KR102354457B1 - Manufacturing method of sludge fuel coal using waste mushroom medium and rice husk - Google Patents

Abstract

According to the present invention, fuel coal that is environmentally friendly and has excellent calorific value by using a large amount of waste medium discarded after use for culturing various kinds of mushrooms, rice husks generated during a milling process of rice, and a huge amount of sewage sludge generated from domestic sewage can be manufactured. Accordingly, in the present invention, reusability of plant residues can be maximized, greatly energy saving is possible due to stable and long-term high calorific value, and the fuel coal has high utility value as new renewable energy.

Description

Manufacturing method of sludge fuel coal using waste mushroom medium and rice husk

The present invention relates to a method for producing sludge fuel coal, and more particularly, a large amount of waste medium that is discarded after being used for culturing various kinds of mushrooms, plant residues generated from plants such as rice, sugar cane, and domestic sewage. It relates to a method for producing an eco-friendly and excellent calorific value by using a huge amount of sewage sludge.

Background to the present disclosure is provided herein, which does not necessarily imply known art.

In general, although the waste medium after culturing various types of mushrooms has a high re-use value as a fuel, it is common to use most of them only as an additive to be mixed in fertilizer or compost production. Alternatively, it is mixed with the contents for diluting the salt concentration during food treatment and used as feed, but it has a disadvantage in that it is difficult to digest and absorb, so that it is not realistic.

In addition, mushroom production has steadily increased in the era of well-being, and the production of waste media in Korea alone in 2011 was 1,500,000 tons.

On the other hand, rice is one of the world's three major grains, used as a staple food by half of the world's population, and is a valuable food resource, especially in Asia, a key national resource that cannot be replaced with other crops. Rice husks generated after milling rice are substances composed of moisture, crude fat, cellulose, lignin, and pectin, and fiber and ash. Such rice husks have been used as litter or compost in livestock and fruit farms, but their efficacy value is insignificant due to the slow decomposition or decay rate. In reality, the range of use is very high, but the volume is very large, so it is difficult to transport and transport, so it is almost discarded.

In addition, sewage sludge generated from domestic sewage was also generated approximately 6,000 tons/day in 2002 in Korea, and the amount is increasing tremendously over the years.

The present invention provides a technique for using the above enormous amount of mushroom waste medium, rice husk and sewage sludge as fuel coal.

In the prior art that utilizes the above-mentioned waste medium of mushrooms to be used as fuel, Korean Patent Publication No. 10-1609696, Republic of Korea Patent Publication No. 10-1728233, Republic of Korea Patent Publication No. 10-1953361, Republic of Korea It has been published in Korean Patent Publication No. 10-2078958 (hereinafter referred to as 'prior art documents 1').

In addition, the prior art using rice husk to be used as fuel has also been published in Korean Patent Publication No. 10-1065459, Korean Patent Application Laid-Open No. 10-2009-0036262, Korean Patent Publication No. 10-0979391, etc. There is (hereinafter referred to as 'prior art documents 2').

In addition, the prior art using sewage sludge to be used as fuel has also been published in Korean Patent Publication No. 10-1779136, Korean Patent Publication No. 10-1896641, Korean Patent Publication No. 10-2009184, etc. Yes (hereinafter referred to as 'Prior Art Documents 3').

The above-mentioned prior art documents 1 to 3 prepared pellets as fuels using only each raw material, but a method for manufacturing a fuel coal using all of these raw materials was not presented.

1. Republic of Korea Patent Publication No. 10-1609696 2. Republic of Korea Patent Publication No. 10-1728233 3. Republic of Korea Patent Publication No. 10-1953361 4. Republic of Korea Patent Publication No. 10-2078958 5. Republic of Korea Patent Publication No. 10-1065459 6. Korean Patent Publication No. 10-2009-0036262 7. Republic of Korea Patent Publication No. 10-0979391 8. Republic of Korea Patent Publication No. 10-1779136 9. Republic of Korea Patent Publication No. 10-1896641 10. Republic of Korea Patent Publication No. 10-2009184

The specific technical solution of the present invention for solving the various conventional problems as described above is a large amount of waste media and vegetable residues that are discarded after being used for culturing various kinds of mushrooms, especially rice husks and domestic sewage generated during milling of rice. An object of the present invention is to provide a method for manufacturing fuel coal which is eco-friendly and has excellent calorific value by using a huge amount of generated sewage sludge.

However, the objects of the present invention are not limited to the above-mentioned objects, and other objects not mentioned will be clearly understood by those skilled in the art from the following description.

The present invention is a pre-treatment step (S1) of pre-treatment of raw materials including mushroom waste medium, rice husk and sewage sludge; a mixing step (S2) of mixing the pre-treated raw materials to obtain a raw material mixture; a first drying step (S3) of primary drying the raw material mixture to have a first moisture content using a bio-drying device; a second drying step (S4) of secondary drying the firstly dried mixture to have a second moisture content lower than the first moisture content using a thermal drying device; and a molding step (S5) of press-molding the secondary dried mixture to form a fuel coal;

In addition, in the pretreatment step (S1), the sewage sludge is dried to a moisture content of 70% by weight to 80% by weight, the mushroom waste medium is dried to a moisture content of 50% to 60% by weight, and the rice hull is dried to a moisture content of 30% to 40% It is characterized in that it is a step of wet processing.

In addition, the mixing step (S2) is characterized in that 100 to 150 parts by weight of the dried mushroom waste medium and 30 to 50 parts by weight of the wet-treated rice hull are mixed with respect to 100 parts by weight of the dried sewage sludge.

In addition, in the first drying step (S3), in controlling the bio-drying device, after the primary control of adjusting the air supply amount according to the temperature change of the exhaust gas, adjusting the air supply amount according to the change in _{the CO 2 concentration inside the device} It is characterized in that it is a step of maintaining the first moisture content of the discharged primary dried mixture by repeating the routine including the secondary control.

In addition, in the second drying step (S4), in controlling the thermal drying device, after the first control of measuring the temperature of the exhaust gas to adjust the temperature of the supplied steam, the pressure inside the device is measured to adjust the gas emission. It is characterized in that it is a step of maintaining the second moisture content of the discharged secondary dried mixture by repeating the routine including the secondary control.

In addition, the molding step (S5) is a primary molding step of forming the primary fuel coal by putting the secondary dried mixture into a molding machine and drying and molding using compression heat and friction heat of 100 to 130° C. generated through the compression process. (S51) and the secondary molding step (S52) of re-injecting the primary fuel coal into the molding machine and drying and molding it using the compression heat and friction heat of 130 to 160° C. generated through the high-pressure compression process (S52) characterized by including.

The present invention is eco-friendly (reducing odor) and also has a calorific value by using a large amount of waste medium discarded after use for culturing various kinds of mushrooms, rice husk, a by-product generated during rice milling, and a huge amount of sewage sludge generated from domestic sewage. By providing a method for manufacturing an excellent coal coal, it has the effect of maximizing reusability and greatly contributing to energy saving due to high calorific value for a long time stably, as well as having a high utility value as a new and renewable energy.

