JP2011218296A - Powder production apparatus - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a powder production apparatus for pulverizing raw materials with high energy efficiency.SOLUTION: The powder production apparatus is provided with: the pipe lines connected from a container 21 to a pulverizer 22 and also connected from the pulverizer 22 to the container 21; a first circulation path 101 forming the circulation path of a fluid between the container 21 and the pulverizer 22; a pipe line connected from the container 21 to a powder collecting device 30, an exhaust treatment device 40 and a temperature adjuster 50 for a circulating air current; a pipe line connected from the adjuster 50 to the container 21; and a second circulation path 201 which forms the circulation path of the fluid between the container 21, powder collecting device 30, exhaust treatment device 40 and the adjuster 50 to provide the double fluid circulation paths. The raw material is circulated together with the circulating air current between the pulverizer 22 and the container 21 using the first circulation path 101 to be powderized. The powder guided from the first circulation path 101 together with the circulating air current is captured and collected by the powder collecting device 30 in the second circulation path 210. The temperature of the circulating air current is adjusted by the adjuster 50, and the air current is introduced into the container 21 to be circulated to the second circulation path 201.

Description

The powder production apparatus of the present invention uses as raw materials food materials (eg, vegetables, grains, beans, moss, mushrooms, fish, seaweed, tea leaves, medicinal herbs), hydrous food processing by-products (eg, raw okara, fermented fish residue, tea). Gallons, coffee lees, cocoons, apple squeezes, liquor lees, etc.), biomass (wood, bamboo, grass, rice straw, etc.), sludge or water-containing waste, chemical products (chemicals, plastics, rubber, pharmaceuticals, cosmetics, Paints, etc.). The present invention relates to a powder production apparatus capable of performing a drying process, a pulverization process, a sterilization process, a heat cooking process, a sludge incineration process, a purification of a chemical product as a raw material, an evaporation removal recovery of a solvent, and the like.
In particular, the calorie of the raw material is effectively used as heat energy, and the heat generated by the steam generated during the drying / pulverization process is also effectively used as heat energy. The present invention relates to a powder manufacturing apparatus that can efficiently dry and pulverize and burn a raw material and recover energy by recovering and reusing heat.

  With increasing environmental awareness, efforts to reduce CO2 emissions continue. Drying and powder processing of raw materials are required for all industries such as food industry, pharmaceutical industry, petrochemical industry, waste treatment. Along with increasing environmental awareness, efforts to reduce CO2 emissions continue, and various technologies have been proposed for drying and powder processing of raw materials that consume large amounts of energy.

If a raw material containing moisture is used as a powder with a pulverizer as it is, it cannot be pulverized due to adhesion and blockage in the apparatus due to adhesion by moisture. Therefore, generally, first, the raw material is dried with a drying device, the obtained dry raw material is pulverized with a pulverizer to obtain a powder, and the obtained powder is further classified with a classifier to obtain a product powder.
Since the apparatus is composed of each of a drying apparatus, a pulverizing apparatus, and a classification apparatus, the entire apparatus becomes large and complicated. Large box dryers are generally used to dry large size raw materials, but large box dryers require a long drying time, and the raw materials are exposed to hot air for a long time. Therefore, the quality is easily deteriorated, and the heat quantity of the exhaust gas after drying is not recovered and released to the atmosphere, so that the thermal efficiency is poor.

Moreover, in food pulverization processing, even if sterilization is performed, there is a high possibility that bacterial contamination of the powder occurs in the process of transporting the dried raw material after drying and in the process of powder processing in the pulverizer and classifier.

Raw materials of coarsely crushed pieces containing a large amount of water are combined by water to form a lump, but food by-products such as okara, tea husk, and coffee cake are similar to this.
In the prior art, fluidized / air dryers are known in which the food by-products and the like are used as raw materials, the bonds due to moisture in the raw materials are divided, and the raw materials are fluidized and dried in an air stream.

