KR20080004637U - This RS high speed fermentation drying system. - Google Patents

Abstract

The present invention is a device for treating organic waste such as livestock waste, such as pig flour, manure, milk powder and food waste as raw material of organic compost as a raw material of organic compost, steam containing odor generated during the process of high-speed fermentation of organic waste is platinum catalyst Deodorization treatment by low-temperature combustion at 300 ~ 320 ℃ using eta, and addition of oxidation reaction heat generated by burning odor and gas in platinum catalyst Riacta to recover heat energy of exhaust gas containing many heat energy step by step By constructing a recyclable energy recycling system, it is possible to provide an organic waste treatment apparatus, which is capable of exhibiting excellent thermodynamic performance. The present invention can be expanded and applied to slaughter waste or high concentration of wastewater, wastewater and sewage sludge. When applied to the system for processing It relates to "high-speed yial S. fermented dry system" in Organic waste treatment unit characterized in that is configured to indicate a superior performance of the cost.

IAS High Speed Fermentation Drying System

Description

RS high speed fermentation drying system. {Omitted}

1 is a block diagram of the basic facilities of the organic waste treatment system according to the present invention

2 is a front perspective view of an organic waste treatment system main body according to the present invention;

3 is a perspective view of the main body of the organic waste treatment system according to the present invention.

Figure 4 is a perspective view of the left side of the organic waste treatment system main body according to the present invention.

5 is a perspective view of the right side of the organic waste treatment system main body according to the present invention.

6 is a water separator and air preheater piping diagram according to the present invention.

7 is a system diagram showing a step-by-step energy recycling process in an organic waste treatment apparatus according to an embodiment of the present invention.

8 is a perspective view of a plate heat exchange coil according to an embodiment of the present invention.

9 is a detailed view of an energy recycle system system unit according to an embodiment of the present invention.

10 is a detailed view of a treatment tank jacket according to an embodiment of the present invention.

11 is a detailed view of a heat exchange coil of a treatment tank jacket according to an embodiment of the present invention.

12 is a schematic diagram of a three-stage energy cycle system according to an embodiment of the present invention.

13 is a detailed view of a deodorization system according to another embodiment of the present invention.

※ Explanation of code about main part of drawing ※

01: High speed fermentation dryer 02: Conveyor for feeding 04: Shaft storage tank

06: Energy Recycling System Unit 07: Driving Driver 12: Air Preheater

14: water separator 30: platinum catalyst reactor 37: heating medium heating part

The present invention relates to an apparatus for treating organic waste, and more specifically, to livestock waste such as pig meal, manure, and manure, or organic waste such as food waste and sewage sludge in a high speed fermentation-drying process in a unit equipped with organic compost. It relates to a method of treating with raw materials.

In the case of the composting treatment facility, which is the most common treatment method of livestock manure among organic wastes, it is mixed with excipients such as sawdust or chaff, and then fermented in a fermentation chamber to produce compost.The leachate is generated to contaminate groundwater and soil. There are many difficulties due to the large amount of odor emissions.

Also, in the case of sewage treatment facilities such as sewage treatment facilities, livestock manure treatment requires large-scale facilities to treat only high concentration sewage discharged by solid-liquid separation and separate sludge from solid-liquid separation. Complete treatment is a direct determinant of animal productivity.

In addition, marine dumping, which was charged about 2.5 million tons per year, will be gradually discontinued in January 2007, and will be completely discontinued in 2012. Therefore, there is a huge disruption in the supply of subsidiary materials such as sawdust as well as facilities for further processing. Recycling livestock waste at high speed without the need for excipients and recycling it as a raw material for organic compost has been spotlighted as a waste treatment measure that is not only a new concept of recycling but also a comprehensive environmental management system.

In particular, since the removal of water is essential among the processes for treating organic waste, the mechanical treatment methods such as the high speed dryer and the high speed fermentation dryer have a large difference in the treatment cost depending on the enormous amount of thermal energy supply corresponding to the latent heat of evaporation of water. It can be an important factor in determining its effectiveness, and since the water vapor generated in the process contains a large amount of odors and gas streams, if it is released into the air as it is, it will cause serious environmental problems. As a matter of fact, devices and facilities for perfect treatment of odors and gases as well as waste treatment have been developed and developed steadily one after another, and other conventional organic waste treatment devices have been deodorized and generated according to the characteristics of equipment and equipment, respectively. Exhaust gas Adsorption, ozone oxidation method, biological treatment method using bio media, washing method using water booth, water cooling condensation system using cooling tower, rapid cooling method using refrigeration cycle, catalytic oxidation method There are treatment methods such as the above, and these treatment methods have their respective advantages and disadvantages. However, they have some effects depending on the method of application, but there is still a need for the improvement of the performance according to the model development and the steady research and development.

When treating organic wastes with mechanization facilities such as fermentation dryers, the largest share of the operating costs is the thermal energy cost for water removal and the operating cost for deodorization, which are the water vapor, odor and gas streams emitted from organic waste treatment facilities. If you ignore the maintenance cost among the deodorizing treatment method, the most effective method is the low-temperature combustion treatment method using catalytic reactor, and the odor and gas flow generated from waste treatment facility are about 900 ℃ ~ 1100 ℃ under normal circumstances. Complete oxidation (combustion) inside and outside, but when passing through a catalyst consisting of a honeycomb-like carrier coated with platinum, it is oxidized at a relatively low temperature of about 300 ℃ to 320 ℃ can almost completely deodorize effect It's an excellent way.