1 is a block diagram for explaining the process of manufacturing a fuel coal using mushroom waste medium, rice husk and sewage sludge of the present invention.
2 schematically shows the configuration of a system in which the method for manufacturing coal fuel according to the present invention is performed.
3 to 7 are exemplary views showing the bio-drying apparatus in more detail, FIG. 3 is a plan view schematically illustrating the internal and external configuration of the bio-drying apparatus, and FIG. 4 is a schematic view of a configuration different from that of FIG. It is an example view of the side indicated by . In addition, FIG. 5 is an exemplary view showing the front part and the central part of the bio-drying apparatus viewed from the direction A of FIG. 3 , and FIG. 6 is a view showing the first mantle part from the direction B of FIG. 3 . It is one example diagram. In addition, FIG. 7 is an exemplary view showing a spiral configured in all of the bio-drying apparatus.
8 to 13 are exemplary views illustrating the thermal drying apparatus of FIG. 2 in more detail. FIG. 8 is a schematic side projection view illustrating the thermal drying apparatus according to the present invention, and FIG. 9 is an internal disk assembly It is an exemplary diagram showing the structure in more detail. And FIG. 10 is an exemplary view showing the disk viewed from the side, and FIGS. 11 to 13 are perspective views showing partial cross-sections of the disk.

All technical and scientific terms used herein have the same meaning as commonly understood by those of ordinary skill in the art, unless otherwise stated. Also throughout this specification and claims, unless otherwise indicated, the term comprise, comprises, comprising is meant to include the recited object, step or group of objects, and steps, and any other It is not used in the sense of excluding an object, step, or group of objects or groups of steps.

Prior to describing the present invention in detail below, it is to be understood that the terminology used herein is for the purpose of describing specific embodiments and is not intended to limit the scope of the present invention, which is limited only by the appended claims. shall.

On the other hand, various embodiments of the present invention may be combined with any other embodiments unless clearly indicated to the contrary. Any feature indicated as particularly preferred or advantageous may be combined with any other feature and features indicated as preferred or advantageous. Hereinafter, embodiments of the present invention and effects thereof will be described with reference to the accompanying drawings.

< Method for manufacturing sludge fuel coal>

The method for producing sludge fuel coal according to the present invention uses a large amount of mushroom waste medium with high reuse value as a fuel, rice husk, a by-product generated during rice milling, and a huge amount of sewage sludge to be used as fuel for combustion in each field. It is a technology that can manufacture fuel that can be used.

The method for producing the sludge fuel coal includes a pre-treatment step (S1) of pre-treating raw materials including mushroom waste medium, rice husk and sewage sludge; A mixing step (S2) of mixing the pre-treated raw materials to obtain a raw material mixture, a first drying step (S3) of primary drying the raw material mixture to have a first moisture content using a bio-drying device (S3), the primary dried A second drying step (S4) of secondary drying the mixture to have a second moisture content lower than the first moisture content using a thermal drying device, and a molding step (S5) of press-molding the secondary dried mixture to form fuel coals (S5) includes

The pre-treatment step (S1) is a step of pre-treating raw materials including mushroom waste medium, rice husk and sewage sludge, and the sewage sludge has a moisture content of 80% by weight or less (preferably 70% to 80% by weight, more preferably 75% by weight). Dry to 80% by weight), and dry the mushroom waste medium to a moisture content of 60% by weight or less (preferably 50% to 60% by weight, more preferably 55% to 60% by weight), and rice husk It is a wet treatment step with a moisture content of 30% by weight or more (preferably 30% to 40% by weight, more preferably 30% to 35%).

When each pretreated with the above moisture content, it has a high calorific value for a long time stably and provides a high utility value as a new renewable energy. In order to support this, the calorific value per unit weight of the fuel coal prepared according to the pretreatment conditions was measured and shown in Table 1 below. Here, the moisture content presented in Table 1 below is adjusted to be close to the value presented in the actual process, and may not have exactly the specified value.

Example 1 Example 2 Example 3 Comparative Example 1 Comparative Example 2 Comparative Example 3 moisture content
(%) sewage sludge
(100kg) 80 70 75 preprocessing X 85 65 Mushroom Waste Media
(130kg) 60 50 55 65 45 chaff
(40kg) 30 40 35 25 45 Calorific value (kcal/kg) 4864 4550 5002 3716 3941 4117 Heating time (hr) 12 11 12 8 10 9

As shown in Table 1 above, the fuel coal manufactured from the raw material pretreated according to the embodiment of the present invention has a calorific value and heat compared to the fuel coal manufactured from the raw material not pretreated according to the comparative example or the fuel coal manufactured from the fuel pretreated outside the conditions It can be confirmed that all of the time is excellent, and in particular, the fuel coal prepared from the raw material pretreated under the conditions according to Examples 1 and 3 has the most stable and high calorific value for a long time, providing a high utility value as a new renewable energy.

The sewage sludge is a residue remaining after separating the fluid from the sewage and drying, and is composed of an organism that can burn easily when dried. Since sewage sludge contains various foreign substances, such as vinyl, tree branches, and iron, remove foreign substances.

In this way, the sewage sludge from which foreign substances are removed is dried to a moisture content of 80% by weight or less using a pretreatment device. When direct heat is applied to drying the sewage sludge, it is preferable to dry the sewage sludge with hot air, which is indirect heat, since the sewage sludge may be carbonized.

In the above, drying the moisture of the collected sewage sludge to 80% by weight or less can increase the mixing efficiency when mixing raw materials, and the mixed raw material mixture in consideration of the moisture content of the pre-treated mushroom waste medium and rice husk is biodrying device to have optimal drying efficiency when drying microorganisms using

Since the mushroom waste medium contains a lot of moisture from mushroom cultivation, it is dried to a moisture content of 60% by weight or less by using a pretreatment device after removing foreign substances like the sewage sludge.

In the above, drying the moisture of the collected mushroom waste medium to 60% by weight or less can increase the mixing efficiency when mixing raw materials, and the mixed raw material mixture is biodrying in consideration of the moisture content of the pretreated sewage sludge and rice husk. to have optimal drying efficiency when drying microorganisms using

In general, the rice hull has a moisture content of 14%-15% and an organic matter of 25% or more, but a C/N ratio of 50 or less is insufficient for the growth of microorganisms. Therefore, the rice hull is treated to have a moisture content of 30% by weight or more.

In the above, wet treatment of rice hull moisture to 30% by weight or more can increase mixing efficiency when mixing with sewage sludge and mushroom waste medium, as well as mixing raw material mixture in consideration of the moisture content of pretreated sewage sludge and mushroom waste medium This bio-drying device is used to ensure optimum drying efficiency when microorganisms are dried, and provides excellent calorific value and exothermic time as described above.

The mixing step (S2) is a step of obtaining a raw material mixture by mixing the pre-treated mushroom waste medium, rice husk and sewage sludge, and 100 to 150 parts by weight of the dried mushroom waste medium with respect to 100 parts by weight of the dried sewage sludge (preferably is 100 to 130 parts by weight), a step of mixing 30 to 50 parts by weight (preferably 30 to 40 parts by weight) of the wet-treated rice husk.

When mixed in the above content ratio, it has a high calorific value for a long time stably and provides a high utility value as a new renewable energy. In order to support this, the calorific value per unit weight of the fuel coal prepared according to the mixing ratio was measured and shown in Table 2 below. Here, the moisture content presented in Table 2 below is adjusted to be close to the value presented in the actual process, and may not have exactly the specified value.

