KR101446838B1 - Reduced-pressure fermenting and drying apparatus - Google Patents

Abstract

An object of the present invention is to provide a method and apparatus for efficiently removing odors generated from a subject to be treated and preventing odor from diffusing to the surroundings and also capable of preventing degradation due to corrosion components And a fermentation drying device.
The reduced-pressure fermentation drying apparatus 1 comprises a dryer 2 having a treatment chamber 22 into which organic matter to which microorganisms are added is charged, a heating jacket 24 installed in the dryer 2 for heating the article to be treated A heating agitating part 25 which is rotatably disposed in the processing chamber 22 of the dryer and which stirs and simultaneously heats the object to be processed and a condensing part 23 for condensing water vapor generated from the organic waste to generate condensed water A gas-liquid separator 3 for guiding a mixture of condensed water in the condenser 23 and the air in the treatment chamber 22 and separating the induced mixture into condensed water and air; And a suction pump 5 connected to the gas-liquid separator for sucking the condensed water of the condenser 23 and the air in the process chamber 22 toward the gas-liquid separator.

Description

REDUCED-PRESSURE FERMENTING AND DRYING APPARATUS

The present invention relates to a vacuum fermentation drying apparatus for drying a subject to be fermented while heating the subject under reduced pressure.

An apparatus for drying an organic matter having a high water content, such as excess sludge or kitchen waste generated in a sewage treatment plant, comprising: an apparatus for drying an object to be treated in a reduced pressure environment, The device is known. In this kind of vacuum fermentation drying apparatus, since the odor of the object to be treated is comparatively strong, various countermeasures for deodorization are carried out.

As shown in Fig. 9, the applicant has a treatment chamber 111 in which the inside is decompressed by a vacuum pump 104, and a pressure chamber 111 provided in an upper part of the treatment chamber 111 A condensation section 115 for condensing water vapor generated by the drying of the object to be treated, a stirring and heating device 114 for heating and simultaneously stirring the object to be processed in the process chamber 111, A heating jacket 113 installed, a steam boiler 106 for generating steam for heating, and a cooling tower 105 for cooling cooling water, which is a cooling medium of the condensing section 115 (see Patent Document 1 Reference).

This reduced-pressure fermentation drying apparatus 101 is for drying an object to be treated such as excess sludge having a water content of more than 95%. The object to be processed put into the processing chamber 111 from the inlet 116 is introduced into a vacuum pump The heating jacket 113 and the stirring and heating device 114 while stirring and stirring by the stirring and heating device 114 to promote drying. A plurality of stirring rods 114b extending in the radial direction are fixed to a rotary shaft 114a in which a steam passage is formed and a stirrer 114b is attached to the front end of the stirring rod 114b, And a transfer blade 114c for transferring in a direction parallel to the rotary shaft 114a while stirring. Both ends of the rotating shaft 114a are rotatably supported by bearings provided on the wall of the casing 112 forming the process chamber 111. [ The bearing supporting the rotating shaft 114a is configured such that steam can flow and the steam supplied from the steam boiler 106 to the heating jacket 113 is guided to the stirring and heating device 114 through the bearing . The object to be processed that has undergone the drying process in the process chamber 111 is discharged from the discharge port 117 provided in the lower portion of the casing 112.

The cooling tower 105 has a water tank 151 for storing cooling water at its lower portion and the cooling water of the water tank 151 is pumped up by a water spray pump 155 so that the filler 153 As shown in FIG. The condensed water in the condensing section 115 and the air in the processing chamber 111 are guided to the cooling tower 105 by a vacuum pump 104 for depressurizing the processing chamber 111 to cool the cooling water flowing in the cooling tower 105 . Microorganisms having a malodor decomposition action are added to the filler 153 of the cooling tower 105. When the cooling water injected from the spray nozzle 152 flows through the filler 153, And the odor is decomposed by microorganisms. As described above, the cooling tower 105 cools the cooling water to be supplied to the condensing section 115 and deodorizes the condensed water and air discharged from the processing chamber 111.

Japanese Patent Application Laid-Open No. 2011-105816

However, in the above conventional vacuum fermentation drying apparatus, since the condensed water or air from the processing chamber 111 is guided to the cooling tower 105 and mixed with the cooling water, the amount of objects to be deodorized becomes large, . In addition, there is a problem that the odor of the condensed water or air guided to the cooling tower 105 leaks to the outside from the cooling tower 105 and diffuses to the surroundings. In addition, there is a problem that the vacuum pump 104 for guiding the condensed water or air from the process chamber 111 to the cooling tower 105 is easily deteriorated by the corrosive components contained in the condensed water or air.

Accordingly, it is an object of the present invention to provide a method and apparatus which can effectively remove the odor generated from the object to be treated, prevent the odor from diffusing to the surroundings, and prevent deterioration due to the corrosion component And which is capable of performing a fermentation process.

Means for Solving the Problems In order to solve the above problems, in the reduced pressure fermentation drying apparatus of the present invention,

A dryer having a treatment chamber into which organic matter to which microorganisms are added is introduced,

A heating unit installed in the dryer and heating the object to be processed,

An agitating part rotatably disposed in the treatment chamber of the dryer and stirring the object to be processed,

A condenser for condensing water vapor generated from the organic waste to generate condensed water,

A gas-liquid separator for guiding a mixture of the condensed water of the condenser and the air in the processing chamber, and separating the induced mixture into condensed water and air;

And a suction pump connected to a downstream side of the gas-liquid separator for sucking the condensed water of the condenser and the air in the treatment chamber toward the gas-liquid separator.

According to the above configuration, the organic object to which the microorganism is added is introduced into the treatment chamber of the drier, and the object to be processed is stirred by the stirring portion while being heated by the heating portion. In the treatment chamber, the air is sucked by the suction pump and the air pressure is lower than the atmospheric pressure, so that the boiling point of the substance is lowered. Therefore, the object to be treated, which is stirred by the stirring portion while being heated by the heating portion, is efficiently vaporized and dried quickly. Further, the heating temperature of the heating section can be set to a low value by lowering the boiling point due to the decompression of the treatment chamber, and the microorganisms can be prevented from being killed by the high temperature, so that the odor can be effectively decomposed by the microorganisms. The water vapor generated from the object to be treated is condensed in the condensing portion to be condensed water, and is sucked by the suction pump together with the air in the processing chamber, and a mixture of these condensed water and air is led to the gas- The condensed water and the air in which the mixture is separated in the gas-liquid separator are treated separately by different treatment devices. Therefore, the odor is removed more efficiently than when the condensed water and the air are mixed and treated in the cooling water. Further, since the condensed water and the air sucked from the treatment chamber can be treated efficiently, the condensed water can be attracted more from the treatment chamber, and the drying efficiency of the treatment object in the treatment chamber can be increased. Further, by treating the condensed water and the air in a sealed processing apparatus, it is possible to prevent the spread of the offensive odor, rather than mixing the condensed water and air into the cooling water from the cooling tower. Further, since the condensed water and the air are led to the gas-liquid separator by the suction pump connected to the downstream side of the gas-liquid separator, deterioration of the suction pump can be reduced. The stirring section may also serve as a heating section. That is, a heating function may be added to the agitating portion to stir the object to be processed and to heat the object to be processed.

The reduced-pressure fermentation drying apparatus of one embodiment includes a wastewater treatment apparatus that treats the condensed water separated by the gas-liquid separation apparatus by the activated sludge method.