However, in order to heat 1CMM from about 65 ℃ to 75 ℃, it is about (1CMM × 60MIN) × 1.24 (standard specific gravity of air) × 0.24 (standard specific heat of air) × (300 ℃ -65 ℃) = 4,196 It is necessary to supply heat energy of ㎉ / HR and when using electric heater as energy source, 4,196 ㎉ / HR ÷ 860 ㎉ / HR = 4.9 ㎾ / HR. Because of the need for energy, the use of platinum catalyst Riacta requires a high cost of maintenance compared to its excellent deodorizing performance. If the preheating temperature is low due to insufficient capacity of the electric heater, deodorization may be insufficient due to incomplete oxidation or toxic gas may be generated. .

Therefore, even though the method of treating odor and gas flow using platinum catalyst Riacta is very excellent, the platinum catalyst carrier is very expensive and due to the high cost of maintenance, it is difficult to apply to deodorization equipment of organic waste treatment facilities. .

The purpose of the present invention is that although the platinum catalyst carrier is expensive but has a high performance effect, it can be manufactured in a very small size compared to the treatment capacity, and recovers the enormous amount of thermal energy possessed by most of the odor treated water vapor and gas in the catalytic reactor. Not only can it be used as a preheating energy of its own, but also it can recover the heat of oxidation reaction generated by the odor and gas flow at low temperature in the catalytic reactor and recycle it as the latent heat of evaporation and air preheating energy to remove the water in the treatment tank. It is to provide an organic waste treatment device that can exhibit excellent performance at low cost maintenance cost by configuring the energy recycling system of.

Another object of the present invention is that in the case of the equipment for fermentation drying treatment of organic waste at high speed, a large amount of water vapor is generated in a short time, so even if the complete deodorization treatment is discharged to the atmosphere as it is discharged in the air state as condensation in the atmosphere In this case, the high speed fermentation drying system of the present invention, since most of the water vapor is condensed through the energy recovery process in three stages, water is discharged to the condensed water state, and only the dehumidified air is discharged to the atmosphere. Therefore, to provide an organic waste treatment system that can exhibit energy efficiency and environmentally superior performance,

Another object of the present invention is that the odor can be inevitably generated during the introduction of waste into the organic waste treatment facility or the primary storage process, the hood is installed on the top of the odor generating portion and the air containing the odor is aerobic As it is used as air supply for oxygen for fermentation and catalytic combustion, odor can be effectively removed without a separate deodorization facility. Especially, in the place where a lot of odors occur, apply only "Energy Recycling System" to construct deodorization facility. It is to provide a high-efficiency odor treatment device by providing the air supply and exhaust.

Therefore, the "LS fast fermentation drying system" (01) of the present invention is a substance inside the treatment tank to ferment and dry organic waste at high speed while maintaining an optimal environment for the fermentation microorganism is activated and multiplied to achieve this purpose. Ribbon type stirring equipment (13), which is designed to stir before, after, left and right, is installed and the treatment tank of the twin structure that maximizes the heat transfer area compared to the contents to continuously supply the latent heat of evaporation of water (08) `` Container means '' consisting of

"Catalyst reactor means" composed of a platinum-based or palladium-based catalyst and composed of a catalytic reactor 30, an electric heating heater 29, and the like for low-temperature combustion oxidation of phase-change gas and odor at 300 to 320 ° C.

Multiple stage plate heat exchangers (23, 24, 25, 26, 27), electric heating heater (29) and catalytic reactor (30) are arranged in series and up to about 320 ° C above the catalytic reactor outlet centered on the catalytic reactor. Heated superheated steam (28) and steam (31) containing odor generated in the treatment tank are heat exchanged while passing in opposite flows, so that the enormous amount of thermal energy of the superheated steam at the catalytic reactor exit is recycled step by step. Saturated water vapor generated and introduced from the tank is introduced into the first stage heat exchanger (23) at the outlet temperature of about 110 to 120 캜, the second stage heat exchanger (24) at the outlet temperature of about 150 to 160 캜, and the third stage heat exchanger (25 ) Outlet temperature about 190 ~ 200 ℃, 4 stage heat exchanger 26 Outlet temperature about 230 ~ 240 ℃, 5 stage heat exchanger 27 Outlet temperature about 270 ~ 280 ℃ Way"

High pressure blower 15 for supplying the exhaust gas 35 discharged in the superheated steam of about 120 to 130 ° C. after the first stage energy recycling to the double jacket 20 of the treatment tank, and the latent heat of evaporation of moisture in the treatment tank. The treatment tank (08) of the double-jacket structure for supply, the heat energy of the superheated steam (35) flowing into the double-jacket at a temperature of about 120 ~ 130 ℃ after the first-stage energy recycling to the inside of the treatment tank "Two-stage energy recycling means" consisting of an energy cycle heat exchanger 36 installed in a structure that maximizes heat transfer efficiency for the purpose of supplying the latent heat by evaporation.

After the two-stage energy recycling, the heat exchange coil 16 for hot water heating is built for the purpose of preheating the air by recovering the thermal energy of the exhaust gas 42 including the condensed water and the saturated steam discharged to about 70 to 80 ° C. Water separator 14, the air preheater 12 for preheating the air supply using the hot water supplied from the heat exchange coil of the water separator, the hot water connecting the heat exchange coil 16 of the water separator and the heat exchange coil 17 of the air preheater "Three-stage energy recycling means" composed of circulation pipe 18 and hot water circulation pump 19, etc.

"Deodorization means" configured to treat the surrounding odors as the air supply supplied for aerobic fermentation and catalytic combustion of the catalytic reactor inside the treatment tank flows from hoppers or shaft storage tanks that generate a lot of odors.