Example 3 Example 4 Example 5 Example 6 Comparative Example 4 Comparative Example 5 Comparative Example 6 Comparative Example 7 content
(kg) sewage sludge
(75%) 100 100 100 100 100 100 100 100 Mushroom Waste Media
(55%) 130 100 150 100 80 170 80 170 chaff
(35%) 40 30 50 50 20 60 60 20 Calorific value (kcal/kg) 5002 4925 4789 4816 4156 4253 4034 3931 Heating time (hr) 12 11 10 11 9 10 9 8

As shown in Table 2 above, it can be confirmed that the fuel coal manufactured with the mixed raw material mixture according to the embodiment of the present invention is superior to both the calorific value and the heating time compared to the fuel coal manufactured with the mixed raw material mixture out of the conditions. The fuel coal produced from the raw material mixture mixed under the conditions according to Examples 3 and 4 is the most stable and has a high calorific value for a long time, providing a high utility value as a new and renewable energy.

When the raw material mixture is mixed in the mixer, an additive may be further added to be mixed. The additive includes a first additive including at least one selected from the group consisting of charcoal, activated carbon, and combinations thereof, and a second additive including at least one selected from the group consisting of dried sludge, dried coffee sludge powder, and combinations thereof. and a third additive including at least one selected from the group consisting of additives, adhesives, lignin, and combinations thereof.

The additive includes the first additive, the second additive, and the third additive in a weight ratio of 1:0.2 to 0.8:0.2 to 0.8, and the ligrin is sodium lignosulfonate or calcium lignosulfonate. (calcium lignosulfonate).

Lignin refers to a fat-soluble phenolic polymer among various components constituting the woody part of conifers and hardwoods, and has heterogeneous and amorphous characteristics. Therefore, when the lignin is used alone among the third additives, the strength and calorific value of the fuel coal can be adjusted without a separate adhesive or additive by adjusting the amount of the lignin.

In the above, the additive serves to enhance the formability of the mixture as well as to reinforce the strength and, in particular, to enhance the calorific value during combustion after being finally formed into the second fuel coal, so that it can have excellent combustion efficiency as well as excellent calorific value.

20 to 30 parts by weight of the additive is mixed with respect to 100 parts by weight of the dried sewage sludge, and the additive is mixed with the first additive, the second additive and the third additive in a weight ratio of 1:0.4 to 0.6:0.4 to 0.6. desirable. This mixing ratio affects the calorific value in the process of burning the manufactured fuel coal.

The first drying step (S3) is a step of primary drying the raw material mixture to have a first moisture content using a bio-drying (microorganism drying) device, and the organic matter in the mixture is decomposed or decomposed by contact with microorganisms or oxygen It is a step in which drying is carried out by oxidizing heat.

More specifically, in the first drying step (S3), oxygen (O ₂ ) in the air is supplied to the inside of the bio-drying apparatus to induce metabolism of aerobic microorganisms, and organic matter is converted into carbon dioxide (CO ₂ ), water ( The raw material mixture is dried using the heat of metabolism generated when decomposed into _{H 2 O) and ammonia.}

The first moisture content is approximately 35 to 40% by weight, and when the first moisture content exceeds 40% by weight, a large amount of fuel is consumed in the second drying step by the subsequent thermal drying apparatus, and when it is less than 35% by weight, bio-dry The size of the incubator must be increased, or the residence time of the raw material mixture in the bio-drying apparatus becomes longer. That is, according to the adjustment of the first moisture content, the economical deterioration due to the fuel consumption for drying or the increase in the residence time of the bio-drying device occurs. Therefore, the first moisture content is a matter to be adjusted according to the structure and size of the bio-drying apparatus, and does not necessarily have to be defined as a specific moisture content.

In addition, in the first drying step (S3), in controlling the bio-drying device, the exhaust gas temperature (or the internal temperature of the device) and the CO ₂ concentration are used as common indicators, and by controlling the air supply amount supplied to the bio-drying device. The drying efficiency can be optimized. _{That is, the temperature and the CO 2} concentration inside the bio-drying device or the exhaust gas are maintained within a certain range, so that the dry state (moisture content) of the discharged primary dried mixture can be maintained at a certain level.

More specifically, after the primary control (control to increase, maintain, or decrease the air supply so that the temperature is constant within a specific range) for adjusting the air supply amount according to the temperature change of the exhaust gas, the air according to the change in the CO ₂ concentration inside the device The routine including the secondary control for adjusting the supply _{amount (control to increase, maintain, or decrease the air supply amount so that the CO 2} concentration is constant within a specific range) is repeated to maintain the first moisture content of the discharged primary dried mixture do.

In the first drying step (S3), the heat of metabolism of aerobic microorganisms, which is the sole or main drying heat source, is generated from the aerobic decomposition reaction of biodegradable organic materials, and the degree of this decomposition reaction can be specified by the concentration of _{CO 2 in the exhaust gas.} can In addition, since the change in the CO ₂ concentration is first observed before the exhaust gas temperature changes, it is a more sensitive reaction index to judge the activity of microorganisms than the temperature change due to the generation of metabolic heat. can be controlled

However, optimal bio by controlling the to measure only the CO ₂ concentration control the air flow rate also is not a suitable control method control according to the temperature change and complementary to exactly proportional to the change in concentration of CO _2, because not the temperature change It can provide a drying effect.

As the second indicator, the _{change in ammonia (NH 3} ) concentration caused by the metabolism of microorganisms can also be used as an indicator, but in the case of _{NH 3 , compared to CO 2} , the reliability of the identification of drying conditions is low due to the nature of the solubility in water. It is preferable to measure the change in the _{CO 2} concentration as an indicator.

The second drying step (S4) is a step of secondary drying the firstly dried mixture to have a second moisture content lower than the first moisture content by using a thermal drying device, and the primary dried mixture is molded into fuel. This is a step in which drying is performed by a heating means so that the second moisture content, which is a possible moisture content, is obtained.

The second drying step (S4) uses an indirect heating method rather than a direct heating method by a heat source to prevent the primary dried mixture having an already lowered moisture content (first moisture content) from being carbonized or oxidized in the secondary drying process. and dry it. For example, it is dried by heating the vessel or the stirring unit through hot air or steam generated through a boiler or heater.

The second moisture content is not limited as long as it is a moisture content that can be molded into fuel and is lower than the first moisture content, and it is not necessarily defined as a specific moisture content. It is preferably dried to about 10% by weight or less. This is to minimize the moisture content as much as possible immediately before molding into fuel coal, and if there is no moisture completely, it contains a small amount of moisture as the moldability deteriorates.

In the second drying step (S4), in controlling the thermal drying device, the temperature of the exhaust gas and the pressure inside the device are used as common indicators, and the temperature and gas intake amount (gas emission) of the steam supplied to the thermal drying device By adjusting the drying efficiency can be optimized. That is, the temperature and internal pressure of the internal or exhaust gas of the thermal drying device are maintained within a predetermined range, thereby maintaining the dry state (moisture content) of the discharged secondary dried mixture at a predetermined level.