For example, a fluidized / air dryer disclosed in Japanese Patent Application Laid-Open No. 2007-78207 is known. FIG. 10 is a view showing the fluidized / air dryer shown in FIG. 1 of the publication. In addition, the number in a figure is the number of FIG. 1 of the gazette.
As shown in FIG. 10, the fluid / air dryer disclosed in Japanese Patent Application Laid-Open No. 2007-78207 is provided in the rotating region of the stirring blade 4 that rotates along the upper surface of the perforated plate 3 provided in the lower part of the casing 1 (container). The granular crushing medium 11 is arranged, the raw material is introduced into the casing 1, hot air is supplied from the lower part, the rotary blade is rotated, the crushing medium 11 and the raw material are stirred, and the raw material is dried while crushing. The dried and lightened raw material is discharged from the upper part of the casing 1 by an exhaust flow and is captured by a cyclone dust collector or a bag filter. Exhaust gas after capturing the dry material is released to the atmosphere.

Next, as a powder manufacturing apparatus using superheated steam as a heat medium, a water-containing organic waste drying system described in JP-A-2009-154100 is known. FIG. 11 is a block diagram of the water-containing organic waste drying system shown in FIG. 1 of the publication. In addition, the number in a figure is the number of FIG. 1 of the gazette.
As shown in FIG. 11, the drying system 1 includes a waste storage tank 2 that stores water-containing organic waste W such as water-containing organic sludge, a superheated steam generator 3 that generates superheated steam S, and a waste W and superheat. A crushing air dryer 4 that breaks and breaks the bonds between the raw material particles due to moisture while directly contacting the steam S, and a supply device 5 that supplies the waste W to the crushing air dryer 4. , A blower 6 for supplying the superheated steam S to the crushing air dryer 4, a cyclone 7 for solid-gas separation of the exhaust gas from the crushing air dryer 4, and a bug filter 8 for recovering dust contained in the steam discharged from the cyclone 7. And a dry waste storage tank 9 for storing the dry organic waste W ′ recovered from the cyclone 7 and the bag filter 8, and a circulation blower 10. The blower 6 is provided on the steam discharge side of the superheated steam generator 3 and supplies the superheated steam S to the crushing air dryer 4. The crushing air dryer 4 is provided to dry the waste W with the superheated steam S supplied from the superheated steam generator 3 through the blower 6 while crushing the waste W. The crushing air dryer 4 is a chain blow type dryer, and includes a waste W supply port at the top and a superheat steam S supply port from the superheated steam generator 3 at the bottom. And superheated steam S are brought into contact in countercurrent. In addition, a rotation shaft 4a and a striking chain 4b that is fixed to the rotation shaft 4a, extends in the horizontal direction by centrifugal force and rotates with the rotation of the rotation shaft 4a, and crushes the waste W are provided inside. In place of the chain striking crushing airflow dryer 4, a rod striking type, cage mill type or swivel type drier having a round bar attached horizontally instead of the chain can be used.

Next, the sludge treatment in the prior art will be described.
Sludge is difficult to treat due to its stickiness, and large-capacity sludge treatment is forcibly incinerated using a lot of auxiliary fuel.
For example, in the prior art, an apparatus using a circulating fluidized bed furnace described in JP-A-11-37410 is known as a sludge treatment apparatus.
FIG. 12 is a view showing the sludge treatment apparatus shown in FIG. 1 of the publication. In addition, the number in a figure is the number of FIG. 1 of the gazette.
As shown in FIG. 12, the circulating fluidized bed furnace includes a riser (furnace body) 1 for charging a combustion target such as industrial waste, drying, pyrolyzing, and burning, as shown in FIG. A cyclone (fluid medium separator) 2 for separating a fluid medium such as silica sand discharged together with the combustion gas and the incineration ash from the combustion gas and the incineration ash, and the fluid medium separated by the cyclone 2 are returned to the lower part of the riser 1. A downcomer (fluid medium return pipe) 3 and a pneumatic valve (fluid medium circulation amount control valve) 4 for adjusting the circulation amount of the fluid medium returned from the downcommer 3 to the riser 1 are configured. A fluidized air supply port 11, a first combustion object supply port 13, a second combustion object supply port 14, an auxiliary fuel supply port 12, and the like are provided at the lower portion of the riser 1. Industrial air, auxiliary fuel, industrial waste, and the like are supplied, and the supplied industrial waste is burned while being dried, crushed and pyrolyzed by a fluid medium such as silica sand kept at a high temperature. In this riser 1, the combustion object and auxiliary fuel complete most of drying, pulverization, thermal decomposition, and combustion, and become combustion exhaust gas, which is led to the cyclone 2 together with the fluid medium. In this cyclone 2, combustion exhaust gas and incineration Fluid medium separation from ash is performed. Further, auxiliary fuel such as oil and gas is supplied from the auxiliary fuel supply port 12 so that the temperature in the furnace becomes a temperature suitable for combustion.