For the purpose of operating while maintaining the environment inside the treatment tank at an optimum state at all times, the axial feed pump (03) is operated at a predetermined time interval about once every 30 minutes or once every hour for continuous operation of the appropriate amount of axial feed. Depending on the quantitative input method and the moisture content of the internal substance detected by the moisture content sensor, the water content of the treatment tank internal water exceeds a certain moisture content. The sensor input method is set in parallel, and it automatically inputs the appropriate amount of shaft powder automatically, and if necessary, it is configured to supply the shaft powder to the processing tank automatically and manually.

When the internal material becomes above a certain level by the quantitative discharge operation method and the material sensor, the discharge conveyor 05 is operated for a predetermined time at a set time once a day for the purpose of discharging the processed by-product that has been fermented and dried. The material sensor discharge method for discharging a certain amount of material is set in parallel. During automatic discharge, the material inside the treatment tank is set to maintain a certain level or more to maintain an optimal fermentation environment. "Measurement by-product discharge means" configured to discharge all or part of the material in tanks

In addition, it is to provide a "LS fast fermentation drying system" composed of "automatic control means" that all functions are controlled automatically.

Hereinafter, an embodiment of the present invention applied to a livestock waste treatment apparatus will be described in detail with reference to the accompanying drawings.

As shown in FIG. 1, the present invention is a "LS fast fermentation drying system" main body 01, a liquid livestock waste input pump 03, a sludge livestock waste input screw conveyor (02), by-products It is divided into a screw conveyor (05), an automatic control panel (10), a liquid livestock storage tank (04), and basic auxiliary equipment for discharging gas. It is the structure that the installation of planting facility for processing organic waste is completed.

[FIG. 2] [FIG. 3] [FIG. 4] [FIG. 5] of the present invention, the "LS fast fermentation drying system" of the present invention is the "energy recycling reactor system unit" on the upper part of the treatment plant main body 01. (Hereinafter, referred to as "LS unit") (06) is installed in the upper teeth type and the "LS high speed fermentation drying system" main body 01 is the outer body is formed by the outer case 51 and installed inside the case. Drive consisting of a double-jacketed twin structure, a ribbon type stirrer 13 for stirring the material in the processing tank, a reducer 07, a chain and a sprocket 50, etc. to drive the stirrer. High pressure blower for return to supply water vapor containing odor generated from the device and treatment tank to "ALS unit" (09) High pressure blower for supply to supply superheated steam discharged from "ALS unit" to jacket of processing tank (15) Jockey at the end of processing tank The air conditioner 12 and the air preheater 12 are disposed, a discharge conveyor 05 for discharging the fermented and dried by-products inside the treatment tank, an inspection port 81 for checking the inside of the treatment tank, and an automatic control panel ( 10) and so on

6 shows a piping diagram of the separator 14 and the air preheater 12. Inside the separator 14, a heat exchange coil 16 made of stainless steel pipes and stainless steel tubes is built in an antifreeze solution. The heat medium mixed with the distilled water is circulated, and the heat preheating coil 17 made of copper pipe and aluminum 휜 is built in the air preheater 12 to circulate the heat medium, and the hot water is heated in the separator. The heat exchange coil 16 and the heat exchange coil 17 for air supply preheating of the air preheater are connected by a pipe 18 and a circulation pump 19 to pass through the air preheater using the heat medium heated in the water separator while the heat medium is circulated. It is structured to preheat air supply.

7 is a process flow diagram illustrating a step-by-step treatment state and an energy cycle action state of water vapor including odor generated in an "LS fast fermentation drying system" according to an embodiment of the present invention. In order to maintain the optimum level at all times, the discharge conveyor (05) is automatically released from the upper level sensor (53) by using the electrode type moisture content sensor of patent No. 0325886 owned by the applicant. It is configured to discharge the internal substance by operating, and the discharge conveyor is automatically stopped at the lower level sensor 54. When the input is set to automatically input 1/24 part of the proper throughput every hour, the water content of the internal substance of the treatment tank And the environment can be operated in almost constant state, and the "ALS Fast Fermentation Drying System" is normally After a certain period of time, the internal temperature of the treatment tank 08 and the temperature of the substance are increased. At this time, gas is generated 21 together with water vapor. Saturated steam 31 including gas and odor is disposed in the upper exhaust chamber of the treatment tank. The high pressure blower 09, which is connected to the 56, enters the heat exchanger through the suction chamber 22 of the "RS unit".

The saturated steam 31 passes through the heat exchangers 23, 24, 25, 26, and 27 arranged in series, and is gradually stepped from the outlet 49 of the final heat exchanger 27 to about 270 to 280 ° C. In this case, the heating energy is a superheated steam 28 at the outlet of the catalytic reactor and does not need any additional heating energy. The heating energy passes through the electric heating heater 29 and is further heated by about 20 to 40 ° C., thereby heating to about 300 to 320 ° C. After that, the catalyst is supplied to the reactant unit 30.

Catalytic reactors are composed of platinum- or palladium-based honeycomb catalysts, and most of the phase change substances such as gases and odors contained in superheated steam heated to about 300 ° C to 320 ° C are almost oxidized while passing through the catalytic reactor unit. The heat of oxidation reaction is generated by conversion to carbon dioxide gas and steam, so the superheated steam at the exit of the catalytic reactor unit is heated to about 320 ° C. or more.