According to the above embodiment, by treating the condensed water with the activated sludge method by the wastewater treatment apparatus, the organic matter contained in the condensed water can be decomposed by the aerobic microorganisms, and the odor can be effectively removed.

The reduced-pressure fermentation drying apparatus of one embodiment includes an ozone reaction tank for treating the air separated by the gas-liquid separator with ozone.

According to the above embodiment, the ozone reaction tank is capable of effectively removing odor by oxidizing the organic substances contained in the air with ozone by treating the air sucked from the treatment chamber and separated from the gas-liquid separation device.

The reduced-pressure fermentation drying apparatus of one embodiment comprises a condensate water storage tank for storing condensate water separated from the gas-liquid separator,

A reservoir tank for measuring the weight of the condensate storage tank,

A dryer-type intermediate machine for measuring the weight of the dryer,

And a drying degree calculator for calculating the degree of drying of the article to be treated in the treatment chamber of the dryer based on the measurement results of the middle tank and the dryer.

According to the above embodiment, the condensed water separated in the gas-liquid separator is stored in the condensed water storage tank, and the weight of the condensed water storage tank is measured by the storage tank medium. On the other hand, the weight of the dryer is measured by the dryer middle stage. Based on the measurement results of the storage tank middle tank and the dryer tank middle tank, the degree of drying of the object to be treated in the treatment chamber of the drier is calculated by the drying degree calculator. This drying degree calculator is based on the weight of the condensed water which is the moisture actually removed from the object to be processed, so that the correct drying degree of the object to be processed can be calculated.

The reduced-pressure fermentation drying apparatus of one embodiment comprises a plurality of the condensed water storage tanks,

And a distribution valve interposed in a pipe connecting the gas-liquid separator and the plurality of condensed water storage tanks and distributing the condensed water led from the gas-liquid separator to each of the condensed water storage tanks so that the plurality of condensed water storage tanks are sequentially filled.

According to the above embodiment, since the condensed water separated in the gas-liquid separator is divided and stored in a plurality of condensed water storage tanks, the weight of the filled condensate water storage tanks can be sequentially and separately measured by the storage tank weighing machine. Since the condensed water in the condensed water storage tank after the measurement of weight is discharged, the condensed water can be received again, so that the condensed water storage, the measurement of the weight, and the discharge of the condensed water are sequentially repeated by the plural condensed water storage tanks, The weight of the condensed water can be measured without. Thus, when the condensate reservoir is filled, as in the case of reserving condensate in a single condensate reservoir, there is no interruption of the condensate water suction for measurement of the weight of the condensate reservoir and discharge of the condensate. As a result, it is possible to quickly remove water vapor from the processing chamber in which the object to be dried is performed, and to rapidly dry the object to be processed. Further, as compared with the case of storing the condensed water in a single condensed water storage tank, the condensed water can be stored in the other condensed water storage tank while discharging the condensed water from the filled condensed water storage tank. Therefore, A small capacity condensate reservoir can be used. Therefore, the size of the condensed water storage tank can be reduced, and the structure of the reduced-pressure fermentation drying apparatus can be downsized.

The reduced pressure fermentation drying apparatus of one embodiment includes a cooling medium for cooling the suction pump and a cooler for cooling the cooling medium of the condensing section.

According to the above embodiment, the energy used for cooling can be reduced by cooling both of the cooling medium and the suction pump and the condenser, which are operated simultaneously, with a single cooler.

In the reduced-pressure fermentation drying apparatus of one embodiment,

A hollow rotary shaft rotatably supported by a bearing installed in the dryer,

A spiral tube connected to the rotary shaft and wound around the outer diameter side of the rotary shaft in a spiral shape and communicating with the inside of the rotary shaft,

And a transfer blade which is disposed on the outer diameter side of the helical tube and transfers the object to be processed in the treatment chamber toward the rotation axis direction.

According to the above-described embodiment, the object to be processed is heated by the rotary shaft and the spiral tube while being rotationally driven while supplying steam, for example, steam as a heating medium into the rotary shaft and the spiral tube, And stirred. Therefore, for example, the object such as excess sludge having a moisture content exceeding 95% can be effectively and quickly dried.

In the reduced-pressure fermentation drying apparatus of one embodiment, the wastewater treatment apparatus includes:

A reaction tank having a closed structure for condensing organic matters by adding aerobic microorganisms to the condensed water,

And a nano bubble generating device for generating nano bubbles of air added to the condensed water of the reaction tank.

According to the above embodiment, the aerobic microorganism is added to the condensed water in the reaction tank, and the organic matter coagulates due to the action of the aerobic microorganism. Nano bubbles of the air generated in the nano bubble generating device are added to the condensed water in the reaction tank, thereby aeration is performed. Since the nano bubbles are stably dispersed in the condensed water, ventilation of the reaction tank is unnecessary even if they are added to the closed reaction vessel. Therefore, it is possible to prevent the problem that the odor is diffused from the reaction tank to the outside. Therefore, this wastewater treatment apparatus can treat the condensed water by the activated sludge method without diffusing the odor to the surroundings. Here, the nano bubble refers to a bubble having a diameter of 10 nm or more and 900 nm or less.

According to the present invention, the object to be treated to which microorganisms have been added is stirred while being heated in a processing chamber in which the air pressure is lower than atmospheric pressure, and the water vapor in the processing chamber is condensed and discharged in the condensing portion. By the discharging action, it is possible to quickly and effectively deodorize and dry the article to be treated. In addition, a mixture of the condensed water condensed in the condenser and the air in the treatment chamber is sucked by the induction pump and guided to the gas-liquid separator, and the condensed water and air separated by the gas-liquid separator are separately treated by different treatment devices , The odor contained in the condensed water and the air can be efficiently removed. Further, since the condensed water and the air sucked from the treatment chamber can be efficiently treated, the condensed water can be attracted more from the treatment chamber, and thus the drying efficiency of the treatment object in the treatment chamber can be increased. Further, by treating the condensed water and the air in a sealed processing apparatus, it is possible to prevent the spread of the offensive odor, rather than mixing the condensed water and air into the cooling water from the cooling tower. Further, since the condensed water and the air are led to the gas-liquid separator by the suction pump connected to the downstream side of the gas-liquid separator, deterioration of the suction pump can be reduced.

1 is a block diagram showing a vacuum pressure fermentation drying apparatus according to an embodiment of the present invention.
2 is a longitudinal sectional view schematically showing a dryer of a vacuum pressure fermentation drying apparatus.
3 is a cross-sectional view schematically showing a dryer of a vacuum pressure fermentation drying apparatus.
4A is a longitudinal sectional view schematically showing a gas-liquid separator.
4B is a cross-sectional view schematically showing the gas-liquid separator.
5 is a schematic diagram showing a wastewater treatment apparatus.
6 is a cross-sectional view showing a finishing nozzle of a nano bubble generating apparatus of a wastewater treatment apparatus;
7A is a plan sectional view of a finely divided block of a finizing nozzle;
7B is a longitudinal sectional view of the micronization block.
8 is a cross-sectional view schematically showing a vacuum pump.
9 is a block diagram showing a conventional vacuum fermentation drying apparatus.

DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings.

