KR20130035238A - Reduced-pressure fermenting and drying apparatus - Google Patents

Abstract

PURPOSE: A depressurized fermentation dryer is provided to efficiently remove odor generated from a target object, to prevent diffusion of odor and to prevent degradation due to a corrosive component generated from a target object. CONSTITUTION: A depressurized fermentation dryer(1) includes a dryer, a heater, a stir unit, a condensation unit(23), a gas liquid separation apparatus(3) and a suction pump. The dryer has a processing room(22) in which an organic target object with a microorganism added is injected. The heater heats the target object by being installed in the dryer. The stir unit is rotatably installed in the processing room of the dryer and stirs the target object. The condensation unit generates condensed water by condensing vapor generated from the organic waste. A mixed body of condensed water of the condensation unit and air of the processing room is induced and the gas liquid separation apparatus separates the induced mixture into condensed water and air. The suction pump is connected to a downstream side of the gas liquid separation apparatus and sucks up the condensed water in the condensation unit and the air of the processing room toward the gas liquid separation apparatus. [Reference numerals] (10) Control device; (3) Gas liquid separation apparatus; (4) Buffer tank; (5) Vacuum pump; (6) Ozone reactor; (61) Ozone generating apparatus; (7) Cooling tower; (8) Steam boiler; (81) Drain collecting tank; (9) Waste water disposal apparatus; (AA) Exhaust; (BB) Drainage;

Description

REDUCED-PRESSURE FERMENTING AND DRYING APPARATUS}

This invention relates to the reduced pressure fermentation drying apparatus which heats a to-be-processed object under reduced pressure and ferments it to dry.

An apparatus for drying organic to-be-processed substances with high water content, such as excess sludge generated in sewage treatment plants and kitchen waste, etc., which are heated under reduced pressure and fermented by drying under reduced pressure. The device is known. In this kind of reduced pressure fermentation drying apparatus, since the malodor of a to-be-processed object is comparatively strong, various deodorization measures are implemented.

The applicant is conventionally a reduced pressure fermentation drying apparatus subjected to odor countermeasures, and is provided in the processing chamber 111 and the upper portion of the processing chamber 111 in which the pressure is reduced by the vacuum pump 104 as shown in FIG. 9. On the outside of the processing chamber 111 and the condensing unit 115 for condensing the water vapor generated along with the drying of the processing object, the stirring heating device 114 which stirs and simultaneously heats the processing object in the processing chamber 111. It is proposed to have a heating jacket 113 provided, a steam boiler 106 for generating steam for heating, and a cooling tower 105 for cooling the cooling water that is a cooling medium of the condensation unit 115 (Patent Document 1). Reference).

This reduced pressure fermentation drying apparatus 101 dries the to-be-processed object, such as excess sludge which has a content rate of more than 95%, and vacuum-processes the to-be-processed object thrown into the process chamber 111 from the inlet 116. In the state which reduced the pressure by 104, it stirs by the stirring heating apparatus 114, heating by the heating jacket 113 and the stirring heating apparatus 114, and accelerates drying. In the stirring heating device 114, a plurality of stirring rods 114b extending in the radial direction are fixed to the rotary shaft 114a having a vapor passage therein, and the object to be processed is placed at the tip of the stirring rod 114b. It has the conveyance blade 114c which conveys in the direction parallel to the rotating shaft 114a, stirring. Both ends of the rotating shaft 114a are rotatably supported by the bearing provided in the wall of the casing 112 which forms the process chamber 111. The bearing which supports the rotating shaft 114a is formed so that steam can flow, and the steam supplied from the steam boiler 106 to the heating jacket 113 is comprised so that it may be guide | induced to the stirring heating apparatus 114 through a bearing. . The to-be-processed object after the drying process in the process chamber 111 is discharged | emitted from the discharge port 117 provided in the lower part of the casing 112. FIG.

The cooling tower 105 has a water tank 151 accommodating cooling water at a lower portion thereof, and the cooling water of the water tank 151 is pumped up to the sprinkling pump 155 to collect the filler 153 from the upper water spray nozzle 152. It is configured to spray toward. In this cooling tower 105, the condensate of the condensation part 115 and the air in the process chamber 111 are guide | induced by the vacuum pump 104 which pressure-reduces the process chamber 111, and the cooling water which flows in the cooling tower 105 is carried out. Are mixed in. The filler 153 of the cooling tower 105 is added with microorganisms having an odor decomposing action, and when the cooling water injected from the water spray nozzle 152 flows through the filler 153, it is caused by the wind from the fan 154. At the same time, the odor is decomposed by the microorganisms. In this manner, the cooling tower 105 performs cooling of the cooling water supplied to the condensation unit 115 and deodorization of the condensed water and the air discharged from the processing chamber 111.

Japanese Patent Application Laid-Open No. 2011-105816

However, in the conventional vacuum fermentation and drying apparatus, since the condensed water and air from the processing chamber 111 are guided to the cooling tower 105 and mixed with the cooling water, the object to be deodorized becomes large and the deodorization treatment efficiency is low. There is. In addition, there is a problem that condensed water or air odor induced in the cooling tower 105 leaks from the cooling tower 105 to the outside and diffuses around. Moreover, there exists a problem that the vacuum pump 104 which guides condensed water and air from the process chamber 111 to the cooling tower 105 tends to deteriorate by the corrosion component contained in condensed water or air.

Therefore, the subject of this invention can remove the odor which arises from a to-be-processed object efficiently, can prevent spreading a odor to surroundings, and also prevents deterioration by the corrosion component which arises from a to-be-processed object. It is providing the reduced pressure fermentation drying apparatus which can be performed.

In order to solve the said subject, the pressure reduction fermentation drying apparatus of this invention,

A dryer having a processing chamber into which an organic to-be-processed object to which microorganisms are added is put,

A heating unit installed in the dryer to heat the object to be processed;

A stirring unit rotatably disposed in the processing chamber of the dryer and for stirring the object to be processed;

A condenser for condensing water vapor generated from the organic waste to produce condensed water;

A mixture of condensate of the condensate and air in the processing chamber is guided, and a gas-liquid separator for separating the induced mixture into condensate and air;

It is connected to the downstream side of the said gas-liquid separator, and is provided with the suction pump which sucks the condensed water of the said condensate part, and the air of the said process chamber toward a gas-liquid separator.

According to the said structure, the organic to-be-processed object which microorganism added to the process chamber of a dryer is thrown in, and this to-be-processed object is stirred by the stirring part, heating by the heating part. In the processing chamber, air is sucked by the suction pump and the air pressure is lower than atmospheric pressure, whereby the boiling point of the substance is lowered. Therefore, the to-be-processed object stirred by the stirring part, while being heated by the said heating part, vaporizes the content efficiently and dries quickly. In addition, by lowering the boiling point due to the reduced pressure of the processing chamber, the heating temperature of the heating section can be set low, and the killing of microorganisms due to high temperature can be prevented, so that the odor can be effectively decomposed by the microorganisms. Water vapor generated from the object to be treated is condensed in the condensation unit to be condensed water, and is sucked by the suction pump together with the air in the processing chamber, so that the mixture of these condensed water and air is led to the gas-liquid separation device. The condensed water and air formed by separating the mixture in the gas-liquid separator are treated separately by different treatment devices. Therefore, the odor is removed more efficiently than the condensed water and the air mixed with the cooling water and treated. In addition, since the condensed water and the air sucked from the processing chamber can be efficiently treated, more condensed water can be sucked from the processing chamber, thereby increasing the drying efficiency of the object to be processed in the processing chamber. In addition, by treating the condensed water and the air in a closed processing device, it is possible to prevent the diffusion of the odor rather than mixing the condensed water and the air with the cooling water in the cooling tower. In addition, since the condensate and air are guided to the gas-liquid separator by the suction pump connected to the downstream side of the gas-liquid separator, the deterioration of the suction pump can be reduced. In addition, the said stirring part may serve as a heating part. That is, you may add so that a stirring function may be added to a stirring part and the to-be-processed object may be heated.