More specifically, the device after the primary control (control to increase, maintain, or decrease the temperature of the supplied steam so that the temperature of the exhaust gas is constant within a specific range) for measuring the temperature of the exhaust gas and adjusting the temperature of the supplied steam By repeating the routine including the secondary control (control to increase, maintain, or decrease the gas discharge so that the pressure inside the device is constant within a certain range) to control the gas discharge by measuring the pressure inside, the secondary drying that is discharged The second moisture content of the prepared mixture is maintained.

In the second drying step (S4), the higher the supply temperature of steam, which is the sole or main drying heat source, is, the greater the amount of thermal energy transferred to the internal mixture. The degree of evaporation of water can be determined.

The higher the steam supply temperature, the higher the exhaust gas temperature and the higher the moisture evaporation rate. However, the supply temperature of steam is limited by the specifications of the steam production facility, and since more fossil fuels or electric power are consumed to produce high-temperature steam, proper control of the steam supply temperature is required.

The water vapor generated by the evaporation of the moisture contained in the mixture is discharged to the outside of the drying device together with the air introduced from the outside, thereby carrying out the second drying step. It is a major factor, and by observing the internal pressure of the thermal drying device, the degree of emission of gases including water vapor can be grasped.

As the amount of gas discharged increases, the internal pressure of the thermal drying device is lowered and the gas is discharged smoothly, but the inflow of outside air, which has a significantly lower temperature than the inside of the thermal drying device, increases, and the drying performance may be reduced due to the cooling effect. Adequate control is also required.

In addition, since the required amount of external air inflow and the amount of water vapor generated differ depending on the operating conditions and conditions of the thermal drying device, it is impossible to determine the smoothness of gas discharge and prevent gas leakage to the outside of the dryer only by observing the gas discharge amount. Therefore, in the present invention, the drying efficiency is optimized by using both the exhaust gas temperature and the internal pressure of the thermal drying apparatus as indicators of control.

The forming step (S5) is a step of press-molding the secondary dried mixture to form a fuel coal, and includes a primary forming step (S51) and a secondary forming step (S52). First, the secondary dried mixture is put into a molding machine and dried and molded using heat of compression and friction heat of 100 to 130° C. generated through the compression process to form a primary fuel coal, a primary molding step (S51) is performed.

This primary forming step (S51) is a primary temporary forming process for forming the fuel coal, and some moisture contained in the secondary dried mixture is evaporated while taking the shape of the fuel coal. At this time, the primary molded fuel coal is in a softer state than the secondary molded fuel coal to be described later.

In this way, when the primary fuel coal is molded, the primary fuel coal is put back into the molding machine and dried and molded using the compression heat and friction heat of 130 to 160° C. generated through the high-pressure compression process to form secondary fuel coal. Step S52 is included.

In the above, the secondary fuel coal can be used immediately for fuel, and is drier than the primary coal coal to prevent cracks or damage during handling, and has high strength due to high cohesion.

In particular, as the air in the primary fuel coal mixture is completely exhausted by compression at 160° C. under high pressure, that is, the secondary fuel coal is molded to have a high density, so that it can be stably burned for a long time.

< Sludge fuel coal manufacturing system >

In another aspect of the present invention, the sludge fuel coal production system includes a pre-treatment device (1) for controlling the moisture content of raw materials including mushroom waste medium, rice husk and sewage sludge; a mixer 10 for mixing the pre-treated raw materials; a bio-drying device (20, 30) for controlling the air supply amount to first dry the raw material mixture to have a first moisture content; a thermal drying device (40, 50) for controlling the temperature and gas discharge of supplied steam to secondary-dry the primary dried mixture to have a 22nd moisture content lower than the first moisture content; And it is configured to include a molding machine 60 for forming a fuel coal by press-molding the secondary dried mixture. In addition, the sludge coal production system is configured to further include a dust collector 70 , a purifier 80 , and a dust collection pipe 90 .

Here, in FIG. 2 and the following drawings, only the necessary components are described in describing the invention, and devices such as a hopper for storage, a boiler for heating, a steam pipe, an air pump, and a hoist may be added when the actual system is built. . However, the omitted configuration is matters that can be easily selected and applied by those skilled in the art, and does not mean that the configuration not described is an unnecessary configuration.

2 schematically shows the device configuration of a system in which sludge fuel coal production is performed according to the present invention.

The pretreatment device 1 is a device for controlling the moisture content of the raw material, and there is no limitation in its configuration. For example, it may be a device for increasing the moisture content by injecting solids or sawdust or supplying hot air to lower the moisture content or spray water to increase the moisture content in the process of transferring to a conveyor belt. The pretreatment device 1 may be configured as a single device to sequentially supply the raw materials to the mixer 10 , or may be configured in plurality to supply the raw materials to the mixer 10 at the same time. In the case of a single device, it takes time until one raw material is pre-treated and put into the mixer, and then it takes time until the remaining raw materials are pre-treated and put into the mixer. It is better to be put in at the same time.

The mixer 10 is a device for generating a stirred-mixed raw material mixture by kneading or kneading when the raw materials each pre-treated in the pre-treatment device are input, and the raw material mixture can be continuously supplied to the bio-drying device for primary drying. .

Here, because the mixing is not smooth due to the aggregation of sewage sludge and the floating phenomenon caused by the small density of the mushroom waste medium and rice husks, the mixer not only makes the maximum contact with the particles of the mixed raw materials, but also eliminates the aggregation of the sewage sludge to facilitate mixing. make it happen By this mixer, the mixing rate and mixing uniformity of the raw material mixture are further increased, and the size of the mixed particles is small and uniformly formed.

To this end, the mixer may be provided with a mixing means in a form that can be kneaded while mixing the raw material mixture inside the container. The mixing means may have a screw-shaped blade continuously formed on the shaft, or a plurality of paddles may be used.

The bio-drying device (20, 30) improves the fermentation efficiency of microorganisms present in the sewage sludge and efficiently removes moisture evaporated by the heat of fermentation decomposition while inducing eco-friendly drying (S3) To perform a first drying step (S3) As a means, it includes a first drum dryer, which is a means for inducing rotation to secure voids while maintaining the composition of the input raw material mixture.

Specifically, the bio-drying apparatus includes: a first drum formed in the shape of one long pipe in one direction, a space provided therein, and a stirring means provided therein so that the raw material mixture is input and fermented and dried; a mantle part including a first mantle part and a second mantle part to which the first drum is rotatably coupled to both ends of the first drum; a driving unit for rotating the first drum; and an air supply unit connected to an air supply unit and disposed inside the first drum through the mantle unit to supply air to the interior of the first drum.

At this time, the first drum is divided into a plurality of sections including a front portion into which the raw material mixture is input, a rear portion through which the primary dried mixture is discharged, and a middle portion between the front portion and the rear portion, and the inner surface of the first drum In, the stirring means is installed in the front and the middle, and the stirring means is not installed in the rear part, so that the moving speed becomes slower as the raw material mixture proceeds from the front to the rear.

3 to 7 are exemplary views showing the bio-drying apparatus in more detail, FIG. 3 is a plan view schematically illustrating the internal and external configuration of the bio-drying apparatus, and FIG. 4 is a schematic view of a configuration different from that of FIG. It is an example view of the side indicated by . Also, FIG. 5 is an exemplary view showing the front part and the central part of the bio-drying apparatus viewed from the direction A of FIG. 3 , and FIG. 6 is a view showing the first mantle part from the direction B of FIG. 3 . It is one example diagram. In addition, FIG. 7 is an exemplary view showing a spiral configured in all of the bio-drying apparatus.