1 is a block diagram showing the overall configuration of a vacuum pressure fermentation drying apparatus according to an embodiment of the present invention. This reduced-pressure fermentation drying apparatus (1) treats excess sludge having a water content of more than 95% as an object to be treated. This reduced-pressure fermentation drying apparatus 1 includes a dryer 2 having a treatment chamber 22 into which a substance to be treated is injected, a gas-liquid separator 3 for guiding condensed water from the dryer 2, Two buffer tanks 4 and 4 as a condensed water storage tank for storing the condensed water separated in the vacuum pump 3, a vacuum pump 5 as a suction pump connected to the downstream side of the gas-liquid separator 3, A cooling tower 7 as a cooler for supplying cooling water as a cooling medium to the vacuum pump 5 and the drier 2 and a cooling tower 7 as a cooler for supplying cooling water as a cooling medium to the drier 2, And a wastewater treatment device 9 for treating the condensed water.

Fig. 2 is a longitudinal sectional view showing a state in which the dryer 2 is cut in the vertical direction along the longitudinal direction, and Fig. 3 is a transverse sectional view showing a state in which it is cut in the vertical direction along the short direction of the dryer 2.

2 and 3, the dryer 2 includes a substantially cylindrical casing 21 having a treatment chamber 22 therein, and a heating jacket 24 (not shown) formed along the lower wall surface of the treatment chamber 22 And a heating stirring portion 25 as a stirring portion disposed in the treatment chamber 22. [

An injection device 26 for injecting the object to be processed is formed at the center of the upper part of the casing 21 and a discharge port 22b for discharging the object to be processed is formed at the other end of the lower part of the casing 21 . The charging device 26 of the casing 21 has a funnel-shaped charging port 261 with an opened upper end and an air lock 262 provided at the lower end of the charging port 261. The air lock 262 is provided with a hermetic valve at the inlet 261 side of the article to be treated and at the side of the treatment chamber 22 so that the object to be processed is introduced from the inlet 261 into the air lock 262, The object to be processed is introduced into the processing chamber 22 without increasing the air pressure in the processing chamber 22 lower than the atmospheric pressure by closing the closing valve of the processing chamber 22 and opening the closing valve at the processing chamber 22 side.

The heating stirring section 25 includes a hollow rotary shaft 251 having both ends supported by bearings 27 and 27 provided on both end faces of the casing 21 and two hollow rotary shafts 251 fixed to surround the outer diameter side of the rotary shaft 251 Helical tubes 255 and 258 and a plurality of rectilinear feed vanes 256 and 259 arranged on the outer circumferential sides of the helical tubes 255 and 258 and having sides of 5 to 10 cm. The inside of the rotary shaft 251 and the spiral pipes 255 and 258 communicate with each other. Steam as a heating medium supplied from the steam boiler 8 is supplied to the rotary shaft 251 through the steam supply pipe 264 connected to one end of the rotary shaft 251. The steam is supplied from the rotary shaft 251 to the spiral pipes 255, 258). ≪ / RTI > A driven pulley 283 is provided at one end of the rotating shaft 251 of the heating stirring section 25 and the driven pulley 283 and the output pulley 282 provided on the output shaft of the motor 281 are connected to the chain 284 . The rotating force of the motor 281 is transmitted to the rotating shaft 251 through the chain 284 so that the heating stirring portion 25 is rotated.

Steam is supplied to the rotary shaft 251 and the spiral tubes 255 and 258 of the heating agitation unit 25 and the heating agitation unit 25 is rotationally driven to rotate the rotary shaft 251 and the spiral tubes 255 and 258 The object to be processed is heated and the object to be processed in the processing chamber 22 is agitated while being conveyed from the center toward both ends or from both ends toward the center. The direction in which the feed vanes 256 and 259 feed the article to be processed can be selected by selecting either of the direction from the center toward both ends and the direction from the both ends toward the center by selecting the rotating direction of the heating agitator 25 .

The spiral pipes 255 and 258 of the heating agitation unit 25 are connected to the upstream side spiral pipe 255 located on the upstream side in the flow of the steam of the rotary shaft 251 and the downstream side spiral pipe 255 located on the downstream side, (Not shown). The upstream side helical tube 255 and the downstream side helical tube 258 are formed so that the winding directions of the helical wires are opposite to each other. The upstream end of the upstream side helical tube 255 is formed in the upstream straight pipe portion 255a extending in the radial direction of the rotary shaft 251 and the upstream straight pipe portion 255a is located on the upstream side of the rotary shaft 251 Respectively. The downstream side end portion of the upstream side helical tube 255 is formed in the downstream straight pipe portion 255b extending in the radial direction of the rotary shaft 251. The downstream straight pipe portion 255b is formed in the longitudinal direction of the rotary shaft 251 And is connected to the center. The upstream side end portion of the downstream side helical tube 258 is formed in an upstream straight pipe portion 258a extending in the radial direction of the rotary shaft 251. The upstream straight pipe portion 258a has a length Direction. The downstream side end of the downstream side helical tube 258 is formed in a downstream straight pipe portion 258b extending in the radial direction of the rotary shaft 251. The downstream straight pipe portion 258b is located on the downstream side of the rotary shaft 251 Respectively.

Steam derived from the steam boiler 8 is supplied to the end portion on the upstream side of the rotary shaft 251 through the steam supply pipe 264 as shown by the arrow V1 in the heating stirring portion 25, Flows into the upstream straight pipe portion 255a of the upstream side spiral pipe 255 as indicated by an arrow G1. The steam introduced into the upstream straight pipe portion 255a is returned to the rotary shaft 251 from the downstream straight pipe portion 255b through the upstream side helical pipe 255 as indicated by an arrow G2. The steam in the rotary shaft 251 flows into the upstream straight pipe portion 258a of the downstream side helical pipe 258 and flows into the downstream straight pipe portion 258b through the downstream side helical pipe 258, As indicated by an arrow G4. The steam flows in the rotary shaft 251, the upstream-side spiral tube 255 and the downstream-side spiral tube 258 to flow the steam to the rotary shaft 251, the upstream side spiral tube 255 and the downstream side spiral tube 258 To be heated is heated. The steam that has flowed through the rotary shaft 251, the upstream side helical tube 255 and the downstream side helical tube 258 flows through the steam discharge pipe 265 connected to the downstream end of the rotary shaft 251, And is returned to the drain recovery tank 81 together with the drain generated on the path of these vapors.

The mounting blades 256 and 259 are capable of adjusting the mounting angle to the spiral pipes 255 and 258 and the mounting position of the spiral pipes 255 and 258 in the radial direction. More specifically, as viewed in the radial direction of the helical pipes 255 and 258, the feed vanes 256 and 259 can be adjusted to a desired angle around the diametrical direction. The feed vanes 256 and 259 are mounted inclined with respect to the axis of the rotary shaft 251 when viewed in the radial direction of the spiral pipes 255 and 258. The ratio of the action of transporting the article to be processed in the direction of the rotation axis 251 and the operation of kneading the object to be processed is adjusted in accordance with the magnitude of the inclination angle of the conveying vanes 256 and 259. More specifically, when the inclination angles of the conveying blades 256 and 259 with respect to the rotary shaft 251 are large, the effect of conveying the article to be processed in the direction of the rotary shaft 251 is large, When the inclination angles of the slits 256 and 259 are small, the action of kneading the material to be processed becomes large. By adjusting the inclination angles of the conveying vanes 256 and 259 in this way, the heating stirring portion 25 can exert an action adapted to the object to be processed.