The superheated steam 28 heated to more than about 320 ° C. by the heat of oxidation in the catalytic reactor unit contains enormous amounts of thermal energy, and the heat exchangers 27, 26, 25, 24, 23 of the “AL unit” are replaced. As it passes back through, it flows in the form of counter current with saturated steam 31 introduced from the treatment tank, and heat energy is recycled in one step to heat saturated steam 31, which was about 65 to 75 ° C., to about 270 ° C. to 280 ° C. The remaining heat energy is in the superheated steam state of about 120 to 130 ° C and is introduced into the discharge chamber 32 of the "RS unit", and the double jacket 20 of the treatment tank constituted by the high-pressure blower 15 has a twin structure. Since the heat energy is recycled in two stages, it is condensed and discharged while being supplied as a necessary heat energy source by the latent heat of evaporation of water in the treatment tank, and the heat energy is recycled again in the separator 14 to provide an air preheater (1). In step 2), it is used as heat energy to preheat the air supply, thus forming a three-stage energy recycling system.

Referring to the drawings shown in more detail with respect to each configuration of the present invention.

FIG. 8 is a view illustrating a general plate heat exchanger. In the present invention, in order to achieve the principle object of the "RS unit", waste heat of the outlet side high temperature on the catalytic side of the inlet is The heat transfer capacity of the plate heat exchanger was applied as a heat conductor for recycling with preheating energy, and a corrosion resistant plate that can withstand high temperature and corrosion was used.

As shown in more detail in FIG. 9, the "LS unit" 06 is installed on the upper portion of the high speed fermentation dryer main body 01 in an upper configuration so as to constitute a one-stage energy recycling system (33). The outer body is formed by) and the inside of the case is a structure in which a plurality of plate heat exchangers (23, 24, 25, 26, 27), an electric heating heater (29) and a platinum catalyst reactor (30) are arranged in series. The inlet end is divided into the upper and lower parts by the partition, and is divided into the suction chamber 22 and the discharge chamber 32. The suction chamber 22 is generated from the treatment tank and supplied by the high pressure blower 09. The steam 31 is smoothly introduced and the discharge chamber 32 has a structure in which the superheated steam 35 is smoothly discharged from the "RS unit", and an electric heating heater 29 is provided at the rear end opposite to the chamber. And platinum or palladium A catalyst reactor 30 composed of a catalyst is installed.

The principle of catalytic combustion is to decompose phase-change substances such as odors and gases generated during fermentation and drying of livestock, and the general direct method requires high temperature environment of about 900 ~ 1100 ℃ for complete combustion. In the combustion method, it is almost oxidized at a low temperature of about 300 to 320 ° C and decomposed into CO2 and water vapor. Therefore, it is easy to recover the durability of the equipment due to the low operating temperature and to recover and recycle the heat of combustion reaction. It is a combustion treatment method and the role of the catalyst is to convert phase-change substances such as gas and odor into other odorless components, and to promote its function so that combustion and decomposition are possible even at low temperatures.

Generally, a platinum or palladium-based catalyst is widely used as a catalyst. A catalyst material such as platinum is coated on a geometrically large support, and a carrier is a gamma-type alumina having a large specific surface area such as honeycomb, pellet, In the present invention, it is used by molding into a shape such as a mesh structure type, and in the present invention, a catalytic reactor or pellet type catalyst in which honeycomb-shaped rectangular honeycomb catalysts are assembled in multiple stages with excellent ventilation, high processing gas volume and excellent performance will be used as a unit. .

The electric heater unit 29, which is installed for the purpose of increasing the combustion efficiency because the phase change gas preheated to about 270 to 280 ° C. and additionally heats about 20 to 40 ° C., is required after the initial preheating. It is installed at the inlet side of the reactor 30, and the general structure of the electric heater unit with the coil coil type electric heater of the proper capacity or the temperature is about 300 ℃ ~ 320 ℃. do.

The core of the present invention is to oxidatively decompose about 65 ° C to 75 ° C of water continuously produced in the treatment tank of a high-speed fermentation dryer, and to change the phase changeable substances such as gas and odor at low temperature in a catalytic environment using a catalytic reactor. Most of the heat energy for heating the temperature of the inlet gas 34 to about 300 ° C. to 320 ° C., which is an appropriate temperature, based on the catalytic reactor unit 30, is superheated at the outlet of the catalytic reactor without supplying external heat energy. ) Is to recycle and recycle the enormous amount of waste heat.

In addition, the temperature of the saturated steam 31, which was 65 ° C to 75 ° C in the inlet chamber 22 of the "ALS unit", was preheated through a one-stage energy recycling system in the outlet chamber 32 of the "ALS unit". After the recovery, the amplification is about 120 ° C. to 130 ° C. due to the heat of oxidation reaction and the additional preheating energy of the electric heater 29 generated during the low temperature combustion of the gas, odor, and phase change materials in the catalytic reactor unit 30. Since the heat energy is sufficient to constitute a two-stage energy cycle system, which is supplied back to the latent heat of evaporation inside the treatment tank through the jacket 20 of the fermentation dryer treatment tank, according to the material and characteristics of the plate heat exchanger and the catalytic reactor It is necessary to give the actual capacity to a special structure for the purpose of processing.

In the two-stage energy cycle system of the present invention, as shown in detail in FIG. 10, the outer wall of the high-speed fermentation dryer treatment tank has a double jacket 20, and the double jacket is an energy cycle heat exchange part 36 which is a heating part using waste heat energy. ) And the heat medium heating part (37), which is a heating part for initial preheating and auxiliary heating, and the heat energy of the exhaust air (35) of the "AL unit" supplied through the double jacket air supply port (58) is jacketed. The inner cylinder 39 supplies heat energy necessary for the treatment material 65 therein. In this case, the material inside the treatment tank is in a sludge state of high water content, while the energy source inside the double jacket is in a gaseous state. ) The heat transfer efficiency is significantly higher because the heat transfer efficiency inside the double jacket, which is outside the inner tube 39 of the treatment tank, is significantly lower than the surface where the treatment material 65 inside contacts. The energy cycle heat exchanger 36, which is a relatively low portion, needs to increase the heat transfer area as a method for improving heat exchange efficiency. As a solution for this, the stainless steel plate is formed on the outer double jacket side of the inner tank 39 of the treatment tank. Since the heat transfer fin 38 is attached at a pitch of about 3 to 10 mm, the heat transfer area 38 is configured to maximize the heat transfer area, and the heat medium oil is filled in the heat medium heating part 37 to be 120 to 130 ° C. by the electric heating heater 39. It is automatically controlled to maintain the temperature and is composed of a structure for supplying heat energy into the treatment tank by the high temperature heat medium oil naturally circulated by the temperature and specific gravity.