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 device, organic matter contained in the condensed water can be decomposed by an aerobic microorganism to effectively remove odors.

The reduced pressure fermentation drying apparatus of one Embodiment is equipped with the ozone reaction tank which processes the air isolate | separated by the said gas-liquid separation apparatus with ozone.

According to the said embodiment, by processing the air attracted from the process chamber and isolate | separated by the gas-liquid separation apparatus by an ozone reaction tank, organic substance contained in air can be oxidized by ozone, and an odor can be removed effectively.

A reduced pressure fermentation drying apparatus of one embodiment includes a condensate storage tank for storing condensed water separated by the gas-liquid separator,

A storage tank repeater for measuring the weight of the condensate storage tank;

A dryer repeater for measuring the weight of the dryer,

A dryness calculator which calculates the dryness of the to-be-processed object in the process chamber of the said dryer based on the measurement result of the said storage tank repeater and a dryer repeater.

According to the said embodiment, the condensed water separated by the gas-liquid separator is stored in a condensate storage tank, and the weight of this condensate storage tank is measured by a storage tank repeater. On the other hand, the weight of the dryer is measured by a dryer repeater. Based on the measurement result of the said storage tank repeater and a dryer repeater, the dryness calculator calculates the dryness of the to-be-processed object in the process chamber of a dryer. This dryness calculator is based on the weight of the condensed water which is water actually removed from the object, and can thus calculate the exact dryness of the object.

A reduced pressure fermentation drying apparatus of one embodiment includes a plurality of the condensed water storage tanks,

It is provided in the piping which connects the said gas-liquid separator and a some condensate storage tank, and is provided with the distribution valve which distributes the condensed water guide | induced from the said gas-liquid separator to each condensate storage tank so that the said some condensate storage tank may be filled sequentially.

According to the said embodiment, since the condensed water isolate | separated by the gas-liquid separator is divided into several condensate storage tanks, and stored, it is possible to measure the weight of the filled condensate storage tank individually by a storage tank weighing device sequentially. When the condensate of the condensate storage tank whose weight has been measured is discharged, the condensate can be accommodated again, so that a plurality of condensate storage tanks repeat the storage of the condensate, the measurement of the weight, and the discharge of the condensate in order to limit the capacity. The weight of the condensate can be measured without Therefore, when the condensate storage tank is filled, as in the case of storing the condensate in a single condensate storage tank, the suction of the condensate is not stopped for measuring the weight of the condensate storage tank and discharging the condensate. As a result, water vapor can be promptly removed from the inside of the process chamber in which the to-be-processed object is dried, and the to-be-processed object can be dried quickly. In addition, as compared with the case of storing the condensate in a single condensate storage tank, it is possible to store the condensate in another condensate storage tank while discharging the condensate from the filled condensate storage tank, so that all the condensate generated from the object can be stored. Small capacity condensate reservoirs can be used. Therefore, the size of a condensate storage tank can be made small and the structure of a pressure reduction fermentation drying apparatus can be miniaturized.

The pressure reduction fermentation drying apparatus of one Embodiment is equipped with the cooling medium which cools the said suction pump, and the cooler which cools the cooling medium of the said condensation part.

According to the said embodiment, the energy used for cooling can be reduced by cooling both cooling mediums with a single cooler with respect to the suction pump and condensation part which operate | move substantially simultaneously.

In the reduced pressure fermentation drying apparatus of one embodiment, the stirring portion,

A hollow rotating shaft rotatably supported by a bearing installed in the dryer;

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

It is arrange | positioned at the outer diameter side of the said spiral tube, and has a conveyance blade which conveys the to-be-processed object in the said process chamber toward a rotation axis direction.

According to the said embodiment, by rotating a stirring part as a heating medium, for example, supplying steam to a rotating shaft and a spiral tube inside, a to-be-processed object is heated by a rotating shaft and a spiral tube, by a feed blade, to a rotating shaft direction. Conveyed and stirred. Therefore, for example, the to-be-processed object, such as excess sludge whose content rate of water exceeds 95%, can be dried effectively and quickly.

As for the pressure reduction fermentation drying apparatus of one Embodiment, the said wastewater treatment apparatus,

A reaction vessel of a closed structure in which aerobic microorganisms are added to condensate to aggregate organic matters;

And a nanobubble generating device for producing nanobubbles of air added to the condensed water of the reactor.

According to the said embodiment, an aerobic microorganism is added to condensate in a reaction tank, and organic substance aggregates by the action of an aerobic microorganism. The nanobubbles of air generated by the nanobubble generating device are added to the condensed water of the reactor, whereby aeration is performed. Since the nanobubbles are stably diffused in the condensed water, the ventilation of the reaction tank is unnecessary even when added to the sealed reaction tank. Therefore, the problem that a bad smell spreads to the exterior from a reaction tank can be prevented. Therefore, this wastewater treatment apparatus can process the condensed water by the activated sludge method, without spreading odor to the surroundings. Here, a nano bubble means the bubble which has a diameter of 10 nm or more and 900 nm or less.

According to the present invention, the workpiece to which the microorganisms are added is stirred while heating in a processing chamber having an air pressure lower than atmospheric pressure, and the vapor of the processing chamber is condensed and discharged from the condensing unit. By the discharge action, deodorization and drying of the workpiece can be performed quickly and effectively. In addition, a mixture of condensed water condensed in the condensation unit and air in the processing chamber is sucked by a draw pump to guide the gas-liquid separator, and the condensed water and the air separated by the gas-liquid separator are treated separately by different processing apparatuses. In addition, the odor contained in condensate and air can be removed efficiently. In addition, since the condensed water and the air sucked from the processing chamber can be efficiently treated, more condensed water can be sucked from the processing chamber, thereby increasing the drying efficiency of the object to be processed in the processing chamber. In addition, by treating the condensed water and the air in a closed processing device, it is possible to prevent the diffusion of the odor rather than mixing the condensed water and the air with the cooling water in the cooling tower. In addition, since the condensate and air are guided to the gas-liquid separator by the suction pump connected to the downstream side of the gas-liquid separator, the deterioration of the suction pump can be reduced.

BRIEF DESCRIPTION OF THE DRAWINGS The block diagram which shows the pressure reduction fermentation drying apparatus of embodiment of this invention.
2 is a longitudinal sectional view schematically showing a dryer of a reduced pressure fermentation drying apparatus.
3 is a cross-sectional view schematically showing a dryer of a reduced pressure fermentation drying apparatus.
4A is a longitudinal sectional view schematically showing the gas-liquid separation device.
4B is a cross-sectional view schematically showing the gas-liquid separation device.
5 is a schematic diagram showing a wastewater treatment device.
6 is a cross-sectional view showing a miniaturization nozzle of the nanobubble generating device of the wastewater treatment device.
7A is a plan cross-sectional view of a refinement block of the refiner nozzle.
7B is a longitudinal cross-sectional view of the miniaturization block.
8 is a cross-sectional view schematically showing a vacuum pump.
9 is a block diagram showing a conventional reduced pressure fermentation drying apparatus.