The feed blades 256 mounted on one spiral pipe 255 and the feed blades 259 mounted on the other spiral pipe 258 are set so that the oblique directions when viewed in the radial direction are reversed . As a result, as the heating agitating section 25 rotates, the heating agitating section 25 is rotated from both ends of the rotating shaft 251 of the heating agitating section 25 toward the center, The object to be processed is transferred from the center of the rotary shaft 251 of the rotary shaft 25 toward both ends. Therefore, by controlling the rotating direction of the heating agitating part 25, the direction of feeding the object to be processed can be controlled.

The adjustment of the mounting position of the feed vanes 256 and 259 with respect to the spiral pipes 255 and 258 allows the distances of the feed vanes 256 and 259 to be spaced apart from the spiral pipes 255 and 258. As the distance of the transfer vanes 256 and 259 from the spiral pipes 255 and 258 increases, the leading edges of the transfer vanes 256 and 259 in the diametrical direction of the spiral pipes 255 and 258, So that the clearance between the leading edge of the conveying vanes 256 and 259 and the inner wall surface of the process chamber 22 is reduced. A heating jacket 24 is provided on the wall of the processing chamber 22 so that the object to be processed adheres to the inner wall surface of the processing chamber 22 by the heat of the heating jacket 24 when the object to be processed is dried. As the attachment of the object to be processed proceeds, there arises a problem that the object to be processed is fixed to the inner wall surface by the heat of the heating jacket 24. By adjusting the clearance between the front edge of the conveying vanes 256 and 259 and the inner wall surface of the process chamber 22, the object to be adhered to the inner wall surface of the process chamber 22 can be scraped off, It is possible to prevent the wall from sticking. By thus adjusting the mounting positions of the conveying vanes 256 and 259, the conveying vanes 256 and 259 can function as scrapers.

A maintenance window, not shown, extending in the longitudinal direction is provided on the side surface of the casing 21. The maintenance window is opened to adjust the mounting angle of the conveying vanes 256, 259 of the heating agitation section 25, Adjustment of the mounting position, and maintenance such as replacement of the feed vanes 256 and 259 are performed.

As shown in Fig. 3, the heating jacket 24 is provided along the casing 21 so as to surround the lower portion of the rotating region of the heating agitating section 25. As shown in Fig. The heating jacket 24 has a steam supply pipe 24a connected to one longitudinal end portion thereof and a steam discharge pipe 24b connected to the center in the longitudinal direction thereof. The steam derived from the steam boiler 8 is supplied to the heating jacket 24 through the steam supply pipe 24a and flows through the heating jacket 24 to discharge the object to be processed in the treatment chamber 22 And is discharged to the outside of the dryer 2 through the steam discharge pipe 24b as shown by the arrow V3 and returned to the drain recovery tank 81 together with the drain generated on the path of these steam.

At the upper part of the casing 21, there is provided a condensing part 23 for condensing the vapor evaporated from the object to be treated. The condensing section 23 has a cooling water supply chamber 231 formed on the other end side of the casing 21 and a cooling water discharge chamber 232 formed on one end side of the casing 21. In the cooling water supply chamber 231, a cooling water supply pipe 233 through which cooling water is led from the cooling tower 7 is connected. In the cooling water discharge chamber 232, a cooling water discharge pipe 234 for returning the cooling water to the cooling tower 7 is connected. A plurality of cooling water pipes 235, 235, ... extending in the axial direction of the casing 21 are provided between the cooling water supply chamber 231 and the cooling water discharge chamber 232. These cooling water pipes 235, The cooling water in the cooling water supply chamber 231 flows into the cooling water discharge chamber 232. The plurality of cooling water pipes 235, 235, ... are arranged on both sides in the width direction of the upper part of the casing 21, as shown in the cross-sectional view in Fig. Water collecting tanks 236 and 236 for collecting condensed water are provided on the side and lower sides of the plurality of divided cooling water pipes 235, 235, ..., respectively. A suction tube 237 for suctioning the air in the treatment chamber 22 is communicated with the condensed water inside the water collection tube 236.

In the treatment chamber 22 of the dryer 2, an enzyme acting on the substance to be treated is present. The enzyme is obtained by collecting microorganisms such as native bacteria or fermenting bacteria that reproduce in the natural world such as sea, mountains and land, and cultivating them into the treatment chamber 22. In particular, an enzyme produced by bacteria, which reproduce in various animals, plants, and soils, is effective for decomposing and deodorizing organic sludge such as excess sludge. Examples of flora and fauna in which the germs reproduce include wormwood, grasses, herbaceous plants, beach grass, bamboo grass, bamboo soil, forest soil, fish, seaweed, fruit, pineapple, apple, mandarin orange, peach and grape. It is preferable to use the bacteria that reproduce in these plants by culturing them in rice bran or sawdust. In the present embodiment, the object to be treated is stirred for 30 minutes to 3 hours at a heating medium temperature of 60 to 80 占 폚 under a reduced pressure of 0.03 to 0.098 MPa, so that the microorganisms growing and fermenting under these conditions are introduced into the processing chamber 22 Is preferably added. The decompression value refers to the amount of pressure to be reduced from atmospheric pressure.

The enzyme present in the treatment chamber 22 by the action of the microorganism may be any of the following, or may be plural. In addition, in parentheses following each enzyme, substances in which each enzyme acts are described. (Alcohols), lactate dehydrogenase (lactose), glucose dehydrogenase (saccharide), aldehyde dehydrogenase (aldehyde), L · aspartate · beta semialdehyde · NADP NADPH2 cytochrome C reductase (NADP), glutathione dehydrogenase (glutathione), trehalose (glutathione), glutamic acid dehydrogenase (amino acid), aspartate dehydrogenase (Carbohydrate), polyphosphate kinase (ATP), ethanolamine phosphate cytidyl transferase (CTP), trehalose phosphatase (carbohydrate), metal thiophosphate glyceralate force (Amino acid), cytosine / diamine (cytosine), methylcysteine synthase (amino acid), and the like. Aspartic acid synthase ( ATP), succinic acid dehydrogenase (succinic acid), aconitic acid hydrogencer (citric acid), fumarate hydrogenase (malonic acid), malate dehydrogenase (malonic acid), citric acid synthase (acetyl CouA) , Histidine dehydrogenase (citric acid), LSNADP oxidase (citric acid), monoamine oxidase (amine), histaminase (amine), pyruvate decarboxylase (oxo acid), ATPase ), Nucleotide pyrophosphatase (nucleic acid), endopolyphosphatase (ATP), ATP phosphohydrolase (ATP), orotidine 5-phosphate decarboxylase (orotidine). By adding a microorganism producing at least one of these enzymes to the substance to be treated, it is possible to effectively decompose the substance to be treated composed of various kinds of organic substances.

The dryer (2) having the above components has a load cell (29, 29) as a dryer-type heavy machine provided between the supporting member at the lower end and the base. The load cells 29 and 29 are connected to the control device 10. The control device 10 measures the weight by operating the load cells 29 and 29 before and after the object to be processed is charged and calculates the weight of the object to be processed based on the measured values of the load cells 29 and 29.

4A is a longitudinal sectional view showing the gas-liquid separator 3, and Fig. 4B is a cross-sectional view showing the gas-liquid separator 3. Fig. 4A, the gas-liquid separator 3 has a vertically elongated casing 31 having a substantially cylindrical shape and having a central axis oriented in the vertical direction. In the lower portion of the casing 31, The introduction pipe 32 for guiding the mixture of the condensed water and the air in the treatment chamber 22 is fixed toward the tangential direction of the casing 31 in the transverse section. In the casing 31, a liquid discharge pipe 33 for discharging the condensed water separated from the mixture is provided at the lower end, and a gas discharge pipe 34 for discharging the air separated from the mixture is provided at the upper end. The gas-liquid separator 3 contains a cyclone portion 35, a demister 36 and a filter portion 37 in this order from the bottom toward the top in the casing 31.