The bio-drying device adjusts the amount of air supplied by adjusting the rotation speed of the blower fan according to the control command of the control means. If the air supply amount is too large, it is advantageous to discharge the internal air containing moisture, but the internal temperature of the bio-drying device becomes too low, which prevents the decomposition of organic components. Although it is advantageous for the decomposition of organic components, it is important to maintain an appropriate supply because the smooth discharge of internal air containing moisture is not achieved.

When the raw material mixture is supplied to the upstream side of the bio-drying device, the internal temperature rises as the bio-drying process progresses toward the downstream side, and accordingly, the amount of water vapor evaporated at the downstream side increases. At this time, if air is supplied to the upstream side along with the raw material mixture, as it goes to the downstream side, the amount of water vapor already contained therein increases to include water vapor evaporated from the downstream side. This water vapor reaches a supersaturated state and is condensed again and dried at the downstream side. There is a problem that the efficiency decreases.

The bio-drying device according to an embodiment of the present invention is a device in which the direction in which the raw material mixture is supplied and discharged and the direction in which the air is supplied and discharged are reversed, and the supplied dry, low-temperature air is in contact with the discharged raw material mixture. This can prevent condensation and minimize the decrease in drying efficiency on the downstream side.

3 to 7 , the bio-drying apparatus 20 and 30 includes a first drum 23 , mantles 21 and 22 , driving units 24 : 24a and 24b , and an air supply unit 28 . is composed by

The first drum 23 forms a space for primary drying of the raw material mixture together with the mantle parts 21 and 22 and serves to blend the raw material mixture. Specifically, the first drum 23 is formed in the shape of one long pipe in one direction, and the first mantle part 21 and the second mantle part 22 are coupled to the front opening and the rear opening, respectively, so that the front opening and the rear opening are respectively connected. is closed The raw material mixture is fed into the first drum 23 through the first mantle part 21 , air is discharged, and the dried raw material mixture is discharged through the second mantle part 22 . A means for crushing, blending, and transporting the raw material mixture is provided inside the first drum 23, and the means for crushing, blending, and transporting the raw material mixture is fixedly installed on the first drum 23 and the first drum 23 The raw material mixture is crushed, blended, and transported by the rotation of the To this end, a driving unit 24 for rotating the first drum 23 is coupled to the outside of the first drum 23 . Basically, the first drum 23 is blended by dropping the raw material mixture while continuously rotating in one direction to induce contact with air and prevent agglomeration and coagulation between particles.

The first drum 23 may be divided into three sections: a front portion 23a, a middle portion 23b, and a rear portion 23c. Here, the sections are for convenience of explanation and do not necessarily have to be divided as described above. However, as will be described below, in each section, the moving speed of the raw material mixture is different, and each section is divided according to the moving speed. That is, the bio-drying apparatus of the present invention changes the moving speed of the raw material mixture in the first drum where drying is performed to achieve optimum drying efficiency. This change in moving speed is achieved by stirring means such as a spiral 25 and a lift blade 27 in contact with the raw material mixture therein, and in the present invention, the first drum 23 is installed in a parallel state without inclination. will use

In detail, the raw material mixture having a high moisture content is fed to the front part 23a of the first drum 23 through the first mantle part 21 . The raw material mixture having a high moisture content has high viscosity due to the moisture content and is adhered to and fixed inside the first drum 23 , and forms a lump between the raw material mixtures. Therefore, in the front (23a), the moisture content is rapidly reduced, the raw material mixture in the form of a lump is crushed, and the rapid transport and stirring are made. To this end, the front (23a) is provided with a stirring means including a spiral (25) and a wire (26).

It serves to raise the raw material mixture by the rotation of the first drum 23 of the spiral 25 and to move rapidly toward the central part 23b when falling. To this end, the spiral 25 is arranged so that a plurality of blades form a spiral inside the first drum 23 and serves to move the raw material mixture fed into the front part 23a backward, and this operation is performed to lift ( It is carried out by the lift & fall process.

The wire 26 is installed to cross the inside of the first drum 23 by connecting two points of the inner wall of the first drum 23 . A plurality of these wires 26 are installed, and one end and the other end of the wire 26 are shifted from each other and coupled to the inside of the first drum 23 . That is, one end is coupled to the front of the front (23a), the other end is coupled to the inner wall of the first drum (23) by retreating in the direction of the central portion (23b) compared to the other end. At this time, the wire 26 is installed to pass through the center of the cross-section of the first drum (23). Accordingly, when a plurality of wires 26 are installed, they are radially arranged with respect to the center of the cross-section as shown in FIG. 5 , and when viewed from the side, the wires 26 are arranged to meander and cross each other.

The wire 26 causes primary blending by allowing the raw material mixture lifted and widened by the spiral 25 to be divided and crushed by contact with the wire 26 when falling. This wire 26 serves to pulverize the agglomeration of the raw material mixture, which has strong initial viscosity but has low mechanical strength, so that the raw material mixture is maintained in small particles, and By increasing the contact rate of

A plurality of lift blades 27 are provided in the central portion 23b of the first drum 23 . The lift blades 27 are provided with a plurality of blade blades at regular intervals parallel to the longitudinal direction of the first drum 23 (the direction connecting the first mantle portion and the second mantle portion) (direction orthogonal to the cross-sectional direction). do. As shown, a plurality of lift blades 27 are installed in the circumferential direction to constitute one row, and these blade rows are installed throughout the central portion 23b at regular intervals.

The lift blade 27 serves to lift and fall of the raw material mixture transferred from the front 23a and serves to transfer it backward at a very slow speed. To this end, as shown in FIG. 5 , the blade end of the lift blade 27 may be bent at a predetermined angle (eg, 120 degrees to 140 degrees) so that a large amount of the raw material mixture can be lifted. This bending portion may be determined in a region that does not exceed half of the length of the lift blade 27 .

In addition, the raw material mixture may be arranged obliquely at an angle within several degrees in parallel with the longitudinal direction so that the raw material mixture can move in the rear 23c direction at a very slow speed in the first drum 23 . That is, as shown in FIG. 3 , the lift blade 27 is arranged in parallel with the longitudinal direction L and the blade, and at this time, may be coupled in the first drum 23 so as to be oblique with respect to the line connecting the longitudinal direction L. . That is, it is obliquely arranged in such a shape so that the raw material mixture can be moved backward little by little in the process of lifting or dropping it. Through this, it is possible to move the raw material mixture at a very slow speed in the middle part 23b compared to the front part 23a, and it is possible to increase the contact time with air. In particular, when moving at a high speed, the efficiency of using the inner space of the first drum 23 is reduced, but due to the movement at a slow speed, the raw material mixture can be sufficiently filled in the first drum to prevent a decrease in efficiency. there will be

On the other hand, agitating means such as a lift blade 27 for mixing or lifting the raw material mixture is not installed in the rear portion 23c of the first drum 23 . The length of the rear part 23c can be variously changed depending on the amount of the raw material mixture to be dried, the diameter and length of the first drum 23, and the moving speed of the raw material mixture, but about 1/4 to 1/6 of the total length can be determined by the length of

The raw material mixture dried in the middle part 23b is transferred to the rear part 23c. At this time, since the blade lift for transfer is not installed, the accumulated state is maintained, and the accumulated raw material mixture acts as an obstacle to the raw material mixture passing through the central part 23b. That is, the movement in the rear part 23c is made while the raw material mixture accumulated in the rear part 23c is pushed out according to the transfer of the raw material mixture dried in the middle part 23b. The moving speed of the raw material mixture moving in the central part 23b is lowered by the raw material mixture accumulated in the rear part 23c, and through this, the filling rate inside the first drum 23, that is, the first drum 23 is present inside The amount of raw material mixture used will increase. That is, the raw material mixture stays inside the first drum 23 for a long time, and the contact between the raw material mixture in which a large amount of microorganisms is present and the raw material mixture in which relatively few microorganisms exist increases to prevent a decrease in drying efficiency, It is possible to increase the utilization rate of the inner space of the first drum 23 .