EMBODIMENT OF THE INVENTION Hereinafter, embodiment of this invention is described in detail, referring an accompanying drawing.

BRIEF DESCRIPTION OF THE DRAWINGS It is a block diagram which shows the whole structure of the pressure reduction fermentation drying apparatus of embodiment of this invention. This reduced pressure fermentation drying apparatus 1 processes surplus sludge which content rate of water exceeds 95% as a to-be-processed object. The pressure reduction fermentation drying apparatus 1 includes a dryer 2 having a processing chamber 22 into which a target object is introduced, a gas-liquid separator 3 through which condensed water is guided from the dryer 2, and a gas-liquid separator. Two buffer tanks 4 and 4 as condensate storage tanks for storing the condensate separated in (3), a vacuum pump 5 as a suction pump connected to the downstream side of the gas-liquid separator 3, and a vacuum pump 5 In the ozone reactor 6 connected to the downstream side of the head), a cooling tower 7 as a cooler for supplying cooling water as a cooling medium to the vacuum pump 5 and the dryer 2, and steam as a heating medium to the dryer 2. It consists of the steam boiler 8 which supplies the oil, and the wastewater treatment apparatus 9 which processes condensed water.

FIG. 2 is a longitudinal sectional view showing a state of cutting in the vertical direction along the longitudinal direction of the dryer 2, and FIG. 3 is a cross-sectional view illustrating a state of cutting in the vertical direction along the short direction of the dryer 2.

As shown in FIG.2 and FIG.3, the dryer 2 has the substantially cylindrical casing 21 which has the process chamber 22 inside, and the heating jacket 24 formed along the wall surface of the lower part of the process chamber 22. As shown in FIG. ) And a heated stirring portion 25 as a stirring portion disposed in the processing chamber 22.

In the center of the upper part of the casing 21, the input device 26 which injects a to-be-processed object is formed, and in the other end part of the lower part of the casing 21, the discharge port 22b which discharges a to-be-processed object is formed. . The feeding device 26 of the casing 21 has a funnel-shaped inlet 261 having an upper end opened and an airlock 262 provided at the lower end of the inlet 261. In the airlock 262, a closed valve is provided at the inlet 261 side and the processing chamber 22 side of the object to be processed, and after the object is injected from the inlet 261, the inlet 261 side is provided. By closing the closed valve at the same time and opening the closed valve on the processing chamber 22 side, the object to be processed is introduced into the processing chamber 22 without raising the air pressure in the processing chamber 22 lower than atmospheric pressure.

The heating stirring portion 25 includes two hollow rotary shafts 251 supported at both ends by bearings 27 and 27 provided on both end faces of the casing 21 and the outer diameter side of the rotary shaft 251. The spiral pipes 255 and 258 and the plurality of rectangular transfer blades 256 and 259 arranged on the outer circumferential side of the spiral pipes 255 and 258 and having one side of 5 to 10 cm are provided. The rotating shaft 251 and the spiral tubes 255 and 258 communicate with each other inside. Steam as a heating medium supplied from the steam boiler 8 is supplied to the rotating shaft 251 through the steam supply pipe 264 connected to one end of the rotating shaft 251, and from this rotating shaft 251 the spiral tube 255, 258) steam is supplied. 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 chains 284. ) Is connected. The rotational force of the motor 281 is transmitted to the rotation shaft 251 through the chain 284, so that the heating stirring portion 25 is driven to rotate.

Steam is supplied to the rotating shaft 251 and the spiral tubes 255 and 258 of the heating stirring unit 25, and the heating stirring unit 25 is driven to rotate, thereby rotating the rotating 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 stirred while being transferred from the center to both ends or from both ends to the center. The direction in which the conveying blades 256 and 259 convey the object to be processed can be selected by selecting the rotational direction of the heating stirring part 25 from either the direction from the center to both ends or the direction from the both ends to the center. It is.

The helix tubes 255 and 258 of the heating stirring part 25 are the upstream helix tube 255 located in the upstream side in the steam flow of the rotating shaft 251, and the downstream helix tube located downstream. And 258. The upstream spiral tube 255 and the downstream spiral tube 258 are formed so that winding directions of a spiral are mutually opposite. The upstream end part of the upstream spiral pipe 255 is formed in the upstream straight pipe part 255a extended in the radial direction of the rotating shaft 251, and this upstream straight pipe part 255a is the upstream side of the rotating shaft 251. It is connected to the end. The downstream end part of the upstream spiral pipe 255 is formed in the downstream straight pipe part 255b extended in the radial direction of the rotating shaft 251, and this downstream straight pipe part 255b of the longitudinal direction of the rotating shaft 251 is carried out. It is connected to the center. Moreover, the upstream end part of the downstream spiral tube 258 is formed in the upstream straight pipe part 258a extended in the radial direction of the rotating shaft 251, and this upstream straight pipe part 258a is the length of the rotating shaft 251. It is connected to the center of the direction. The downstream end of the downstream spiral tube 258 is formed in the downstream straight pipe portion 258b extending in the radial direction of the rotary shaft 251, and the downstream straight pipe portion 258b is located on the downstream side of the rotary shaft 251. It is connected to the end.

As shown by the arrow V1, this heating and stirring unit 25 is supplied with steam introduced from the steam boiler 8 to an end portion on the upstream side of the rotating shaft 251 through the steam supply pipe 264, thereby rotating shaft 251. At the same time, the inside flows into the upstream straight pipe portion 255a of the upstream spiral pipe 255 as indicated by arrow G1. Steam flowing into the upstream straight pipe portion 255a is returned from the downstream straight pipe portion 255b to the rotation shaft 251 via the upstream spiral pipe 255 as indicated by arrow G2. In addition, the steam in the rotation shaft 251 flows into the upstream straight pipe portion 258a of the downstream spiral pipe 258 as shown by arrow G3, and the downstream straight pipe portion 258b through the downstream spiral pipe 258. Is returned to the rotating shaft 251 as indicated by arrow G4. In this way, steam flows inside the rotary shaft 251, the upstream spiral tube 255, and the downstream spiral tube 258 to thereby rotate the rotary shaft 251, the upstream spiral tube 255, and the downstream spiral tube 258. The to-be-processed object which contacts the outer surface of () is heated. The steam which flowed through the rotating shaft 251, the upstream spiral pipe 255, and the downstream spiral pipe 258 is shown by the arrow V2 through the steam discharge pipe 265 connected to the downstream end of the rotating shaft 251. Similarly, it is discharged to the outside of the dryer 2 and is returned to the drain recovery tank 81 with the drain which generate | occur | produced on the path | route of these vapors.

As for the feed vanes 256 and 259, the attachment angle with respect to the spiral tubes 255 and 258, and the mounting position of the spiral tubes 255 and 258 in the radial direction are adjustable. Specifically, when viewed in the radial direction of the spiral tubes 255 and 258, the feed vanes 256 and 259 can be adjusted at a desired angle around the radial direction. The feed vanes 256 and 259 are mounted in a state inclined with respect to the axis of the rotating shaft 251 when viewed in the radial direction of the spiral tubes 255 and 258. According to the magnitude | size of the inclination-angle of the conveyance vanes 256 and 259, the ratio of the action | movement which transfers a to-be-processed object to the direction of the rotating shaft 251, and the action which mixes a to-be-processed object is adjusted. Specifically, when the inclination angles of the feed vanes 256 and 259 with respect to the rotary shaft 251 are large, the action of conveying a workpiece in the direction of the rotary shaft 251 is large, and the feed vanes with respect to the rotary shaft 251 are large. When the inclination angles of (256, 259) are small, the effect of kneading the workpiece is increased. Thus, by adjusting the inclination angles of the transfer blades 256 and 259, the heating stirring part 25 can exhibit the effect according to the to-be-processed object.