As shown in more detail in FIG. 11, the energy cycle heat exchanger 36 is divided into a partition 40 so that the exhaust gas flows reciprocally, and the chamber 41 in which the gas rotates to the lower end of the partition is joined stepwise. (64) Since it is formed as a V-shaped turning chamber by the heat transfer fin 38, the flow of gas circulating inside the heat exchange coil part is smoothly circulated. Since it supplies the necessary heat energy to the interior of the two-stage energy cycle system is gradually cooled and discharged through the exhaust port (63).

In the three-stage energy cycle system of the present invention, as shown in detail in FIG. 12, the gas 42 discharged through the exhaust port 63 of the treatment tank jacket heat exchange part is configured to be exhausted 43 through the water separator 14. The heat exchanger coil 16 for heating the medium is heated inside the water separator 14, and the heat exchanger coil 17 for supplying air is preheated inside the air preheater 12, and the two heat exchange coils are connected to the pipe 18. The inside is composed of a structure in which the heat medium in which the antifreeze and the distilled water are properly mixed is circulated through the circulation pump 19 to recover the thermal energy of the exhaust gas 42 passing through the water separator and supply it to the air preheater.

The "LS high speed fermentation drying system" of the present invention is to supply external air for the air supply necessary for aerobic fermentation and the low-temperature combustion in the catalytic reactor in the treatment tank, which is another object of the present invention odor For the purpose of removal, the air supply duct 44 connected to the treatment tank air supply unit 66 is connected to the upper end of the storage tank through the air preheater 12 from the upper end of the hopper or livestock waste storage tank 04 where odor is generated a lot. Since the air 45 is used as the air supply, the external tank 46 is supplied to the storage tank 04 so that the odor generating unit can be deodorized at the same time. In this case, a two-stage energy cycle system is used to obtain a heat source for preheating the air supply. The gas (42) discharged through the exhaust gas through the heat exchange coil (16) in the separator 14, the exhaust 43 and through the circulation pump 19 and the pipe 18 It is composed of a structure for preheating the outside air 45 supplied through the air preheater 12 by the heat energy transmitted through the heat medium is circulated by the sea.

In addition, as shown in detail in FIG. 13, when the separate energy cycle heat exchange system 67 is extended and configured at the upper end of the existing "LS unit" 78, the air 53 where odor is generated is generated. While deodorizing and exhausting 54, the deodorizing system can be configured to recycle energy to preheat the outside air 55 to supply air to the room 56.

In the pilot unit, saturated steam 31 introduced from the treatment tank 08 of the "LS fast fermentation drying system" through the suction chamber 22 of the "LS unit" (06) is operated when the fermentation dryer is operating normally. The temperature of about 65-75 degreeC was kept.

The pre-heating of the high-speed fermentation dryer is completed, and the average amount of saturated water vapor is about 320kg / hr based on 10 tons / 24hr capacity of organic waste with a water content of 90% in normal operation. The air supply for oxygen supply to the processing system is about 600 ㎥ It was about / hr and the cross-sectional area of heat exchange COIL passage was about 1.5 ~ 2.5 M / S.

In addition, the heat transfer capacity of heat exchange coil ΔT is the outlet temperature of the low temperature side air and the high temperature side air at the inlet temperature when the temperature difference between the inlet temperature of the low temperature side air and the high temperature side air where the saturated steam passes through the first stage of the heat exchange coil is about 80 ° C. The air volume and the wind speed were adjusted to exchange heat at an intermediate temperature, so that the saturated steam (31) flowing into the suction chamber, which is the low temperature side inlet of the "RS unit", was about 65-75 ° C and the high temperature side inlet. When the catalytic reactor outlet superheated steam 28 is above 320 ° C, the low temperature side inlet air 31 passes through the heat exchanger 23, 24, 25, 26, 27, 110-120 ° C ⇒ 150-160 ° C ⇒ 190 It is heated to ～ 200 ℃ ⇒ 230 ~ 240 ℃ ⇒ 270 ~ 280 ℃ and the high temperature side inlet air 28 passes through the heat exchanger 27, 26, 25, 24, 23, 280 ~ 290 ℃ ⇒ 240 ~ It means cooling to 250 ℃ ⇒ 200 ~ 210 ℃ ⇒ 160 ~ 170 ℃ ⇒ 120 ~ 130 ℃. To obtain a ΔT of about 200 ° C. between 65 ° C. and 75 ° C., the inlet temperature of the S unit ", between 270 ° C. and 270 ° C., the temperature of the air after the last heat exchanger 27 and the inlet temperature of the auxiliary electric heater unit 29. Since the heat exchanger is assembled into three to eight stages according to the air flow rate and the wind speed, the saturated water vapor 31 having about 65 to 75 ° C. flowing into the suction chamber 22 of the “AL unit” is fed to the catalytic reactor inlet 34. When reached to the auxiliary heater 29 was configured to be heated to about 300 ~ 320 ℃ due to the additional preheating.