The cyclone portion 35 includes a vortex chamber 351 formed between the lower portion of the casing 31 and the partition plate 353 fixed transversely to the inside of the casing 31 and a vortex chamber 351 formed at the center of the partition plate 353 And a discharge chamber 352 which is fixed and protrudes into the vortex chamber 351. As shown in Fig. 4 (b), the mixture introduced through the introduction pipe 32 flows into the vortex chamber 351 of the cyclone portion 35 in a swirling manner, and the condensed water and the air are separated by the centrifugal force. The air separated from the mixture is led to the demister 36 upward through the exhaust tower 352. On the other hand, the condensed water separated from the mixture flows downward along the inner surface of the casing 31, is discharged from the discharge hole 33a opened at the center of the bottom surface of the vortex chamber 351, passes through the liquid discharge pipe 33 And is led to the wastewater treatment device 9. The demister 36 is formed of a wire mesh in which a plurality of metal meshes are superimposed and is disposed above the partition plate 353 and adjacent to the outlet of the exhaust chamber 352 of the cyclone portion 35. When the air separated from the mixture in the cyclone portion 35 and led from the exhaust passage 352 passes through the demister 36, fine particles of the condensed water contained in the air are generated in the gap of the fibers of the demister 36 It is captured by capillary action. The filter unit 37 is provided between the upper support plate 371 on the annular plate provided at the lower end of the gas discharge pipe 34 and the lower support plate 372 in the form of a cylindrical annular filter element formed of a resin or a lump of cellulose fibers. And a filter cloth 374 surrounding the outer circumferential surface of the filter element 373 are inserted and supported. When air passing through the demister 36 passes through the filter cloth 374 and the filter element 373 of the filter unit 37, fine particles and condensed water of the condensed water remaining in the air are captured. The air that has passed through the filter cloth 374 and the filter element 373 passes through the cavity 375 inside the filter element 373 and passes through the gas discharge pipe 34 communicating with the cavity 375, And is sucked into the pump 5. The condensed water trapped by the demister 36 and the filter portion 37 falls through the casing 31 and is discharged from the liquid discharge pipe 33.

The buffer tank 4 is a tank for temporarily storing the condensed water separated from the gas-liquid separator 3 before performing the wastewater treatment of the condensed water. In this embodiment, two buffer tanks 4 and 4 are connected to the downstream side of the switching valve 41 connected to the liquid discharge pipe 33 of the gas-liquid separator 3. Each of the buffer tanks 4 is provided with load cells 42 and 42 as a storage tank middle load for measuring the weight of the buffer tank 4 and water level gauges 43 and 43 for detecting the level of condensed water in the tank. The discharge pipes of the buffer tanks 4 and 4 are provided with open / close valves 44 and 44, respectively. The switch valve 41, the load cells 42 and 42, the water level gauges 43 and 43 and the open / close valves 44 and 44 are connected to the control device 10. The two buffer tanks 4 operate under the control of the control device 10 as follows. The condensate water from the gas-liquid separator 3 is led to the one buffer tank 4 by the switching valve 41 and the water level in the buffer tank 4 is detected by the water level gauge 43. [ When the controller 10 detects that the buffer tank 4 is filled based on the detection signal of the water level gauge 43, the control device 10 operates the switching valve 41 to switch the supply of the condensed water to the other buffer tank 4 do. At the same time, the load cell 42 of the buffer tank 4 is operated to measure the weight, and the weight of the condensed water stored in the buffer tank 4 is calculated based on the measured value of the load cell 42 . When the measurement of the weight is completed, the controller 10 opens the drain valve 44 of one of the buffer tanks 4 to discharge the condensed water. When the buffer tank 4 is detected to be empty based on the detection signal of the water level gauge 43, the control device 10 closes the drain valve 44. [ In this way, by supplying the condensed water, measuring the weight, and draining the water alternately between the two buffer tanks 4, the weight of the large amount of condensed water is continuously increased by the comparatively small buffer tanks 4, . Further, two or more buffer tanks 4 may be provided.

The control device 10 calculates the sum of the weights of the condensed water measured at the load cells 42 and 42 of the buffer tanks 4 and 4 after the start of the processing of the object to be processed and the sum of the weights of the condensed water measured at the dryer 2 And the weight of the object to be processed measured by the load cells 29 and 29 of the load cells 29 and 29. In this case, Since the measurement values of the load cells 29 and 29 of the dryer 2 include the weight of the drain accumulated in the heating jacket 24 and the heating agitator 25 as the processing of the object to be processed proceeds, It is difficult to calculate the degree of drying of the treated material based on the weight of the dryer 2 alone. Therefore, the weight of the drier 2 is measured immediately after the object to be processed is put in, and the weight of the buffer tanks 4 and 4 is measured when the object to be processed is processed. The drying degree of the article to be treated is accurately calculated on the basis of the weight of the article to be treated immediately after the injection and the weight of the condensed water during the treatment.

The wastewater treatment device 9 for treating the condensed water discharged from the buffer tank 4 removes organic matter by an activated sludge method. 5, the wastewater treatment device 9 includes a pre-settling tank 91 for precipitating relatively large fine particles contained in the condensed water sent from the buffer tank 4, A reaction tank 92 for adding microorganisms and causing organic matter to flocculate under an aeration environment by the action of aerobic microorganisms and a sedimentation tank 93 for sedimenting the organic matter aggregated in the reaction tank 92. The pre-settling tank 91, the reaction tank 92, and the post-settling tank 93 are structured to be sealed by a tank, and are configured to prevent the spread of malodor. In the reaction tank 92, a nano bubble generating device 94 is provided. The nano bubble generating device 94 generates nano bubbles which are bubbles of air having a diameter of 10 nm or more and 900 nm or less. The reaction tank 92 is configured such that the nano bubbles generated by the nano bubble generator 94 are added to the condensed water so that the condensed water is brought into the aeration environment in the closed state. The water after removing the organic matter from the post-sedimentation tank 93 is discharged to the outside after adding a disinfectant such as chlorine or sodium hypochlorite. In addition, the wastewater treatment device 9 does not need to be provided with the pre-settling tank 91.

The nano bubble generating device 94 provided in the reaction tank 92 is provided with a refining nozzle 95 which is installed in the condensation water of the reaction tank 92 to be installed in the condensation water and a supply pipe 96 for supplying a mixed fluid of air and water to the refining nozzle 95 And a two-phase pump 97 for generating a two-phase mixed fluid of air and water. 7A is a plan sectional view of the miniaturization block as a component of the miniaturization nozzle 95 and FIG. 7B is a longitudinal sectional view of the miniaturization block 95. FIG. 6A is a cross- to be.

