowing the steam so as to face the direction of carbonization.   The production facility for solid fuel according to claim 6 or 7, further comprising a granulator for granulating the dried organic sludge in a preceding stage of the carbonization facility.

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