The raw material mixture accumulated in the rear part 23c is gradually pushed out and moved to the second mantle part 22 , and a transfer means connected to the second mantle part 22 or a connector provided in the second mantle part 22 . (36) is discharged to the outside.

The mantle parts 21 and 22 are provided to seal the front and rear openings of the first drum 23 and to connect the inside and the outside of the first drum 23 . To this end, the mantle parts 21 and 22 are configured to include the first mantle part 21 and the second mantle part 22 .

The first mantle part 21 is coupled to the front part 23a side opening. The first mantle part 21 is provided with an inlet 30 , and the raw material mixture is introduced from the mixer 10 . In particular, the discharge pipe 31 to which the dust collection pipe 90 is connected may be provided in the first mantle part 21 . The discharge pipe 31 is connected to the inlet 30 pipe so that the air inside the first drum 23 discharged through the inlet 30 pipe can move to the dust collector 70 through the dust collecting pipe. To this end, the discharge pipe 31 is coupled to the opening formed at the upper end of the inlet (30). On the other hand, one end of the discharge pipe 31, that is, a portion exposed to the inside of the first drum 23 is provided with a dust outlet 29.

This dust outlet 29 is formed in a tubular shape communicating with the inlet 30, in a direction perpendicular to the inlet 30, and the upper end of the first drum (here, the upper end means the far side from the ground). is installed The suction part of the dust outlet 29 protrudes into the first drum as shown, and the lower part (part facing the floor) is formed to be inclined. This lower part is communicated, and internal air is sucked into the dust outlet 29 through the lower part. A sieve for restricting that the dust inside the first drum 23 is discharged through the dust outlet 29 may be provided at the lower portion thereof.

Meanwhile, the dust outlet 29 and the discharge pipe 31 may be connected through the inlet 30 , but a connection pipe connecting the dust outlet 29 and the discharge pipe 31 may be provided in the inlet 30 . However, when the amount of the mixture discharged through the discharge pipe 31 is sufficient, and the discharge port of the mixture provided in the discharge pipe 31 is formed toward the bottom of the discharge pipe 31, the connection pipe is omitted and the discharge pipe 31 By using the upper space of the dust outlet 29 and the discharge pipe 31 can be in communication.

The second mantle portion 22 is coupled to the rear portion 23c side opening of the first drum 23 . When the connector 36 is provided in the second mantle part 22 , the primary dried mixture is discharged through the connector 36 . A hopper or conveyor is connected to the connector 36 to transfer the raw material mixture to the intermediate storage tank or the thermoelectric drying device 50 .

In addition, an air supply pipe 28 is installed through the second mantle part 22 . More specifically, a plurality of air supply pipes 28 are assembled in the second mantle portion 22 , and the assembly portion 35 is connected to an air supply to supply air to the inside of the first drum 23 .

The driving unit 24 rotates the first drum 23 in contact with the outside of the first drum 23 . To this end, the first drum 23 is configured to include a wheel 32 rotating in contact with the surface, and a driving device 33 providing a driving force to the wheel 32 . One or more of these driving units 24 are installed to rotate the first drum 23 as shown in FIGS. 3 and 4 .

The air supply unit 28 supplies air for drying and microbial activity inside the first drum 23 . This air supply unit 28 is connected by one pipe connected to an air supply unit (not shown, for example, a blower) and an assembling unit 35 , and a plurality of air supply pipes 28a and 28b by the assembling unit 35 . , 28c) and installed inside the first drum 23 .

In particular, the air supply pipes (28a, 28b, 28c) are formed in different lengths are provided so that the air nozzles are located in different parts of the first drum (23). As shown, one air supply pipe is provided to supply air to the boundary between the front 23a and the central 23b, the other to the center of the central 23b, and the other to the boundary between the central 23b and the rear 23c. can be provided.

Through this, it is possible to maintain the activity of the microorganisms in a high state by continuously supplying air containing oxygen to the microorganisms at each position of the first drum 23 . In addition, by lowering the humidity at each location, quick drying can be achieved. In addition, air passes in the opposite direction to the passage direction of the raw material mixture in the bio-drying apparatus and is continuously discharged through the discharge pipe 31 provided on the upstream side of the bio-drying apparatus.

In the bio-drying apparatus having the above configuration, a non-rotating sludge wall is formed in the second half of the first drum to prevent sludge accumulation. As a result, the sludge is stirred evenly and the space is kept constant, so that the filling ratio of the raw material mixture inside the dryer rises to 50% or more.

The thermal drying apparatus can be configured to be continuous input and continuous discharge like the bio-drying apparatus, but in this case, the size of the thermal drying apparatus increases and the drying efficiency decreases. A method of drying the entire input amount of the primary dried mixture to the second moisture content, which is the target moisture content, and discharging all of the secondary dried mixture produced after drying is complete, can be used so that the primary dried mixture is added again. have.

Therefore, an intermediate storage tank in which the primary dried mixture discharged from the bio-drying apparatus is primarily stored may be provided between the bio-drying apparatus and the thermal drying apparatus, but the present invention is not limited thereto.

The thermal drying devices 40 and 50 are devices for secondary drying the primary dried mixture to have a second moisture content lower than the first moisture content by controlling the temperature and gas discharge of supplied steam. It is an indirect heating device including a pipe-shaped shaft through which steam supplied from the outside is distributed, and a plurality of disks coupled to an outer circumferential surface of the shaft at predetermined intervals.

Specifically, a second drum formed long in the longitudinal direction horizontal to the ground, the primary dried mixture is put through an inlet provided at one end in the longitudinal direction, and an outlet for discharging the secondary dried mixture is provided at the other end; a support frame coupled to both ends in the longitudinal direction to support the second drum; a pipe-shaped shaft passing through the second drum and disposed in the longitudinal direction, both ends being coupled to the support frame and having an inner space through which steam supplied from the outside flows; It is disposed inside the second drum and a plurality of disks coupled to the shaft at predetermined intervals; is configured to include.

The disk is composed of a pair of ring-shaped disks, the inner periphery coupled to the shaft is spaced apart, the outer periphery is bonded to each other disk body to form a space therein; and a disk wing formed of a ring-shaped disk and coupled to an outer edge of the disk body.

8 to 13 are exemplary views illustrating the thermal drying apparatus of FIG. 2 in more detail. FIG. 8 is a schematic side projection view illustrating the thermal drying apparatus according to the present invention, and FIG. 9 is an internal disk assembly It is an exemplary diagram showing the structure in more detail. And FIG. 10 is an exemplary view showing the disk viewed from the side, and FIGS. 11 to 13 are perspective views showing partial cross-sections of the disk.