JP 2007-78207 A JP 2009-154100 A Japanese Patent Laid-Open No. 11-37410

The conventional apparatus described above has the following problems.
First, the fluidized / air dryer disclosed in Japanese Patent Application Laid-Open No. 2007-78207 has a complicated structure with a stirring blade at the bottom, and uses industrial glass beads or the like as a heat medium. There is a risk of breakage of the glass beads. Moreover, in order to make the heavy raw material stagnated in the lower part flow, a large air volume is required. However, since the hot air is a one-through air stream introduced from the lower part of the casing 1 and exhausted from the upper outlet, The large amount of heat is also released into the atmosphere along with the exhaust. This device has the function of crushing and drying the raw material lump, but does not have the function of crushing it into powder. When trying to obtain a powder, a pulverizer is required.

  Next, there is a problem with the water-containing organic waste drying system described in JP-A-2009-154100. In this equipment, high water content organic matter and superheated steam supplied from the boiler are brought into countercurrent contact in the dryer to obtain a dry matter, but inside it, the high water content organic matter is crushed by rotating the chain. Is complicated and requires time for crushing and drying. In addition, the raw material lump is divided while falling downward from above, and is contacted with superheated steam flowing from below to dry. The dried product is discharged together with the superheated steam from the upper part, but the size of the discharged raw material varies, and there is a possibility that the undried product is discharged. In addition, a large amount of air current is required for the flow of a heavy raw material lump. Although the steam circulates, the air flow in the dryer is one-through. Therefore, the circulation amount increases, the entire apparatus becomes large, the apparatus heat dissipation loss increases, and the power of the blower 6 and the circulation blower 10 also increases. In addition, since the superheated steam generated in the boiler is used as a drying heat source, the entire amount of superheated steam supplied from the boiler and the steam generated by drying high water content organic matter is discharged out of the system, and large heat energy is released. End up. In the first place, this apparatus has a crushing function that breaks the bond between the raw material particles due to moisture, but does not have a pulverizing function that makes the raw material particles smaller than the true particle size.

  Next, there is a problem with the sludge treatment apparatus using the circulating fluidized bed furnace described in JP-A-11-37410. In this equipment, circulating fluid sand heated to high temperature by combustion of auxiliary fuel is blown up and collided with sludge with a high moisture content, which has a strong adhesive bonding force, put into the furnace, and collided to lumpy sludge. , Burn while flowing and drying. A hot air flow with a large flow velocity is required for blowing up, circulating and flowing the sludge mass. This requires a large amount of auxiliary fuel along with a large amount of combustion air. More air is required for complete combustion of sludge, the air-fuel ratio is large, the combustion efficiency is poor, and a large amount of combustion exhaust gas is generated. Since the exhaust gas from ash and sludge is contained in the combustion exhaust gas, the exhaust gas treatment device is not shown, but is complicated and large-scale. In other words, it can be said that a large amount of energy is wasted in the case where the raw material that can be used as a resource when dried is forcibly incinerated using auxiliary fuel.

In addition, when a raw material that can be said to be in a dry state is pulverized to produce powder, the product quality is deteriorated due to oxidation due to heat generated by the pulverizer.