In addition, the feed vane 256 attached to one spiral tube 255 and the feed vane 259 attached to the other spiral tube 258 set the inclination direction in the radial direction opposite to each other. It is preferable. Thereby, as the heating stirring part 25 rotates, it is toward the center from the both ends of the rotating shaft 251 of the heating stirring part 25 according to the rotation direction of the heating stirring part 25, or a heating stirring part The to-be-processed object is conveyed toward the both ends from the center of the rotating shaft 251 of (25). Therefore, by controlling the rotation direction of the heating stirring part 25, the direction to convey a to-be-processed object can be controlled.

The adjustment of the mounting position of the feed vanes 256 and 259 with respect to the helix tubes 255 and 258 can change the distance spaced apart from the helix tubes 255 and 258 of the feed vanes 256 and 259. When the distance from the spiral pipes 255 and 258 of the transfer blades 256 and 259 increases, the leading edge in the radial direction of the spiral pipes 255 and 258 of the transfer blades 256 and 259 becomes the process chamber 22. ), The clearance between the leading edges of the transfer blades 256, 259 and the inner wall surface of the processing chamber 22 is reduced. The heating jacket 24 is provided in the wall of the process chamber 22, and when a to-be-processed object progresses, the to-be-processed object adheres to the inner wall surface of the process chamber 22 by the heat of the heat jacket 24. FIG. When adhering the workpiece proceeds, a problem occurs that the workpiece is stuck to the inner wall by the heat of the heating jacket 24. Here, by adjusting the clearance between the leading edges of the transfer blades 256 and 259 and the inner wall surface of the processing chamber 22, the workpiece to be adhered to the inner wall surface of the processing chamber 22 can be scraped off, Sticking to the wall can be prevented. In this way, by adjusting the mounting positions of the feed vanes 256 and 259, the feed vanes 256 and 259 can function as a scraper.

On the side surface of the casing 21, a maintenance window (not shown) extending in the longitudinal direction is provided, and the maintenance window is opened to adjust the mounting angles of the feed vanes 256 and 259 of the heating stirring part 25, Maintenance of adjustment of a mounting position, exchange of conveyance vanes 256, 259, etc. is performed.

The heating jacket 24 is provided along the casing 21 so that the lower part of the rotation area of the heating stirring part 25 may be enclosed as shown in FIG. The heating jacket 24 is connected to a steam supply pipe 24a at one end in the longitudinal direction, and is connected to a steam discharge pipe 24b at the center in the longitudinal direction. As indicated by the arrow V1, steam induced from the steam boiler 8 is supplied to the heating jacket 24 through the steam supply pipe 24a, flows through the heating jacket 24, and removes the target object in the processing chamber 22. After heating, as shown by arrow V3, it is discharged out of the dryer 2 through the steam discharge pipe 24b, and it returns to the drain recovery tank 81 with the drain which generate | occur | produced on the path | route of these steam.

The upper part of the casing 21 is provided with the condensation part 23 which condenses the vapor evaporated from the to-be-processed object. The condensation part 23 has the cooling water supply chamber 231 formed in the other end side of the casing 21, and the cooling water discharge chamber 232 formed in the one end side of the casing 21. The cooling water supply pipe 233 to which the cooling water is guided from the cooling tower 7 is connected to the cooling water supply chamber 231. A cooling water discharge pipe 234 for returning the cooling water to the cooling tower 7 is connected to the cooling water discharge chamber 232. Between the cooling water supply chamber 231 and the cooling water discharge chamber 232, a plurality of cooling water pipes 235, 235,..., Extending in the axial direction of the casing 21 are interposed, and these cooling water pipes 235, 235,. Cooling water in the coolant supply chamber 231 flows to the coolant discharge chamber 232 through the. The plurality of cooling water pipes 235, 235, ... are divided and arranged in both sides of the upper direction of the upper part in the casing 21, as shown in the cross-sectional view of FIG. At the side and the bottom of the plurality of divided cooling water pipes 235, 235, ..., respectively, the collection tanks 236 and 236 which collect condensate are provided, respectively. Inside the sump 236, a suction pipe 237 that sucks air in the process chamber 22 together with the condensate is in communication.

In the processing chamber 22 of the dryer 2, an enzyme acting on the to-be-processed object exists. Enzymes are obtained by collecting microorganisms such as indigenous bacteria and fermented bacteria that grow in nature such as the sea, mountains, and land, and injecting them into the processing chamber 22. In particular, in order to decompose and deodorize organic sludges, such as surplus sludge, the enzyme produced | generated by the microbe in various plants and animals or soil is effective. The flora and fauna in which the bacteria inhabit includes wormwood, wild grass, herbs, beach grass, stalks, large forest soil, forest soil, fish, seaweed, fruits, pineapples, apples, tangerines, loquats and grapes. It is preferable to culture | cultivate and to use the microbe which reproduces in these in rice bran or sawdust. In this embodiment, since the to-be-processed object is stirred over 30 minutes-3 hours at the heat medium temperature of 60-80 degreeC under reduced pressure of 0.03-0.098 Mpa of pressure reduction, the microorganism which grows and ferments under such conditions is sent to the process chamber 22. It is preferable to add. In addition, a decompression value means the magnitude | size of the pressure reduced from atmospheric pressure.

The enzyme present in the process chamber 22 by the action of microorganisms may be one of the following or a plurality of enzymes. In addition, in the parenthesis following each enzyme, the substance to which each enzyme functions is described. Alcohol dehydrogenase (alcohol), lactate dehydrogenase (lactose), glucose 6-phosphate dehydrogenase (sugar), aldehyde dehydrogenase (aldehyde), L-asphatate beta semialdehyde, NADP Oxidoreductase (aldehyde), glutamate dehydrogenase (amino acid), asparagine acid semialdehyde dehydrogenase (amino acid), NADPH2 cytochrome C reductase (NADP), glutathione dehydrogenase (glutathione), tre Haloose phosphate synthetase (sugar), polyphosphate kinase (ATP), ethanolamine phosphate cytidyl transferase (CTP), trehalose phosphatase (saccharides), metalthio phospho glycelate phosphate Fatase (glycerine), inulinase (inulin), β-mannosidase (saccharides), uridine nucleosidase (amino acids), cytosine deaminase (cytosine), methylcysteine synthetase (amino acids), Aspartic acid synthetase ( ATP), succinic acid dehydrogenase (succinic acid), aconic acid hydrogenase (citric acid), fumarate hydrogenase (malonic acid), malate dehydrogenase (malonic acid), citric acid synthase (acetyl CoA) , Isocitric acid dehydrogenase (citric acid), LSNADP oxidase (citric acid), monoamine oxidase (amine), histaminase (amine), pyruvate decarboxylase (oxo acid), ATPase (ATP ), Nucleotide pyrophosphatase (nucleic acid), endopolyphosphatase (ATP), ATP phosphohydrolase (ATP), orotidine 5 phosphate decarboxylase (orotidine). By adding the microorganism which produces | generates at least 1 of these to a to-be-processed object, it can decompose effectively the to-be-processed object which consists of many kinds of organic substance components.