8 to 11 , the thermal drying apparatus according to the present invention includes a second drum 43 , a disk assembly 50 provided inside the second drum 43 , and a steam supply means 48 . do.

The second drum 43 forms a space for secondary drying of the primary dried mixture, and heat supply means for secondary drying and a means for mixing the mixture are provided. Specifically, the second drum 43 is formed in the shape of a long cylindrical pipe in one direction. Hereinafter, this direction will be defined as the longitudinal direction (L). Here, it is formed in the shape of a cylindrical pipe, but a space protruding with a constant width and height along the longitudinal direction may be provided at the upper portion for collecting dust and moisture. In addition, an inlet 44 is provided at one end of the second drum 43 in the longitudinal direction (L), and an outlet 45 is provided at the other end so that the input of the primary dried mixture and the discharge of the secondary dried mixture are performed. is done To this end, an input device 41 for introducing the primary dried mixture into the second drum 43 is connected to the inlet 44 , and an ejector 42 for supplying the dry mixture to the rear end is connected to the outlet 45 . do.

In addition, separately from the inlet 44 and the outlet 45, the second drum 43 is provided with an exhaust port 46 connected to the dust collecting pipe 90 to discharge dust and moisture. The exhaust port 46 is formed in the protruding space when the protruding space is provided as described above.

Support frames (47: 47a, 47b) are provided at both ends of the second drum (43) in the longitudinal direction. The support frame 47 fixes and supports the second drum 43 on the ground. In addition, the support frame 47 is coupled to the shaft 51 to support the disk assembly 50 . At this time, the support frame 47 is coupled to the shaft 51 by a bearing means so that the shaft 51 is rotatable. In addition, both ends of the shaft 51 are coupled to the support frame 47 through the support frame 47 .

A disk assembly 50 for heating and mixing of the primary dried mixture is provided inside the second drum 43, and steam supply means for rotation of the disk assembly 50 and supply of the heated fluid ( 48) is provided.

The steam supply means 48 supplies a heated fluid for heating the primary dried mixture inside the second drum 43 . Hereinafter, it is assumed that the heated fluid is high-temperature steam, and the description will proceed. However, the present invention is not limited thereto, and the present invention is not limited only by suggesting that a high-temperature liquid such as heated water or oil may be used.

Steam is generated in a separate heating device and supplied through a pipe. Here, the pipe includes a supply pipe for supplying steam to the shaft 51 and a recovery pipe for recovering the steam that has passed through the shaft 51 . In order to supply this steam to the shaft 51 provided in the disk assembly 50, a steam inlet 48a and a steam outlet 48b are provided at both ends of the second drum 43 in the longitudinal direction. The steam inlet 48a and the steam outlet 48b connect the rotating shaft 51 and the fixed pipe, so that the steam supplied from the pipe passes through the shaft 51 and is recovered through the pipe again. connect To this end, the steam inlet 48a and the steam outlet 48b are respectively coupled to both ends of the shaft 51 exposed through the support frame 47 . Since this type of connection method uses a structure and confidentiality maintenance method through known techniques, a detailed description thereof will be omitted for the present invention.

The disk assembly 50 is installed on the second drum 43 and dried by heating the primarily dried mixture by steam supplied from the outside. To this end, the disk assembly 50 includes a shaft 51 , a disk 52 , a paddle 53 , and a mixing blade 57 installed inside the second drum 43 . In addition, a pulley 49 or a gear connected to a driving device (not shown) such as a motor for rotation of the shaft 51 is provided at one end of the shaft 51 .

The shaft 51 is installed inside the second drum 43, is coupled to the disk 52, transfers thermal energy supplied in the form of steam to the disk 52, and rotates by external power to rotate the disk 52. rotate the To this end, the shaft 51 is formed in the shape of a hollow cylindrical pipe, and both ends pass through the second drum 43 and the support frame 47 and are coupled to the support frame 47 . In addition, both ends of the shaft 51 are connected to a steam inlet (48a) and a steam outlet (48b) relaying the connection with the pipe. A plurality of disks 52 are coupled to the shaft 51 at predetermined intervals. In addition, one or more steam distribution holes 97 for the distribution of steam are formed in the shaft 51 at a portion to which the disk 52 is coupled, in the inner space 96 of the disk 52 . Through this, the shaft 51 directly transfers the heat by the steam to the disk 52 by conduction, and also directs the steam into the disk 52 through the steam distribution hole 97 so that as much heat as possible is mixed to be transmitted to

The disk 52 is formed in a ring shape so that the inner periphery wraps around the outer periphery of the shaft 51 and is coupled, and directly contacts the first dried mixture to heat it. In addition, the disk 52 rotates in synchronization with the rotation of the shaft 51 to rotate the mixing paddle 53 and the mixing blade 57 provided at the end of the disk 52 to remix and crush the mixture, and the length to be transported in the direction

The disk 52 is composed of a disk body 54 and a disk wing 55 .

The disk body 54 has a space formed therein, and the disk wings 55 are formed or coupled along the circumference. Specifically, the disk body 54 is formed of a pair of ring-shaped disks, and one end coupled to the shaft 51 of the disk is spaced apart from each other at a specific interval and coupled to the shaft 51 , respectively. And, the other end of the disk is joined to each other so that the cross-sectional shape of the half of the disk body 54 is configured to be a triangle. Steam supplied from the shaft 51 through the steam distribution hole 97 is injected into the inner space 96 of the disk body 54 .

The disk wing 55 is coupled to the outer edge of the disk body 54 and is formed in a plate-shaped ring shape. The disk wing 55 receives heat from the disk body 54 to increase the contact area. In addition, a plurality of transfer holes 56 for transferring the mixture are formed in the disk wing 55 at regular intervals. Specifically, the distance between the outer boundary of the disk wing 55 and the inner surface of the second drum 43 is determined to the extent that the disk 52 does not cause friction with the inner surface of the second drum 43 . In this case, the mixture between the neighboring disks 52 cannot move. Therefore, a plurality of transfer holes 56 are formed in the disk wing 55 so that the mixture can move to an adjacent space when the mixture is mixed by its own weight, mixing paddles, and mixing blades.

Meanwhile, the mixing paddle 53 and the mixing blade 57 are coupled to the disk wing 55 .

The mixing paddle 53 is coupled to the shaft 51 and serves to agitate the mixture between neighboring disks 52 . For this purpose, the mixing paddles 53 are connected to both sides of the neighboring disks 52 . These mixing paddles 53 are coupled between neighboring disks 52 so that their faces are parallel to the diameter of the disks 52 . One or more mixing paddles 53 are installed on a pair of disks 52 , and when a plurality of mixing paddles 53 are installed, they are installed to be spaced apart from each other at specific intervals. In addition, adjacent mixing paddles 53 are also arranged to be spaced apart from each other by a specific angle. That is, as shown in FIG. 9 , the mixing paddle coupled between the first disk and the second disk and the mixing paddle coupled between the second disk and the third disk are spaced apart.