  In addition, when evaporative separation and recovery of solvents and the like of chemical products in the chemical industry and pharmaceutical industry in the prior art are studied, they also have problems. In the apparatus of the prior art, mainly a heated inert gas such as nitrogen gas is used to evaporate and remove the solvent from the product, capture and recover the product after removing the solvent, and cool the heated gas exhaust gas after collecting the product. The vaporized solvent is liquefied and recovered, the inert gas after the solvent recovery is introduced and heated in a heater, the heated inert gas is introduced into a drying container, and the inert gas is circulated. However, a large air flow is required for the flow of heavy products including solvents in the container, and the air flow in the container is one-through, so the circulating air flow rate is large, the device is large, and the heat dissipation loss is large. The power of the blower also increases. As above, there is room for improvement.

  In view of the above problems, the present invention provides a powder manufacturing apparatus that solves the above-described conventional problems and pulverizes raw materials with high energy efficiency and manufactures high-quality powder in a short time with a simple apparatus. The purpose is to do.

In order to achieve the above object, the powder production apparatus of the present invention comprises:
A pipe connected from the first discharge port of the container to the suction port of the pulverizer; and a pipe connected from the discharge port of the pulverizer to the first inlet of the container; the container and the pulverizer A first circulation path forming a fluid circulation path therebetween;
A conduit connected to the circulating airflow temperature controller from the second outlet of the container via the powder recovery device and the exhaust treatment device, and a conduit connected to the second inlet of the container from the circulating airflow temperature controller A double fluid circulation path comprising a second circulation path that forms a fluid circulation path between the container, the powder recovery device, the exhaust treatment device, and the circulation airflow temperature controller,
In the first circulation path, the raw material introduced from the outside is circulated between the pulverizer and the container together with the circulating air flow to advance powdering of the raw material,
In the second circulation path, the powder guided from the first circulation path together with the circulating airflow is captured and recovered by the powder recovery device, and the temperature of the circulating airflow after capturing the powder is controlled by the circulating airflow temperature controller. The powder manufacturing apparatus is characterized in that the circulating air flow is circulated through the second circulation path by adjusting the pressure and introducing the second air flow into the second inlet of the container.
Here, the crusher includes a casing provided with the suction port and the discharge port, an impeller installed in the casing, and a screen, and the impeller sends the circulating airflow to the suction port. More suction and delivery to the discharge port.
Further, in the first circulation path, a swirling flow of the circulating airflow is formed in the container, the raw material is classified by the centrifugal force by the swirling flow and the circulating airflow, and pulverized to a predetermined size by the classification. The discharged powder is discharged from the second discharge port of the container together with the circulating airflow, and the powder that has not yet been pulverized to the predetermined size is discharged from the first discharge port of the container to the first circulation path. To circulate.

  The raw material of the powder production apparatus of the present invention includes food raw materials such as vegetables, cereals, beans, potatoes, mushrooms, fish, seaweed, tea leaves, medicinal herbs, raw okara, fermented fish residue, tea gala, coffee lees, coffee Any of food processing by-products such as dashigara, apple pomace, sake lees, or combinations thereof, and any of biomass such as wood, thinned wood, pruned wood, bamboo, grass, rice straw or combinations thereof, and sludge Or any of the hydrous wastes or combinations thereof, and any chemical product such as chemicals, plastics, rubbers, pharmaceuticals, cosmetics, paints and the like.

By the said structure, the powder manufacturing apparatus of this invention becomes a confluence | merging airflow by which two circulation airflows merged in the container by providing a double circulation path. Even if it is a heavy raw material that contains moisture, a heavy material with sticky mass, a heavy raw material that is large in size, or a light raw material, the combined airflow will flow into the container and circulate through the first circuit. Thus, it is possible to perform an appropriate pulverization process according to the properties of the respective raw materials, and it is possible to produce high-quality powder.
Further, by providing the double circulation path, the circulation flow rate of the second circulation path is reduced. In the present invention, the circulating airflow in the second circulation path is also recycled without being released to the atmosphere. High energy efficiency is achieved, and the size of the device can be reduced, thereby reducing the overall cost of the device. Lower cost and continuous production of powder can be achieved in a short time.