The dryer 2 which has each said component has the load cells 29 and 29 as a dryer repeater provided between the support member of a lower end part, and a base. The load cells 29 and 29 are connected to the control device 10. The control apparatus 10 measures the weight by operating the load cells 29 and 29 before and after input of the workpiece, and calculates the weight of the workpiece based on the measured values of the load cells 29 and 29.

4A is a longitudinal cross-sectional view showing the gas-liquid separation device 3, and FIG. 4B is a cross-sectional view showing the gas-liquid separation device 3. As shown in FIG. 4A, the gas-liquid separation device 3 has a substantially cylindrical shape and includes a longitudinally long casing 31 arranged in a vertical direction with a central axis. An introduction tube 32 which guides a mixture of condensed water and air in the processing chamber 22 from the section 23 is fixed toward the tangential direction of the casing 31 in the cross section. The casing 31 is provided with a liquid discharge pipe 33 for discharging condensate separated from the mixture at the lower end, while a gas discharge pipe 34 for discharging air separated from the mixture is provided at the upper end. This gas-liquid separation apparatus 3 accommodates the cyclone part 35, the demister 36, and the filter part 37 in the casing 31 from the lower part upwards.

The cyclone part 35 is located in the center of the partition plate 353 and the swivel chamber 351 formed between the lower part of the casing 31, and the partition plate 353 fixed across the casing 31, and fixed. It has an exhaust cylinder 352 that is fixed and protrudes into the swing chamber 351. In the swinging chamber 351 of the cyclone portion 35, as shown in FIG. 4B, a mixture guided through the introduction pipe 32 flows into the swinging shape, and condensed water and air are separated by centrifugal force. The air separated from the mixture is led to the demister 36 upward through the exhaust column 352. On the other hand, the condensed water separated from the mixture flows downward along the inner surface of the casing 31 and is discharged from the discharge hole 33a open at the center of the bottom surface of the swing chamber 351, and through the liquid discharge pipe 33. Guided to wastewater treatment device 9. The demister 36 is formed of a wire mesh formed by stacking a plurality of metal meshes, and is disposed above the partition plate 353 adjacent to the outlet of the exhaust cylinder 352 of the cyclone portion 35. When the air separated from the mixture in the cyclone section 35 and guided from the exhaust tube 352 passes through the demister 36, fine particles of condensed water contained in the air are generated in the gap between the fibers of the demister 36. Captured by capillary action. The filter portion 37 is a cylindrical annular filter element formed of a lump of resin or cellulose fibers between the annular plate-shaped upper support plate 371 and the disc-shaped lower support plate 372 provided at the lower end of the gas discharge pipe 34. The 337 and the filter cloth 374 surrounding the outer peripheral surface of the filter element 373 are clamped and comprised. When the air passing through the demister 36 passes through the filter cloth 374 and the filter element 373 of the filter portion 37, the fine particles and the dust 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 is vacuumed through the gas discharge pipe 34 communicating with the cavity 375. Aspirated by the pump (5). The condensed water trapped by the demister 36 or the filter unit 37 falls inside the casing 31 and is discharged from the liquid discharge pipe 33.

The buffer tank 4 is a tank which once stores the condensed water separated by the gas-liquid separator 3 before performing 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 buffer tank 4 is provided with load cells 42 and 42 as storage tank repeaters for measuring the weight of the buffer tank 4 and water level meters 43 and 43 for detecting the level of condensate in the tank. Opening and closing valves 44 and 44 are interposed in the discharge pipes of the buffer tanks 4 and 4. The switching valve 41, the load cells 42 and 42, the water gauges 43 and 43, and the opening and closing valves 44 and 44 are connected to the control device 10. The two buffer tanks 4 operate as follows by the control of the control apparatus 10. First, the condensed water from the gas-liquid separator 3 is led to 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. Upon detecting that the buffer tank 4 is filled based on the detection signal of the water gauge 43, the control device 10 operates the switching valve 41 to switch the supply of condensed water to the other buffer tank 4. do. At the same time, the load cell 42 of one 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 control apparatus 10 opens the drain valve 44 of one buffer tank 4, and discharges condensed water. When the buffer tank 4 is detected to be empty based on the detection signal of the water gauge 43, the control apparatus 10 closes the drain valve 44. FIG. Thus, by supplying condensate, measuring the weight, and draining alternately between the two buffer tanks 4, the weight of the large amount of condensate is continued by the relatively small buffer tanks 4 and 4. It is supposed to measure. In addition, two or more buffer tanks 4 may be provided as long as it is plural.

The control apparatus 10 is a dryer 2 immediately after the addition of the weight of the condensed water measured by the load cells 42 and 42 of the buffer tanks 4 and 4 after the processing of the to-be-processed object started, and into the process chamber 22. It has a function as a dryness calculator which calculates the dryness of the to-be-processed object based on the weight of the to-be-processed object measured by the load cells 29 and 29 of (). Since the measured values of the load cells 29 and 29 of the dryer 2 include the weights of the drains accumulated in the heating jacket 24 and the heating stirring part 25 as the processing of the target object proceeds, It is difficult to calculate the degree of dryness of the treatment based only on the weight of the dryer 2. Therefore, the weight of the dryer 2 is measured immediately after the injecting of the to-be-processed object, and when the process of a to-be-processed object advances, the weight of the buffer tanks 4 and 4 is measured. Based on the weight of the to-be-processed object immediately after preparation calculated | required from these measured values, and the weight of the condensed water in the process, the dryness of a to-be-processed object is calculated correctly.

The wastewater treatment apparatus 9 which processes the condensed water discharged | emitted from the buffer tank 4 removes organic substance by the active sludge method. As shown in FIG. 5, the wastewater treatment apparatus 9 is aerobic to the pre-sedimentation tank 91 for precipitating relatively large fine particles contained in the condensed water sent from the buffer tank 4 and the condensate from the pre-sedimentation tank 91. A microorganism is added, and the reaction tank 92 which aggregates organic substance in an aeration environment by the action of an aerobic microorganism, and the precipitation tank 93 after depositing the organic substance which aggregated in the reaction tank 92 are provided. The pre-sedimentation tank 91, the reaction tank 92, and the post-sedimentation tank 93 are sealed structures formed of tanks, and are configured to prevent diffusion of odors. The nanobubble generating device 94 is provided in the reactor 92. The nanobubble generating device 94 generates nanobubbles that are bubbles of air having a diameter of 10 nm or more and 900 nm or less. The reactor 92 is configured to add the condensed water to the condensed water by adding the nanobubbles generated by the nanobubble generating device 94 to the condensed water. After the organic matter is removed from the settling tank 93, the disinfectant such as chlorine or sodium hypochlorite is added and then discharged to the outside. In addition, it is not necessary to provide the all settling tank 91 in the wastewater treatment apparatus 9.

The nanobubble generating device 94 provided in the reaction tank 92 includes a refinement nozzle 95 that is settled in the condensate of the reaction tank 92, and a supply pipe 96 that supplies a mixed fluid of air and water to the refinement nozzle 95. ) And a two-phase pump 97 for producing a two-phase mixed fluid of air and water. FIG. 6 is a cross-sectional view showing the micronization nozzle 95 of the nanobubble generating device 94, FIG. 7A is a cross-sectional view of a micronization block that is a component of the micronization nozzle 95, and FIG. 7B is a longitudinal cross-sectional view of the micronization block. to be.