When the high-speed fermentation drying system is started for the first time, the pre-heating is completed by operating with the shaft 52 containing a large amount of fiber and solid materials such as powder and flour to the shaft 52 of the stirrer 13 first. Since this high money is automatically injected by a certain amount every hour by the pump (03), it is configured to operate while maintaining the internal environment and moisture content at all times. Since the heat medium heating heater 39 is activated by the temperature sensor to supply the thermal energy to the preheating jacket 37 to increase the temperature of the material and after a while begins to generate gas and odor with a small amount of water vapor.

Therefore, when the "ALS unit" is also operated for the first time, only the air supply 67 is introduced into the suction chamber 22 together with a small amount of water vapor 21, so that the preheating is performed in the electric heating heater 29 after passing through the heat exchanger. Since the amount of water vapor and gas is small, it is preheated to about 250 ℃ or more by the heat energy of the heater alone, and the phase change materials such as gas and odor are burned and decomposed while passing through the catalytic reactor 30 to about 270 ~ 280 ℃ by the heat of oxidation reaction. As the energy is amplified and returned through the heat exchangers 27, 26, 25, 24, and 23, most of the thermal energy included is a one-stage energy cycle, and when the apparatus continues to operate, the heating medium in the treatment tank is heated by the auxiliary heater 39. When the temperature of the material gradually rises and the amount of water vapor generated increases, the amount of the phase change material treated in the catalytic reactor unit 30 increases with it. As the heat of oxidation increases, a large amount of thermal energy of the superheated steam 28 at the outlet of the catalytic reactor unit is used for catalytic combustion of the saturated steam 31 at the inlet of the "RS unit" circulated along the one-stage energy cycle system. As the energy for heating to the proper temperature is sufficiently recovered, the "AL unit" exit air temperature 35 is gradually raised as the preheating of the "AL unit" is gradually completed, resulting in a two-stage energy cycle and a three-stage energy cycle. Even if the preheating is sufficient and the energy cycle system system is configured as normal, the temperature of the material in the treatment tank suddenly rises at any moment, and the amount of water vapor is not increased abruptly but gradually increases steadily. Requires time, but handles once warmed up Without additional supply of latent heat of evaporation to remove moisture inside the tank, stable operation is possible only by supplying a small amount of auxiliary energy corresponding to the recycled internal energy and the heat dissipation loss.

Therefore, according to the "ESL high speed fermentation drying system" of the present invention generated in the treatment tank 08 of the high speed fermentation dryer in the fermentation drying at high speed in order to convert organic wastes such as nutrients or food waste into raw material of environmentally compost. In order to completely process the saturated water vapor 21 containing the phase change materials such as gas and odor, the energy cycle system is basically configured to recycle only the preheated energy and then recycle the input heat energy. Catalytic reactor system which can be oxidized and decomposed almost entirely with little energy at low temperature of about 300 ~ 320 ℃, but requires a high temperature environment of about 900 ~ 1100 ℃ for complete combustion. the generation were equipped with CO ₂ is fossil Since not generated by burning charge is biogas generated in the fermentation drying process and because it is carbon-neutral (CARBON NEUTRAL) no additional CO ₂ generation as well not be replaced in the Kyoto Protocol recovered from the oxidation reaction heat generated in the catalytic reactor unit It can be recycled, showing excellent performance for building low cost organic waste recycling systems.

Another effect of the present invention is to install a hood on the top of the nutrient storage tank or organic waste storage hopper that generates a lot of odors to prevent aerobic fermentation and catalytic combustion of the "AL unit in the" LS fast fermentation drying system "of the present invention In order to supply the necessary air supply in order to obtain the effect of removing the surrounding odor and another effect of the present invention is applied to the deodorization unit using the energy recycling system for the deodorization of the place where the odor occurs intensively low maintenance cost It is possible to construct an excellent "LS deodorizer" which can be operated.

Therefore, although the invention has been shown and described with respect to specific embodiments thereof, it will be apparent to those skilled in the art that various modifications and changes can be made without departing from the spirit and scope of the invention as indicated by the appended claims. Anyone can grow up easily.

Claims (20)