As shown in Fig. 6, the finishing nozzle 95 is roughly constituted by a substantially spherical pressure-resistant casing 951 and a fine-finishing block 954 embedded in the pressure-resistant casing 951. Fig. The mixed fluid is sent from the two-phase upstream pump 97 into the pressure-resistant casing 951 through the supply pipe 96 connected to the pressure-resistant casing 951. The mixed fluid pumped into the pressure-resistant casing 951 flows into the miniaturization block 954 under pressure and is air-fined to the outside of the pressure-resistant casing 951 through the discharge pipe 955 connected to the miniaturization block 954 . The discharge pipe 955 is fixedly inserted through the opposite side of the side of the pressure-resistant casing 951 on which the supply pipe 96 is provided and also serves as a fixture for fixing the miniaturization block 954 to the pressure- The two-phase pump 97 mixes water and air, and pressurizes the mixed fluid of water and air to a predetermined pressure. It is preferable to use a centrifugal pump for the two-phase pump 97, but any type of pump may be used as long as it is capable of feeding the gas-liquid two upstream. The water in which the two-phase upstream pump 97 is mixed with the air may be condensed water in the reaction tank 92 or may be a constant derived from the outside.

The refinement block 954 includes a block body 956 of approximately right angle polygonal column in plan view and four swiveling chambers 957, 957, 957, 957 formed equi-angularly around the central axis of the block body 956 And a right angle passage 958 formed concentrically with the central axis of the block body 956 and perpendicular to the line connecting the opposing vortex chambers 957 and 957. The refinement block 954 can be made of, for example, a synthetic resin such as a fluororesin. Further, according to conditions such as the object to be micronized or the temperature of the mixed fluid, the other minute synthetic resin may be used to manufacture the micronized block 954. Further, the fine block 954 may be made of a metal such as stainless steel.

The vortex chamber 957 of the micronization block 954 has a rotating body shape such that a hemisphere is connected to the end face of the cylinder and the cylinder is directed toward the outer diameter side of the micronization block 954, As shown in Fig. The two vortex chambers 957 opposed to each other are arranged in a straight line on the central axis to constitute a pair of vortex chambers. Further, the two vortex pairs are arranged so that the central axes connecting the vortex chambers 57 are orthogonal to each other. The right angle passage 958 extends in a direction perpendicular to the central axis connecting between the vortices 957 of the pair of vortex chambers. The tip of the hemispherical portion of the four vortex chambers 957 is communicated with the right angle passage 958. A portion of the right angle passage 958 located between the vortex chambers 957 of each pair of vortex chambers is an impingement chamber 958a in which the mixed fluid ejected from the vortex chamber 957 collides. The portion of the right angle passage 958 located closer to the discharge pipe 55 than the collision chamber 58a is the discharge passage 958b for discharging the mixed fluid finely divided in the collision chamber 58a. On the other hand, the end of the right angle passage 958 on the side of the supply pipe 96 is closed by the cap 961. An end of the discharge passage 958b of the right angle passage 958 is connected to a discharge pipe 955. [

In the refinement block 954, a supply path 959 for supplying a mixed fluid to the vortex chamber 957 is formed. The supply passage 959 is formed so as to draw a tangent to the inner peripheral surface when viewed in the central axis direction of the vortex chamber 957. The mixed fluid flows from the inlet opening 959a formed in the end surface of the miniaturization block 954 And the mixed fluid is discharged from the inlet opening 959b formed in the inner surface of the vortex chamber 957 to the room. Two supply paths 959 are provided at symmetrical positions with respect to the central axis of the vortex chamber 957 and the inlet openings 959a of the supply paths 959 are provided at both end surfaces of the miniaturization block 954 Respectively. 7A, the position in the plane direction of the supply path 959 on the side not shown in the cross section is indicated by imaginary lines. One of the two supply paths 959 may be closed depending on the flow rate or pressure of the mixed fluid supplied to the casing 2, the speed of the swirling flow to be formed in the vortex chamber 957, and the like. Alternatively, only one supply passage 959 may be formed in the finer block 954 with respect to one vortex chamber 957. The finer block 954 is provided with a supply path 959 so as to draw a tangent to the inner circumferential surface of the vortex chamber 957. When a mixed fluid of a predetermined pressure is filled outside the fine block 954, The mixed fluid flows into the rotary shaft 959, and a swirling flow can be formed in the vortex chamber 957 without using the movable portion. The vortex chamber 957 of the miniaturization block 954 is formed by forming a cylindrical hole having a bottom shape on four sides of one of the eight side surfaces of the block body 956 of the approximately right angle polygonal column, And the opening of the circular hole is closed by a lid 960 of a circular dome shape.

The nano bubble generator 94 operates as follows. First, the two-phase upstream pump 97 passes a mixed fluid formed by mixing condensed water and air in the reaction tank 92 through the supply pipe 96 and supplies the mixed fluid to the miniaturization nozzle 95. It is preferable that the bubble of the mixed fluid supplied to the refinement nozzle 95 by the two-phase upstream pump 97 has a diameter of 100 mu m or more and 3 mm or less. It is preferable that the mixed fluid supplied to the micronizing nozzle 95 has a flow rate of about 1 L / min or more and 50 L / min or less and a pressure of about 0.1 MPa to 5 MPa in the supply pipe 96. Particularly preferably, in the supply pipe 96, the pressure of the mixed fluid is about 0.5 MPa to 5 MPa. This mixed fluid is mixed with water having a flow rate of 0.8 L / min or more and 40 L / min or less and air having a flow rate of 0.2 L / min or more and 10 L / min or less.

The mixed fluid supplied to the miniaturization nozzle 95 through the supply pipe 96 is discharged into the pressure-resistant casing 951 and is filled between the inner surface of the pressure-resistant casing 951 and the outer surface of the miniaturization block 954. The mixed fluid filled between the pressure-resistant casing 951 and the finer block 954 flows into the supply passage 959 from the inlet opening 959a formed in the end face of the miniaturization block 954 and flows from the inlet opening 959b Is introduced into the chamber 957. The mixed fluid guided from the supply path 959 to the vortex chamber 957 is formed so that the supply path 959 is formed in the tangential direction with respect to the center axis of the vortex chamber 957, And becomes a swirling flow around the axis. The swirling flow of the mixed fluid formed in the vortex chamber 957 flows from the end of the cylindrical portion provided with the inlet opening 959b of the vortex chamber 957 toward the end of the hemispherical portion, Is increased. The mixed fluid reaching the end of the hemispherical portion located on the inner diameter side of the finer block 954 of the vortex chamber 957 is discharged into the collision chamber 958a of the right angle passage 958 while turning at high speed.

The swirling flow of the swirling flow generated in the two vortices 957 constituting the pair of vortex chambers is opposite to each other so that the swirling flow in the opposite direction in the collision chamber 958a of the right- do. These vortical flows are discharged from the vortex chamber 957 to the collision chamber 958a, and a swirling flow (or jet flow) is formed from the discharge port to turn into a conical shape. Since these turning classes swivel in the opposite directions, colliding with each other in the collision chamber 958a effectively breaks the air bubbles in the mixed fluid, thereby making the air bubbles finer. Further, by providing two pairs of vortex chambers, the swirling flow of the mixed fluid in each of the vortex chambers collides in the collision chamber 958a in an overlapping manner, whereby the air bubbles in the mixed fluid are effectively miniaturized, Nano bubbles of air bubbles of 900 nm or less are generated.

The nano bubbles generated in the miniaturization block 954 are discharged to the outside of the pressure-resistant casing 951 through the discharge pipe 955 and added to the condensed water in the reaction tank 92. The nano bubbles generated by the nano bubble generator 94 are diffused into the condensed water for a long time without rising to the surface of the condensed water because the diameter is 10 nm or more and 900 nm or less. Therefore, the aerobic microorganisms added to the condensed water can be effectively activated, and the organic matter of the condensed water can be effectively flocculated. Further, since the nano bubbles are dispersed into the condensed water for a long time, there is no need to ventilate the reaction tank 92, and the reaction tank 92 can be kept in a sealed state. Therefore, the spread of the odor contained in the condensed water can be effectively prevented.