As shown in FIG. 6, the refinement | miniaturization nozzle 95 is substantially comprised by the substantially spherical pressure-resistant casing 951 and the refinement | miniaturization block 954 built in the pressure-resistant casing 951. As shown in FIG. The mixed fluid is pumped into the pressure resistant casing 951 from the two-phase pump 97 through a supply pipe 96 connected to the pressure resistant casing 951. The mixed fluid pumped into the pressure resistant casing 951 flows into the micronized block 954 under pressure, and air is refined to the outside of the pressure resistant casing 951 through the discharge pipe 955 connected to the micronized block 954. Discharged. The discharge pipe 955 is inserted and fixed to the side opposite to the side where the supply pipe 96 of the internal pressure casing 951 is installed, and serves as a fixture for fixing the miniaturization block 954 to the internal pressure casing 951. The two-phase pump 97 mixes water and air, and pumps 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 can pump the gas-liquid two-phase. The water mixed with the air by the two-phase pump 97 may be condensed water in the reaction tank 92 or a constant derived from the outside.

The miniaturization block 954 includes four block chambers 957, 957, 957, 957 formed at an equiangular angle around the central axis of the block main body 956 and the block main body 956 of a substantially octagonal pillar in plan view. ) And a right angle passage 958 formed concentrically with the central axis of the block main body 956 and perpendicular to a line connecting the opposing turning chambers 957 and 957 are formed therein. The miniaturization block 954 can be manufactured with synthetic resin, such as a fluororesin, for example. In addition, you may manufacture the refinement | miniaturization block 954 using another synthetic resin according to the object to refine | miniaturize, and conditions, such as the temperature of a mixed fluid. Further, the miniaturization block 954 may be manufactured from a metal such as stainless steel.

The turning chamber 957 of the miniaturization block 954 has a shape of a rotating body in which a hemisphere is connected to the end face of the cylinder, and the cylindrical part faces the outer diameter side of the miniaturization block 954 and the hemisphere part is the miniaturization block 954. It is formed to face the inner diameter side of. Two opposed swinging chambers 957 have a central axis arranged in a straight line to form a pair of swinging chambers. In addition, the two swinging chamber pairs are arrange | positioned so that the center axis | shaft which connects between each pair of swinging chambers 57 may orthogonally cross. The right angle passage 958 extends in the direction perpendicular to the central axis which connects between the swing chambers 957 of each swing chamber pair. In the right angle passage 958, the tip ends of the hemispheres of the four swing chambers 957 communicate with each other. 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 located on the discharge pipe 55 side of the right angle passage 958 rather than the collision chamber 58a is a discharge passage 958b for discharging the mixed fluid refined in the collision chamber 58a. On the other hand, the end part of the supply pipe 96 side of the right angle passage 958 is closed by the cap 961. An end portion of the discharge passage 958b of the right angle passage 958 is connected to the discharge tube 955.

The refinement block 954 is provided with a supply passage 959 for supplying a mixed fluid to the swing chamber 957. The supply path 959 is formed to draw a tangent of the inner circumferential surface when viewed in the direction of the central axis of the turning chamber 957, and the mixed fluid flows from the inlet opening 959a formed in the end surface of the miniaturization block 954. The mixed fluid is discharged into the room from the inflow opening 959b formed on the inner surface of the swing chamber 957. Two supply paths 959 are provided at positions symmetrical with respect to the central axis of the swinging chamber 957, and the inlet openings 959a of each supply path 959 are provided at both end faces of the miniaturization block 954. Each is formed. In the sectional view of FIG. 7A, the position in the planar direction of the supply path 959 on the side not shown in the cross section is shown by an imaginary line. In addition, one of the two supply paths 959 may be closed depending on the flow rate and pressure of the mixed fluid supplied to the casing 2 or the speed of the swirl flow to be formed in the swing chamber 957. Alternatively, only one supply path 959 may be formed in the miniaturization block 954 with respect to one swing chamber 957. The refinement block 954 is provided with a supply path 959 so as to draw a tangent to the inner circumferential surface of the swinging chamber 957. When the mixed fluid having a predetermined pressure is filled outside the refinement block 954, the supply is performed. Mixed fluid flows into the furnace 959 to form swirl flow in the swing chamber 957 without using the movable portion. The revolving chamber 957 of the miniaturized block 954 forms a cylindrical hole having a spherical bottom in four sides of one interval among the eight sides of the block main body 956 of the substantially octagonal column, The opening of this cylindrical hole is closed by the cover 960 of a circular dome shape.

The nanobubble generating device 94 operates as follows. First, the two-phase pump 97 supplies the mixed fluid formed by mixing the condensed water and the air in the reaction tank 92 to the refinement nozzle 95 through the supply pipe 96. It is preferable that the bubble of the mixed fluid supplied to the refinement | miniaturization nozzle 95 by the two-phase pump 97 is 100 micrometers or more and 3 mm or less in diameter. In the supply pipe 96, the mixed fluid supplied to the miniaturization nozzle 95 preferably has a flow rate of about 1 L / min or more and 50 L / min or less and about 0.1 MPa or more and 5 MPa or less. Particularly preferably, in the supply pipe 96, the pressure of the mixed fluid is about 0.5 MPa or more and 5 MPa. In this mixed fluid, water at a flow rate of 0.8 L / min or more and 40 L / min or less and air at a flow rate of 0.2 L / min or more and 10 L / min or less are mixed.

The mixed fluid supplied to the miniaturization nozzle 95 through the supply pipe 96 is discharged into the pressure resistant casing 951 and 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 miniaturization block 954 flows into the supply path 959 from the inlet opening 959a formed in the end face of the miniaturization block 954 and pivots from the inflow opening 959b. Guided into yarn 957. The mixed fluid guided from the supply passage 959 to the swinging chamber 957 is centered in the swinging chamber 957 because the supply passage 959 is formed in a tangential direction with respect to the central axis of the swinging chamber 957. It is a swirl flow around the axis. Swirl flow of the mixed fluid formed in the revolving chamber 957 flows from the end of the cylindrical portion provided with the inflow opening 959b of the revolving chamber 957 toward the end of the hemisphere, and the flow velocity is reduced by the reduction of the revolving diameter accompanying this. Is increased. The mixed fluid which has reached the end of the hemisphere located on the inner diameter side of the miniaturization block 954 of the revolving chamber 957 is discharged to the collision chamber 958a of the right angle passage 958 while turning at high speed.

The turning directions of the swirl flows generated in the two swing chambers 957 constituting the swing chamber pairs are opposite directions, whereby the swing flows in opposite directions collide with each other in the collision chamber 958a of the right-angle passage 958. do. These swirling flows are discharged from the swinging chamber 957 to the collision chamber 958a, and the swirling flow which turns in cone shape from the discharge port is formed. Since these swing classifications rotate in opposite directions, they collide with each other in the collision chamber 958a, whereby air bubbles in the mixed fluid are effectively destroyed, and air bubbles are made fine. In addition, since the two swinging chamber pairs are provided, the swirl flow of the mixed fluid of each swinging chamber pair overlaps in the collision chamber 958a, and the air bubbles in the mixed fluid are effectively refined, and the diameter is 10 nm or more. Nano bubbles, which are air bubbles of 900 nm or less, are produced.

In this way, the nanobubble generated in the miniaturization block 954 is discharged to the outside of the pressure-resistant casing 951 through the discharge pipe 955 and added to the condensed water of the reaction tank 92. Since the nanobubbles generated in the nanobubble generating device 94 have a diameter of 10 nm or more and 900 nm or less, they diffuse into the condensed water for a long time without rising to the surface of the condensed water. Therefore, the aerobic microorganisms added to the condensate can be effectively activated, and the organic matter of the condensate can be effectively aggregated. In addition, since the nanobubbles are dispersed in the condensed water for a long time, there is no need to vent the reaction tank 92, and the reaction tank 92 can be kept in a sealed state. Therefore, it is possible to effectively prevent the diffusion of odor contained in the condensed water.