In the present invention, an example in which the neighboring mixing paddles 53 are arranged to form a right angle when viewed at 90 degrees, that is, the disk 52 from one end of the shaft 51 is shown. However, these angles can be changed, and the present invention is not limited to the drawings.

Meanwhile, the end of the mixing paddle 53 protrudes from the outer periphery of the disk wing 55 and is coupled to the disk 52 so as to be closer to the inner surface of the second drum 43 . Through this, the mixture adhering to the inner surface of the second drum 43 can be scraped off, and the mixture moves through the gap between the disk 52 and the inner surface of the second drum 43 to move the space between the disks 52 . available to be The length of the mixing paddle 53, that is, the length of the portion in contact with the disk 52, is advantageous in terms of convenience of installation and manufacturing, but it is advantageous in terms of convenience of installation and manufacturing to be formed to be narrower than the width of the wing 55, but the disk body 54 part It is also possible to extend it to

One or more mixing blades 57 are coupled to the edge of the disk 52 . The mixing blade 57 serves to scrape the mixture between the disk 52 and the inner surface of the second drum 43 while mixing, crushing and pushing the agglomerated mixture into the space between the disks. To this end, the mixing blade 57 may be composed of a blade 58 and a breaker 59 .

The blade 58 is formed in a plate shape, and is coupled to the edge of the disk 52 . At this time, the blade 58 is coupled to the disk 52 so that the surface of the blade 58 intersects in a direction perpendicular to the surface of the disk. Then, a breaker 59 is formed on the surface on the rotational direction side.

The breaker 59 is formed to protrude from the surface of the blade 58, and is formed at an angle. Through this, the mixture that is agglomerated or adhered to the inner surface of the second drum may be crushed and separated from the inner surface of the second drum. In addition, one or more breakers 59 may also be formed in the mixing paddle 53 .

The mixing blade 57 may be coupled to the edge of the disc wing 55 , or may be coupled to the disc body 54 in which the disc wing 55 is omitted instead of the disc wing 55 . Also, like the mixing paddle 53 , the mixing blade 57 may also be coupled to be shifted so that the coupling positions between adjacent disks are different.

Meanwhile, FIGS. 12 and 13 show other examples of the disk.

12 and 13 , the disk 52 receives heat through steam supplied through the shaft 51 and serves to heat the mixture inside the second drum 43 . In this case, the surface of the shaft 51 may also serve to heat the mixture in contact with the mixture, but the contact frequency is small and the contact area is small even if the contact frequency is low, so that the thermal efficiency is lowered. Therefore, the disk 52 is used to increase the contact area to improve thermal efficiency.

This thermal efficiency is directly related to the contact area. Therefore, a method of increasing the surface area of the disk 52 to increase the chance of contact between the mixture and the disk is required. To this end, irregularities 96 (96a, 96b) may be formed on the surface of the disk 52 . As exemplarily shown in FIGS. 12 and 13 , the irregularities 96 may be formed by making the surface convex, and for this, the surface area due to the irregularities without increasing the weight by pressing the plate-shaped disk to form the irregularities 96 . can increase

As an example, as shown in FIGS. 12 and 13 , the radial unevenness 96a around the shaft 51 and the unevenness 96b in the form of concentric circles with respect to the shaft 51 may be formed. In addition, irregularities may be provided in various forms, such as forming irregularities in a box or polygonal shape on the surface.

In particular, it is also possible to use the irregularities for the same purpose as a blade by forming a shape in which the height in the rotation direction is higher and the height of the continuous portion is gradually lowered. In addition, it is also possible to form a plurality of convex portions such as hemispheres in the form of embossing.

The thermal drying apparatus may optimize the drying performance by controlling the steam temperature by measuring the temperature of the exhaust gas and then controlling the gas emission by measuring the pressure inside the drying apparatus.

The molding machine 60 is a device capable of press-molding at a high pressure, and there is no limitation in configuration. For example, the molding machine 60 includes an injection tool for injection molding, a pressing unit for pressing the secondary dried mixture to the injection tool, and a supply unit for supplying the secondary dried mixture between the pressing unit and the injection mold. can be The molding machine 60 may be formed not only in the form of pellets, but also in the form of large-sized compressed coals such as briquettes or lightning bullets.

The dust collector 70 is provided to collect dust generated during pretreatment and mixing of raw materials such as sludge and rice husk. To this end, the dust collector 70 may be configured in a cyclone method using rotation and gravity. The dust collector 70 is connected to the dust collecting pipe 90 connected to each device, and serves to collect the dust collected through the dust collecting pipe 90 and store it in the storage unit so that it can be re-inserted. To this end, the dust collector 70 includes a supply unit receiving air mixed with dust, a dust collecting unit collecting dust, a first discharge unit discharging the dust collected by the dust collecting unit to the storage unit, and a second discharge unit discharging the air from which the dust is removed. It can consist of parts. The second discharge unit may be connected to the purifier 80 .

The purifier 80 is provided to remove fine particles contained in the air discharged from the dust collector 70 . To this end, the purifier 80 may be configured to include a filter for adsorption and filtering of fine powder. The purifier 80 discharges the air discharged from the dust collector 70 through the filter, and through this, the fine powder not collected by the dust collector 70 is removed to discharge the purified air.

Features, structures, effects, etc. exemplified in each of the above-described embodiments may be combined or modified for other embodiments by those of ordinary skill in the art to which the embodiments belong. Accordingly, the contents related to such combinations and modifications should be interpreted as being included in the scope of the present invention.

Claims (3)

With respect to the raw material comprising the mushroom waste medium, rice hull and sewage sludge, the sewage sludge is dried to a moisture content of 70% to 80% by weight, and the mushroom waste medium is dried to a moisture content of 50% to 60% by weight, the rice husk A pre-treatment step (S1) of wet treatment with a moisture content of 30% to 40%;
A mixing step (S2) of obtaining a raw material mixture by mixing 100 to 150 parts by weight of the dried mushroom waste medium and 30 to 50 parts by weight of the wet-treated rice husk with respect to 100 parts by weight of the dried sewage sludge;
a first drying step (S3) of primary drying the raw material mixture to have a first moisture content using a bio-drying device;
a second drying step (S4) of secondary drying the firstly dried mixture to have a second moisture content lower than the first moisture content using a thermal drying device; and
A molding step (S5) of forming a fuel coal by press-molding the secondary dried mixture;
In the first drying step (S3), in controlling the bio-drying device, after the primary control of adjusting the air supply amount according to the temperature change of the exhaust gas, the air supply amount according to the change in the CO ₂ concentration inside the device is adjusted 2 maintaining the first moisture content of the discharged primary dried mixture by repeating the routine including the difference control,
In the second drying step (S4), in controlling the thermal drying device, after the primary control of measuring the temperature of the exhaust gas and adjusting the temperature of the supplied steam, the pressure inside the device is measured to control the gas emission. maintaining the second moisture content of the discharged secondary dried mixture by repeating the routine including the difference control;
In the forming step (S5), the secondary dried mixture is put into a molding machine and dried and molded using compression heat and friction heat of 100 to 130° C. generated through the compression process to form a primary fuel coal ( S51) and a secondary molding step (S52) of re-injecting the primary fuel coal into the molding machine and drying and molding it using compression heat and friction heat of 130 to 160° C. generated through a high-pressure compression process to form secondary fuel coal. A method of manufacturing sludge fuel coal.
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