In fermentation drying at high speed to convert organic waste into environmentally friendly compost raw materials, the internal material of the fermentation dryer treatment tank 08 maintains an appropriate level while maintaining the environment for the high temperature aerobic fermentation microorganism to be activated and multiply. A ribbon type stirrer 13 is installed to stir the material to the front, back, left and right, and the double jacket 32 has a twin structure for supplying necessary heat energy by evaporative latent heat of moisture contained in the inner material. Container means consisting of treatment tanks Saturated water vapor 31 containing odor and gas generated in the treatment tank 08 of the high speed fermentation dryer is catalytically deodorized by the catalytic reactor 30 of the energy recycling system unit 06, and then deodorized. `` One-stage energy cycle system '' configured to recycle the thermal energy of the reactor outlet gas 28 and recycle it as catalytic combustion preheating energy. The superheated steam gas 35 discharged from the energy recycle reactor system unit (hereinafter referred to as "RS unit") after the first stage energy recycle is supplied to the double jacket 20 of the high speed fermentation dryer, thereby treating the process tank (08). Two-stage Energy Recycling System configured to supply latent heat of evaporation to vaporize moisture in materials After the two-stage energy cycle, the three-stage energy cycle system configured to recover the residual heat of the saturated humid air 42 discharged from the double jacket 20 of the high speed fermentation dryer and preheat the treatment tank air supply 67. Since the air supply for aerobic fermentation and catalytic combustion of the catalytic reactor inside the treatment tank flows from the primary storage hopper or the upper end portion 82 of the organic waste which generates a lot of odors, the odors of the surroundings are treated together. "Deodorization means" to say And organic waste high-speed fermentation drying system, characterized in that it consists of an "automatic control system" that all functions are automatically controlled. According to claim 1, wherein the "container means" is discharged from the upper level sensor 53 using the electrode type moisture content sensor in the applicant's patent No. 0325886 patent technology in order to maintain the proper capacity and the appropriate moisture content of the material inside the treatment tank (05), the lower level sensor (54) stops the discharge conveyor, and the processed material is configured to automatically input 1/24 part of the proper throughput per hour per hour, so that the water content of the internal material of the treatment tank during normal operation is 50 to 60%, temperature 65-75 ℃, the level of the material in the treatment tank is maintained at 50-70% of the capacity of the organic waste, characterized in that the high temperature aerobic fermentation microorganisms are activated while maintaining the optimum environment for growth High speed fermentation drying system. The treatment tank of the two-win structure is a means for supplying the latent heat of evaporation of moisture to the material 65 of the treatment tank of the high speed fermentation dryer by dividing the inside of the double jacket 20 in two and then recovering the waste heat. Energy cycle heat exchanger (36) consisting of a structure for supplying the interior of the treatment tank and the heating medium for the purpose of auxiliary heating for supplying the heating energy for the initial pre-heating operation and only the waste heat recovery in normal operation, the heating medium (37) The organic waste high-speed fermentation drying system, characterized in that the operation is operated while maintaining the optimum environment with only minimal heat energy. The "first stage energy cycle system" according to claim 1, wherein the saturation water vapor 21 containing odor and gas generated in the treatment tank during the normal operation of the `` ALS high speed fermentation drying system '' When oxidizing by low-temperature combustion in the catalytic reactor 30, it needs to be preheated to 300 ~ 320 ° C, which is a proper temperature for complete combustion, and is a means for obtaining preheating energy by recycling its own waste heat without supplying external heat energy. The heat energy of the catalytic reactor outlet gas 28 in the superheated steam state of 320 ° C. or higher is recycled using the plate heat exchangers 27, 26, 25, 24, and 23. 21) is used as a heat energy for preheating to 270 ~ 280 ℃, and the heat energy for preheating to 300 ~ 320 ℃, which is the proper combustion temperature of the catalytic reactor, is 20 ~ 40 ℃. The only high speed fermentation of organic waste drying system, characterized in that the electricity is supplied by using the opening 29, the thermal energy for heating. 5. The saturated oil vapor of claim 4, wherein the "ALS unit" is 65 to 75 DEG C supplied to the suction chamber 22 by the high pressure blower 09 from the exhaust chamber 56 at the upper end of the high speed fermentation dryer processing tank 08. Since the 31 and the catalytic reactor outlet superheated steam 28 having a temperature of 320 ° C. or higher pass through each other in phase flow, the low temperature side inlet air 31 is connected to the plate heat exchanger 23, 24, 25, 26, 27. Each time it passes through, it is heated to 65-75 ℃ ⇒ 110-120 ℃ ⇒ 150-160 ℃ ⇒ 190-200 ℃ ⇒ 230-240 ℃ ⇒ 270-280 ℃ and the hot air outlet air 28 is a plate heat exchanger (27). Each time it passes through the chamber, it is cooled to 320 ℃ ⇒ 280-290 ℃ ⇒ 240-250 ℃ ⇒ 200-210 ℃ ⇒ 160-170 ℃ ⇒ 120-130 ℃. 22) Energy cycles are phased at the same rate according to the inlet temperature, air flow rate and wind speed of air containing phase-change materials such as malodors and gases supplied to 22). Organic waste high speed fermentation drying system, characterized in that. 6. The plate heat exchanger (23, 24, 25, 26, 27) according to claim 5, wherein the plate heat exchanger (23, 24, 25, 26, 27) is supplied with electricity containing air containing a phase change material such as odor and gas flowing into the suction chamber 22 of the "AL unit". When recycling the thermal energy of the catalytic reactor outlet superheated steam 28 which is 320 ° C. or higher to preheat it to 270-280 ° C., which is the inlet temperature of the hot air 29, the plate heat exchanger 3 to 8 according to the inlet temperature, air volume and wind speed of the suction chamber. High-speed organic waste fermentation drying system characterized in that it is configured to obtain ΔT of the required temperature because the units in series heat-assembly in the stage or in series-assembly in two to four stages in series or in parallel. 