The vacuum pump 5 is connected to the gas discharge pipe 34 of the gas-liquid separator 3, and is the processing chamber 22 of the dryer 2 via the gas-liquid separator 3 from the downstream side of the gas-liquid separator 3. By sucking the air in, the mixture of the condensed water of the condensation part 23 and the air of the processing chamber 22 is guide | induced to the gas-liquid separator 3. The vacuum pump 5 is formed by a root pump, and as shown in FIG. 8, a casing 51 having a circumferentially shaped working chamber 52 and two circumferentially shaped shapes accommodated in the working chamber 52. Has rotors 53 and 53. In addition to the shape of the gourd, the rotors 53 and 53 may have a three-lobed shape. The vacuum pump 5 is driven to rotate in opposite directions by a motor (not shown) connected to the rotating shafts 53a and 53a in a state where two circumferential rotors 53 and 53 are engaged in a cross-sectional view. . In connection with this, the air which entered from the intake port 54 formed in the upper part of the casing 51 is confined to the space between the casing 51 and the rotors 53 and 53, and accompanies the rotation of the rotors 53 and 53. Is moved downward, and is discharged | emitted from the exhaust port 55 formed in the lower part of the casing 51. FIG. Since the vacuum pump 5 operates with a clearance of 0.1 mm or more and 0.5 mm or less between the rotors 53 and 53 and between the rotor 53 and the casing 51, no lubricant is required in the operating 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, and the cooling water removes heat generated by the operation of the vacuum pump 5.

The reduced pressure fermentation drying apparatus 1 of this embodiment sucks the mixture of condensed water and air of the process chamber 22 from the downstream side of the gas-liquid separator 3 by the vacuum pump 5, and the condensed water is a gas-liquid separator ( Separated from 3) only air is directed to the vacuum pump 5. Therefore, the problem that the vacuum pump 5 is damaged by the corrosive substance contained in condensate can be prevented.

The ozone reaction tank 6 mixes ozone with air in the processing chamber 22 separated by the gas-liquid separator 3 to decompose odor components and harmful substances contained in the air. The ozone reactor 6 is provided with a reaction passage through which the air of the processing chamber 22 sucked by the vacuum pump 5 flows down and to which the ozone generated by the ozone generator 61 is supplied, and downstream of the reaction passage. Has a filter installed.

The ozone generator 61 generates ozone from the atmosphere by silent discharge, and is disposed in an oxygen concentrating unit for concentrating oxygen in the atmosphere to produce high concentration oxygen, and a discharge space supplied with oxygen from the oxygen concentrating unit. It has a pair of electrodes and AC power supply which applies a voltage between electrodes. The ozone generator 61 introduces oxygen in the air and applies an alternating voltage of 4 to 10 kW to the high concentration oxygen generated in the oxygen concentrating unit to generate an silent discharge, thereby generating ozone. The ozone generating method of the ozone generating device may be a surface discharge, a plasma discharge, or a photochemical action using ultraviolet rays, in addition to the silent discharge.

The ozone reaction tank 6 guides the air discharged from the exhaust port 55 of the vacuum pump 5 to the reaction passage, and supplies ozone generated by the ozone generator 61 to the reaction passage, thereby providing a reaction passage. The odor component and the harmful substance contained in flowing air are decomposed | disassembled by the oxidation action of ozone. The air passing through the reaction passage removes particulates by a filter and is discharged to the atmosphere.

The cooling tower 7 cools the cooling water supplied to the vacuum pump 5 and the cooling water supplied to the dryer 2. Between the cooling tower 7 and the casing 51 of the vacuum pump 5, the circulation pipe which circulates a cooling water is provided. Moreover, the circulation pipe provided with the circulation pump which circulates a cooling water between the ring tower 7 and the condensation part 23 of the dryer 2 is provided. The cooling tower 7 receives a water tank accommodating cooling water, a sprinkling pump for sprinkling the cooling water of the water tank, a sprinkling nozzle for spraying the coolant pumped by the sprinkling pump, and the cooling water sprayed from the sprinkling nozzle to promote evaporation. It has a filler to make and a fan which blows air with a filler. The return pipe which returns cooling water from the vacuum pump 5 and the condensation part 23 is connected to the watering nozzle of the cooling tower 7. The conveying piping which sends cooling water to the vacuum pump 5 and the condensation part 23 is connected to the water tank of the cooling tower 7. In the transfer piping between the cooling tower 7 and the vacuum pump 5, the circulation pump 71 which sends cooling water to the vacuum pump 5 is interposed. In the transfer piping between the cooling tower 7 and the dryer 2, the circulation pump 72 which sends cooling water to the dryer 2 is interposed. When the pressure reduction fermentation drying apparatus 1 starts operation, the watering pump and the fan of the cooling tower 7 start, and the circulation pumps 71 and 72 installed in the circulation pipe start. Thereby, the heat which generate | occur | produces when the vacuum pump 5 operates, and the heat which the condensation part 23 heat-exchanged with steam are collect | recovered, and are discharged | emitted from the cooling tower 7 to air | atmosphere. Replenishment water is added to the water tank of the cooling tower 7 via the water supply valve 73, and it is made to replenish the cooling water evaporated with cooling operation.

The steam boiler 8 supplies the dryer 2 with steam as a heating medium of the heating jacket 24 and the heating stirring part 25 which heat the to-be-processed object by the dryer 2. The steam boiler 8 is formed of a perfusion boiler, has a cylindrical casing in which a combustion chamber is formed therein, a burner installed at an upper portion of the combustion chamber to emit flames in the combustion chamber downward, and a water pipe arranged around the combustion chamber. Has The form of the water pipe may be a multi-pipe type formed by a plurality of straight pipes disposed between the annular upper header and the annular lower header and extending in the vertical direction, or may be a single pipe type in which a single pipe is wound in a coil shape. The drain recovered in the drain recovery tank 81 is led to the water pipe by the drain pump 82. When the amount of the drain drawn from the drain recovery tank 81 is small, the make-up water is added to the steam boiler 8 through the water supply valve 83. In addition, replenishment water is added to the drain recovery tank 81 via a water supply valve 84 as necessary.

The drain recovery tank 81 recovers the steam and the drain after the heating of the object to be processed by the heating jacket 24 and the heating agitator 25, extracts the drain, and returns the steam to the steam boiler 8. The steam recovered from the heating jacket 24 and the heating stirring portion 25 is discharged to the atmosphere as flash steam. In addition, the flash steam may be cooled to generate condensed water, and the condensed water may be returned to the steam boiler 8.

Hereinafter, the example which processes the surplus sludge as a to-be-processed object by the reduced pressure fermentation drying apparatus 1 of the said structure is demonstrated. The surplus sludge is produced by sewage treatment by the activated sludge method, and is generally high moisture having a water content of 80% or more and 99% or less by mass ratio.

First, air in the processing chamber 22 is sucked by the vacuum pump 5 and reduced in pressure to a pressure lower than atmospheric pressure. Here, it is preferable to make the pressure reduction value of the process chamber 22 into 0.03-0.098 Mpa, and to reduce the boiling point of water to about 90-68 degreeC. In addition, a decompression value means the magnitude | size of the pressure reduced from atmospheric pressure. In addition, 0.2-0.7 MPa and 120-170 degreeC steam are supplied to the heating jacket 24 and the heating stirring part 25 of the dryer 2 from the steam boiler 8 as a heating medium. 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. Moreover, since the heating temperature of the to-be-processed object is low, the death of the microorganism added in the process chamber 22 can be prevented, and deodorization can be performed stably and effectively.