The vacuum pump 5 is connected to the gas discharge pipe 34 of the gas-liquid separator 3 and is connected to the processing chamber 22 of the drier 2 through the gas-liquid separator 3 from the downstream side of the gas- Liquid separator 3 by sucking the air of the condenser 23 and the air in the process chamber 22. [ 8, the vacuum pump 5 is formed of a root type pump. The vacuum pump 5 includes a casing 51 having a gripe-type working chamber 52 having a transverse cross section, Of the rotor (53, 53). Further, the rotors 53 and 53 may have a triple-lobe shape other than a gourd shape. This vacuum pump 5 is rotationally driven in mutually opposite directions by a motor (not shown) connected to the rotary shafts 53a and 53a in a state where the two gutter-shaped rotors 53 and 53 are engaged with each other when viewed from the transverse section . The air that has entered from the intake port 54 formed in the upper portion of the casing 51 is congested in the space between the casing 51 and the rotors 53 and 53 to cause the rotation of the rotors 53 and 53 And is discharged from the exhaust port 55 formed in the lower portion of the casing 51. [ The vacuum pump 5 operates between the rotors 53 and 53 and between the rotor 53 and the casing 51 with a clearance of 0.1 mm or more and 0.5 mm or less so that no lubricant is required in the working chamber 52 Do. The casing 51 of the vacuum pump 5 is provided with a cooling water passage for circulating the cooling water as the cooling medium. The heat generated by the operation of the vacuum pump 5 is removed by the cooling water.

The vacuum pressure fermentation drying apparatus 1 of the present embodiment draws a mixture of condensed water and air in the treatment chamber 22 from the downstream side of the gas-liquid separator 3 by means of a vacuum pump 5, 3) so that only air is introduced into the vacuum pump 5. Therefore, the problem of damaging the vacuum pump 5 due to the corrosive substance contained in the condensed water can be prevented.

The ozone reaction tank 6 mixes ozone with air in the treatment chamber 22 separated from the gas-liquid separation device 3 to decompose odorous components and harmful substances contained in the air. The ozone reaction tank 6 is a chamber in which the air in the treatment chamber 22 sucked by the vacuum pump 5 is lowered and is supplied to the reaction passage through which the ozone generated by the ozone generator 61 is supplied and the reaction passage It has a filter installed.

The ozone generator 61 generates ozone from the atmosphere by silent discharge. The ozone generator 61 includes an oxygen concentration section for concentrating oxygen in the atmosphere to generate high-concentration oxygen, A pair of electrodes, and an AC power supply for applying a voltage between the electrodes. The ozone generator 61 introduces oxygen in the air and applies an alternating voltage of 4 to 10 kV to the high-concentration oxygen generated in the oxygen concentrator to generate silent discharge, thereby generating ozone. The ozone generation method of the ozone generator may be not only by silent discharge but also by surface discharge, plasma discharge, or photochemical action using ultraviolet rays.

The ozone reaction tank 6 guides the air exhausted from the exhaust port 55 of the vacuum pump 5 to the reaction path and supplies the ozone generated by the ozone generation device 61 to the reaction path, The odor component and the harmful substance contained in the flowing air are decomposed by the oxidation action of ozone. The air having passed through the reaction passage is removed by the filter, and is discharged to the atmosphere.

The cooling tower 7 cools the cooling water to be supplied to the vacuum pump 5 and the cooling water to be supplied to the dryer 2. [ Between the cooling tower 7 and the casing 51 of the vacuum pump 5, a circulation pipe for circulating cooling water is provided. Between the ring tower 7 and the condenser 23 of the dryer 2, there is provided a circulation pipe provided with a circulation pump for circulating cooling water. The cooling tower 7 includes a water tank for containing cooling water, a water spray pump for pumping up the cooling water in the water tank, a water spray nozzle for spraying the cooling water pumped by the water spray pump, And a fan for blowing with the filler. The return pipe for returning the cooling water from the vacuum pump 5 and the condenser 23 is connected to the water spray nozzle of the cooling tower 7. [ A transfer pipe for sending cooling water to the vacuum pump 5 and the condenser 23 is connected to the water tank of the cooling tower 7. [ A circulation pump 71 for sending cooling water to the vacuum pump 5 is interposed in the transfer pipe between the cooling tower 7 and the vacuum pump 5. A circulation pump 72 for sending cooling water to the dryer 2 is interposed in the transfer pipe between the cooling tower 7 and the drier 2. When the decompression fermentation drying apparatus 1 starts operating, the sprinkling pump and the fan of the cooling tower 7 are started, and the circulation pumps 71 and 72 installed in the circulation pipe are started. Thereby, the heat generated when the vacuum pump 5 is operated and the heat obtained by heat exchange with the steam by the condenser 23 are recovered and discharged from the cooling tower 7 to the atmosphere. The water tank of the cooling tower 7 is supplemented with water through the water supply valve 73 so that the evaporated cooling water is supplemented by the cooling operation.

The steam boiler 8 supplies the heating jacket 24 for heating the article to be treated by the dryer 2 and the steam as the heating medium for the heating agitator 25 to the dryer 2. The steam boiler (8) comprises a cylindrical casing formed of a flow-through boiler and having a combustion chamber formed therein, a burner installed at an upper portion of the combustion chamber to discharge the flame into the combustion chamber toward the downward direction, Respectively. The shape of the water tube may be a multi-tube type which is formed by a plurality of straight tubes arranged between an annular upper header and an annular lower header and extends in the vertical direction, or may be a single tube type in which a single tube is wound in a coil shape. In the water tube, the drain recovered in the drain recovery tank 81 is led by the drain pump 82. When the amount of the drain derived from the drain recovery tank 81 is small, the supply water is added to the steam boiler 8 via the water supply valve 83. Further, the drain recovery tank 81 is supplemented with the water supply valve 84, if necessary.

The drain recovery tank 81 recovers the steam and the drain after heating the object to be treated in the heating jacket 24 and the heating agitator 25 and extracts the drain and returns it to the steam boiler 8. The steam recovered from the heating jacket 24 and the heating stirrer 25 is discharged to the atmosphere as flash steam. Further, the flash steam may be cooled to generate condensed water, and the condensed water may be returned to the steam boiler 8.

Hereinafter, an example of treating an excess sludge as an object to be treated in the reduced-pressure fermentation drying apparatus 1 having the above-described structure will be described. Surplus sludge is produced by sewage treatment by an activated sludge process, and generally has a moisture content of 80% or more and 99% or less in a mass ratio.

First, the air in the treatment chamber 22 is sucked by the vacuum pump 5 and decompressed to a pressure lower than the atmospheric pressure. Here, it is preferable that the decompression value of the treatment chamber 22 is 0.03 to 0.098 MPa and the boiling point of water is lowered to about 90 to 68 캜. The decompression value refers to the amount of pressure to be reduced from atmospheric pressure. A steam of 0.2 to 0.7 MPa or 120 to 170 DEG C as a heating medium is supplied to the heating jacket 24 and the heating agitator 25 of the dryer 2 from the steam boiler 8. Here, since the pressure in the treatment chamber 22 is reduced, the temperature of the heating medium can be set lower than that at the normal pressure. In addition, since the heating temperature of the object to be treated is low, the microbes added in the treatment chamber 22 can be prevented from being killed, and deodorization can be performed stably and effectively.