2. The "two-stage energy cycle system" according to claim 1, wherein the superheated steam (35) which is discharged from the discharge chamber (32) of the "AL unit" (06) by using the high pressure blower (15). It is to supply heat energy necessary for the latent heat of evaporation to the inside of the treatment tank by supplying it to the energy cycle heat exchanger 36 of the treatment tank double jacket 20, and to improve the heat transfer efficiency on the surface of the heat exchanger double jacket inner cylinder 39. The organic waste high-speed fermentation drying system, characterized in that configured to expand the heat transfer area by closely bonding the heat transfer fin (38) for the purpose. The heat transfer fin 38 is made of a stainless steel sheet having a thickness of 0.6 ~ 1.2t, and the heat transfer fin 38 is formed of a flat plate or an uneven embossed plate according to the treatment capacity, air volume and wind speed. A high speed fermentation drying system for organic wastes, characterized in that the spacing (pitch) of the fins is composed of 3 mm to 10 mm. 8. The energy cycle heat exchange part 36 is divided into four stages, five stages, or six stages by the partition 40, and the high temperature steam supplied through the inlet 58 of the heat exchange portion is the uppermost coil portion ( 68 through the chamber 41 to reciprocate to the next coil unit (69, 70, 71) to make the heat transfer effect, and after passing through the last coil unit 71 through the outlet (63) As the heat energy contained during the exhaust is lost to the latent heat of evaporation of the internal material of the treatment tank, it is gradually condensed and is discharged in the state of mixed wet vapor and condensed water. High-speed fermentation drying system for organic waste, characterized in that the structure is circulated while transmitting to. The method of claim 7, wherein the heat transfer fin (38) is joined in a step (64) to form a portion in which the circulating air at both ends of the heat exchange part is turned into a V-shaped chamber 41 form saturated steam (59, 60, 61) , 62) organic waste high-speed fermentation drying system, characterized in that the structure of the flow is smoothly U-turn. According to claim 1, wherein the "three-stage energy cycle system" is a two-stage energy cycle after the saturation wet steam 42 discharged through the outlet 63 of the treatment tank jacket energy cycle heat exchange unit through the water separator 14 to exhaust ( 43) The organic waste high-speed fermentation drying system, characterized in that configured to preheat the outside air supplied through the air preheater (12) while recovering thermal energy. The stainless steel heat exchange coil of claim 11, wherein the saturated water vapor 42 discharged through the outlet 63 of the treatment tank jacket energy cycle heat exchanger flows into the suction chamber 72 at the bottom of the water separator. 16) After passing through the chamber 73 and the exhaust port 43 of the upper end and reciprocating circulating from the upper head 74 while flowing to the lower head 75, the heat medium inside the heat exchange coil of the structure and mutually opposed flow The organic waste high-speed fermentation drying system, characterized in that the thermal energy of the saturated wet steam (42) is transferred to the heat medium while crossing the furnace. The air preheater of claim 11 is a device for preheating the air supply 67. The air preheater preheats the outside air at a low temperature when supplying air necessary for aerobic fermentation and catalytic combustion. The outside air 46 supplied through the 44 is introduced into the air preheater 12 and passes through the heat exchange coil 17. The inside of the heat exchange coil having a structure flowing back and forth from the inner header 76 to the inlet side 77 It is configured to be heated while intersecting with the heat medium in the opposite flow to the air supply (67) through the air inlet (66), and the necessary heat energy is to use the waste heat recovered from the gas (43) exhausted without supplying external heat energy. Organic waste high speed fermentation drying system. The heat exchange coil (14) of the water separator and the heat exchange coil (12) of the air preheater are connected through a circulation pump (19) and a pipe (18). The heat medium mixed in proportion is filled and circulated by the circulation pump 19, and is heated while recovering thermal energy from the exhaust gas 42 exhausted through the heat exchange coil 16 inside the water separator 14. The organic waste high speed fermentation drying system, characterized in that configured to be supplied to the heat exchange coil (16) of the air preheater (12) to preheat the air supply (67). The hopper or animal husbandry according to claim 1, wherein the deodorizing means is used for the purpose of simultaneously deodorizing the surrounding area while supplying air necessary for aerobic fermentation and catalytic combustion when the LS high speed fermentation drying system is normally operated. Connect the air supply duct 44 connected to the treatment tank air supply 66 through the air preheater 12 from the upper end of the manure storage tank 04, and then the odorous air 45 at the upper end of the hopper or storage tank. Organic waste high-speed fermentation drying system, characterized in that the storage tank (04) is supplied with fresh external air (46) is supplied to the storage tank so that the deodorization of the odor generating unit at the same time. According to claim 1, wherein the "automatic control system" is operated when the fermentation dryer is operated, the preheating is completed, the system of each part is maintained in normal operation, all the operation process of injecting organic waste into the treatment tank and discharge the fermentation dried by-products Organic waste high speed fermentation drying system, characterized in that configured to be controlled automatically. 17. The method according to claim 16, wherein the automatic input control means adjusts the operation time of the input device by a timer so that a predetermined amount determined per hour is set, so that the input amount is controlled to control the input amount. The water content of the material inside the treatment tank is gradually lowered. When the water content is lower than the predetermined water content, the water content sensor 55 is automatically configured to add a certain amount of time in parallel. If there is no material in the waste storage tank, the input device does not operate. A high speed fermentation drying system for organic waste, characterized in that the system is automatically stopped after cooling the inside of the processing tank overheated by the moisture content sensor 55 for 30 minutes. 17. The method according to claim 16, wherein the automatic discharge control means adjusts the operation time of the discharge device by a timer so that a predetermined amount determined at a predetermined time is set every day, so that the discharge is controlled by default. Depending on the level of the treatment tank, there may be a change in the level of the treatment tank. When the structure of the treatment tank is automatically discharged, even if the discharge conveyor is operated for a long time, a certain level or less is not discharged. Also, the upper level sensor 53 and the lower level sensor are not discharged. The organic waste high-speed fermentation drying system, characterized in that (54), in parallel with the discharge by the timer, can always maintain the level of the substance inside the treatment tank at an appropriate state. In order to obtain another effect of the present invention, when the energy recycle acta system is applied to a deodorizing system, another energy cycle unit ( 67) is composed of a two-layer structure to complete the deodorizing " ELS unit " and deoxidizes the air 53 containing the odors introduced from the odor generating place 81 after catalytic combustion and deodorization. 79) and the air supply 56 necessary for the indoors is pre-heated fresh air 55 in the heat exchanger, and then supplied by the air supply (80), characterized in that the deodorizing " LS unit " 20. The energy recycling unit according to claim 19, according to the inlet temperature, air volume and wind speed of the air containing the phase change material such as odor and gas supplied to the suction chamber 22, and the temperature and environment of the odor generating place 81. Deodorization-only "LS unit" characterized by being suitably applied according to the odor generating environment and processing purpose by adjusting the quantity and arrangement of heat exchangers of the lower heat exchanger unit and the upper heat exchanger unit.

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