Subsequently, surplus sludge of high moisture as a to-be-processed object is thrown into the process chamber 22 via the input device 26 of the dryer 2. Depending on the amount of surplus sludge added, microorganisms are appropriately added. The to-be-processed object thrown into the process chamber 22 is stirred by the heating stirring part 25, heating by the heating jacket 24 and the heating stirring part 25 under air pressure lower than atmospheric pressure. Since the boiling point of water lowers to 100 degrees C or less because air pressure is lower than atmospheric pressure in the process chamber 22, the to-be-processed object stirred by the heating stirring part 25, being heated by the said heating jacket 24 and the heating stirring part 25. The water vaporizes efficiently, and dries rapidly. In addition, since the heating temperature of the heating jacket 24 and the heating stirring part 25 can be set low by the fall of the boiling point by the pressure reduction of the process chamber 22, since the death of the microorganism by high temperature can be prevented, The odor can be decomposed effectively.

Water vapor generated from the object to be treated is condensed in the condensation unit 23 of the dryer 2 to be condensed water, and is sucked by the vacuum pump 5 together with the air in the processing chamber 22, and a mixture of these condensed water and air Is led to the gas-liquid separator 3. The condensed water and the air in which the mixture is separated by the gas-liquid separator 3 are treated separately by different devices of the wastewater treatment device 9 and the ozone reaction layer 6. Therefore, the malodor can be removed more efficiently than the conventional pressure reduction fermentation drying apparatus which mixes and processes condensed water and air to cooling water. Further, since the condensed water and the air are treated by the wastewater treatment device 9 and the ozone reaction layer 6, the diffusion of the odor can be prevented rather than mixing the condensed water and the air with the cooling water in the cooling tower as in the prior art. In addition, since the mixture of condensed water and 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 part of the vacuum pump 5. Since it does not, the deterioration of the vacuum pump 5 can be reduced.

In addition, since the condensed water formed by condensing the water of the object to be treated is treated by the activated sludge method in the wastewater treatment apparatus 9, organic matter contained in the condensed water can be decomposed into an aerobic microorganism to effectively remove odors. In addition, the wastewater treatment device 9 adds nanobubbles of air to the condensed water of the sealed reaction tank 92 to perform aeration, so that the condensed water can be treated by an active sludge method while effectively preventing the diffusion of odors. .

Moreover, since the air sucked from the process chamber 22 is processed by the ozone reactor 6, it can remove effectively, without spreading the odor of air to surroundings.

Further, the condensed water separated by the gas-liquid separator 3 is stored in the buffer tanks 4 and 4, and the weight of the buffer tanks 4 and 4 is measured by the load cells 42 and 42, and the object to be processed is added. The weight of the dryer 2 immediately after it is measured by the load cells 29 and 29, and the dryness of a to-be-processed object is calculated by the control apparatus 10 based on these measured values. Thus, the control apparatus 10 functions as a dryness calculator. By calculating the dryness of the workpiece by the control device 10 in this manner, the degree of drying of the workpiece within the processing chamber 22 without stopping the operation and opening the processing chamber 22 to directly check the workpiece. Can be accurately detected in real time while performing the processing.

In addition, since the condensate generated due to drying of the object to be treated is stored in two buffer tanks 4 and 4, the condensate after the measurement of the weight by the load cell 42 of the buffer tank 4 and the measurement is completed. By discharging, the condensed water can be measured continuously without being limited by the capacity of the buffer tank 4 by alternately performing the two buffer tanks 4 and 4. Therefore, even if there is much water content of a to-be-processed object, drying process can be performed continuously, without being restrict | limited by the buffer tank. Therefore, the drying process is not interrupted for the measurement of condensed water, so that the time required for the treatment can be shortened. In addition, the two buffer tanks 4 and 4 are stored alternately to measure the weight of the condensate, and after the measurement, the condensate is discharged. The size can be reduced, and the structure of the reduced pressure fermentation drying apparatus 1 can be miniaturized.

In addition, since the cooling water, which is a cooling medium for both of them, is cooled in the single cooling tower 7 for the vacuum pump 5 and the condenser 23 which operate substantially simultaneously, the energy used for cooling can be reduced. have.

In the above embodiment, an example of treating surplus sludge generated in a sewage treatment plant as a to-be-processed object has been described. However, the to-be-processed material is a waste discharged from a head or a head deposited on the bottom of an appeal or sea. In addition, a high-moisture organic to-be-processed object which arises in various industries, such as the food residue discharged from a food factory and the kitchen waste discharged from a general household, may be sufficient.

1: reduced pressure fermentation drying device
2: dryer
3: gas-liquid separator
4: buffer tank
5: vacuum pump
6: ozone reactor
7: cooling tower
8: steam boiler
9: wastewater treatment device
10: control unit

Claims (8)

A dryer having a processing chamber into which an organic to-be-processed object to which microorganisms are added is put,
A heating unit installed in the dryer to heat the object to be processed;
A stirring unit rotatably disposed in the processing chamber of the dryer and for stirring the object to be processed;
A condenser for condensing water vapor generated from the organic waste to produce condensed water;
A gas-liquid separator for introducing a mixture of condensate from the condenser and air in the treatment chamber, and separating the induced mixture into condensate and air;
And a suction pump connected to the downstream side of the gas-liquid separator, for sucking condensed water from the condensation unit and air from the processing chamber toward the gas-liquid separator. The pressure reduction fermentation drying apparatus according to claim 1, further comprising a wastewater treatment apparatus for treating the condensed water separated by the gas-liquid separator by an activated sludge method. The pressure reduction fermentation drying apparatus according to claim 1, further comprising an ozone reactor for treating the air separated by the gas-liquid separator with ozone. The condensate storage tank according to claim 1, further comprising: a condensate storage tank for storing condensate separated by the gas-liquid separator;
A storage tank weigher for measuring the weight of the condensate storage tank;
Dryer weight measuring device for measuring the weight of the dryer,
And a dryness calculator for calculating the dryness of the object in the treatment chamber of the dryer based on the measurement results of the storage tank weigher and the dryer weigher. The method of claim 4, wherein the plurality of condensate storage tank,
A distribution valve interposed between the gas-liquid separator and a plurality of condensate storage tanks, and distributing condensate derived from the gas-liquid separator to each condensate storage tank so that the plurality of condensate storage tanks are sequentially filled. The reduced pressure fermentation drying apparatus made into. The pressure reduction 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 unit. The method of claim 1, wherein the stirring unit,
A hollow rotating shaft rotatably supported by a bearing installed in the dryer;
A spiral tube connected to the rotating shaft and wound around the outer diameter side of the rotating shaft in a spiral shape and communicating with an inside of the rotating shaft;
It is arrange | positioned at the outer diameter side of the said spiral tube, and has a feed vane which conveys the to-be-processed object in the said process chamber direction to the rotation axis direction, The pressure reduction fermentation drying apparatus characterized by the above-mentioned. The wastewater treatment apparatus of claim 2,
A reaction vessel of a closed structure in which aerobic microorganisms are added to condensate to aggregate organic matters;
And a nanobubble generating device for producing nanobubbles of air added to the condensed water of the reactor.

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