Subsequently, the surplus sludge with high water as the object to be treated is charged into the treatment chamber 22 through the charging device 26 of the drier 2. Depending on the amount of the excess sludge, microorganisms are appropriately added. The object to be processed put in the treatment chamber 22 is heated by the heating jacket 24 and the heating agitating section 25 and agitated by the heating agitating section 25 under an air pressure lower than atmospheric pressure. The treatment chamber 22 is heated by the heating jacket 24 and the heating agitator 25 and is stirred by the heating agitator 25 because the air pressure is lower than atmospheric pressure and the boiling point of water is lowered to 100 ° C or lower. Water efficiently vaporizes the inclusion and dries quickly. In addition, the heating temperature of the heating jacket 24 and the heating agitator 25 can be set low by the decrease of the boiling point due to the decompression of the treatment chamber 22, and the microorganisms can be prevented from being killed by the high temperature, It is possible to effectively decompose the odor.

The water vapor generated from the object to be processed is condensed in the condenser 23 of the dryer 2 to be condensed water and sucked by the vacuum pump 5 together with the air in the processing chamber 22, Liquid separator 3, as shown in Fig. The condensed water and the air in which the mixture is separated by the gas-liquid separator 3 are separately treated by the different apparatuses of the wastewater treatment device 9 and the ozone-reactive layer 6. Therefore, it is possible to efficiently remove odors as compared with the conventional vacuum pressure fermentation drying apparatus in which condensed water and air are mixed with cooling water. Further, since the condensate and air are treated in the wastewater treatment device 9 and the ozone reaction layer 6, it is possible to prevent the spread of the odor as compared with mixing the condensed water and air into the cooling water in the cooling tower. Since the mixture of the condensed water and the air is guided to the gas-liquid separator 3 by the vacuum pump 5 connected to the downstream side of the gas-liquid separator 3, the condensed water contacts the operating portion of the vacuum pump 5 The deterioration of the vacuum pump 5 can be reduced.

Further, since the condensed water obtained by condensing the water of the object to be treated is treated by the activated sludge process in the wastewater treatment apparatus 9, the organic matter contained in the condensed water can be decomposed into aerobic microorganisms and the odor can be effectively removed. Further, since the wastewater treatment device 9 performs aerating by adding nano bubbles of air to the condensed water in the closed reaction tank 92, the condensed water can be treated by the activated sludge method while effectively preventing the spread of the odor .

Further, since the air sucked from the treatment chamber 22 is treated in the ozone reaction tank 6, the odor of the air can be effectively removed without diffusing to the surroundings.

The condensed water separated from the gas-liquid separator 3 is stored in the buffer tanks 4 and 4. The weight of the buffer tanks 4 and 4 is measured by the load cells 42 and 42, The weight of the dryer 2 immediately thereafter is measured by the load cells 29 and 29 and the degree of drying of the article to be processed is calculated by the controller 10 based on these measured values. Thus, the control device 10 functions as a drying degree calculator. By thus calculating the degree of drying of the article to be treated by the control device 10, the degree of drying of the article to be treated in the treatment chamber 22 can be improved without stopping the operation and opening the treatment chamber 22 to directly confirm the substance to be treated Can be accurately detected in real time while performing processing.

Since the condensed water generated by the drying of the object to be treated is divided and stored in the two buffer tanks 4 and 4, it is possible to measure the weight by the load cell 42 of the buffer tank 4, The condensed water can be continuously measured without being limited by the capacity of the buffer tank 4 by alternately discharging the condensed water in the two buffer tanks 4 and 4. [ Therefore, even if the water content of the object to be treated is large, the drying process can be continuously performed without being restricted by the buffer tank. Therefore, since the drying treatment is not interrupted for measuring the condensed water, the time required for the treatment can be shortened. Further, since the two buffer tanks 4 and 4 are alternately stored to measure the weight of the condensed water and the condensed water is discharged after the measurement, the amount of condensed water in the buffer tank 4 It is possible to make the size of the reduced pressure fermentation drying apparatus 1 small.

Cooling water, which is a cooling medium for both of the vacuum pump 5 and the condenser 23 which are operated simultaneously, is cooled by a single cooling tower 7, so that energy used for cooling can be reduced have.

In the above-described embodiment, the example in which excess sludge generated in a sewage treatment plant is treated as an object to be treated is described. However, the object to be treated is not limited to a head lake deposited on the lake or a sea floor, Or a food waste produced from a food factory, or a kitchen waste discharged from a general household.

1: Pressure-Fermentation Drying Device
2: dryer
3: Gas-liquid separator
4: Buffer tank
5: Vacuum pump
6: ozone reaction tank
7: Cooling Tower
8: Steam boiler
9: Wastewater treatment device
10: Control device

Claims (8)

A dryer having a treatment chamber into which organic matter to which microorganisms are added is introduced,
A heating unit installed in the dryer and heating the object to be processed,
An agitating part rotatably disposed in the treatment chamber of the dryer and stirring the object to be processed,
A condenser disposed in the processing chamber of the dryer for condensing water vapor generated from the object to be processed to generate condensed water;
A gas-liquid separator for guiding a mixture of condensed water in the condensing portion in the treatment chamber and air in the treatment chamber and separating the induced mixture into condensed water and air;
And a suction pump connected to a downstream side of the gas-liquid separator for sucking condensed water in the condenser in the process chamber and air in the process chamber toward the gas-liquid separator,
And a wastewater treatment device for treating the condensed water separated by the gas-liquid separation device by an activated sludge process. delete 2. The reduced-pressure fermentation drying device according to claim 1, further comprising an ozone reaction tank for treating the air separated by the gas-liquid separation device with ozone. The apparatus according to claim 1, further comprising: a condensed water storage tank for storing condensed water separated from the gas-
A storage tank weigher for measuring the weight of the condensate storage tank,
A dryer weigher for measuring the weight of the dryer,
And a drying degree calculator for calculating a degree of drying of the object to be processed in the treatment chamber of the dryer based on the measurement results of the storage tank weighing machine and the dryer weighing machine. The apparatus according to claim 4, further comprising: a plurality of said condensate reservoirs;
And a distribution valve interposed in a pipe connecting the gas-liquid separator and the plurality of condensate storage tanks and distributing the condensed water derived from the gas-liquid separator to each of the condensate storage tanks so that the plurality of condensed water storage tanks are sequentially filled By weight. The reduced-pressure fermentation drying apparatus according to claim 1, further comprising: a cooling medium for cooling the suction pump; and a cooler for cooling the cooling medium of the condensation section. The stirring device according to claim 1,
A hollow rotary shaft rotatably supported by a bearing installed in the dryer,
A spiral tube connected to the rotary shaft and wound around the outer diameter side of the rotary shaft in a spiral shape and communicating with the inside of the rotary shaft,
And a conveying blade which is disposed on an outer diameter side of the spiral tube and conveys the article to be processed in the treatment chamber toward a rotation axis direction. The waste water treatment system according to claim 1,
A reaction tank having a closed structure for condensing organic matters by adding aerobic microorganisms to the condensed water,
And a nano bubble generating device for generating nano bubbles of air added to the condensed water of the reaction tank.

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