Here, in the configuration of the powder production apparatus of the present invention, it is preferable that the circulating air flow is any one of superheated steam, nitrogen, and an inert gas.
The raw material is pulverized in a closed system that is shut off from the outside world. By using an inert gas such as superheated steam or nitrogen in the circulating airflow as described above, quality deterioration due to oxidation can be prevented. High quality powder. Moreover, by using nitrogen for the circulating airflow, a powder free from quality deterioration due to oxidation can be produced.

  Next, in the powder production apparatus of the present invention, the circulating airflow is heated by the circulating airflow temperature controller, the raw material is pulverized by the heated circulating airflow, the raw material is dried, and the raw material It is preferable that any one or combination of sterilization treatment, cooking of the raw material, roasting of the raw material, and vaporization treatment of the liquid containing the raw material is performed.

Next, in the powder manufacturing apparatus of the present invention, the powder captured and recovered by the powder recovery apparatus, or the powder molded into pellets is used as a fuel for heating the circulating airflow in the apparatus. It is preferable.
It is preferable to generate steam from the feed water based on the surplus combustion heat value of the fuel.
Further, it is preferable that superheated steam is used as the circulating air flow, and an amount commensurate with the steam generated from the raw material is extracted from the circulating air flow and used for preheating and preliminary drying of the raw material.

  For example, if the raw material is sludge, the vapor evaporated from the sludge-containing water generated by the pulverization process (pulverization and drying) is used for preliminary drying of the raw material sludge having a high moisture content, and the pre-dried raw material is pulverized, Evaporated moisture of sludge is contained in combustion exhaust gas by making it dry powder, using the dry powder as powder fuel for circulating airflow temperature control device (heating furnace), or by molding the powder into pellets and using it as fuel. In addition, the combustion exhaust gas treatment is simplified, and sludge incineration that does not require auxiliary fuel can be performed by the simplified apparatus.

  In addition, for example, if the raw material is a raw material such as thinned wood, pruned wood, rice straw, grass, etc., which has a relatively low water content, it is pulverized, and the resulting dry powder is circulated air temperature controller (heating furnace) Or a powder obtained by molding the powder into pellets as a heating source for circulating superheated steam, and a boiler that generates steam with an excess amount of heat.

According to the powder manufacturing apparatus of the present invention, a double circulating path results in a combined airflow in which two circulating airflows are merged in the container. Even if the raw material contains moisture, the bulky raw material having stickiness, and the size is heavy. Whether it is a raw material or a light raw material, it can be flowed into a container, circulated through the first circulation path, and can be properly pulverized according to the properties of each raw material. Can be manufactured.
In addition, according to the powder production apparatus of the present invention, the circulation flow rate of the second circulation path is reduced, and the circulation airflow in the second circulation path is not released to the atmosphere and can be circulated. That is, high energy efficiency can be achieved, and the apparatus can be miniaturized, thereby reducing the overall cost of the apparatus. Lower cost and continuous production of powder can be achieved in a short time.

Examples of the powder production apparatus of the present invention will be described below.
The powder production apparatus according to the present invention has a double circulation path including a first circulation path and a second circulation path, and pulverization treatment of raw materials, drying treatment of raw materials, and sterilization treatment of raw materials through the circulation airflow. The raw material is cooked, the raw material is roasted, the raw material-containing liquid is vaporized, and the like.

Here, the circulation path (first circulation path, second circulation path) is a path through which the circulating airflow circulates in an annular shape. In addition, a detour route in which the circulating airflow is detoured may be provided in the circulation path. These detours can be considered part of the circuit if a circuit is formed in which the circulating airflow returns to the first point through them.
Further, “circulating” the circulating airflow in the circulation path includes the case where a part of the circulating airflow circulates. That is, part of the circulating airflow in the circulation path may be discharged out of the system, and conversely, gas outside the system may be introduced into the circulation path.

  The circulating gas circulating in the circulation path is preferably an inert gas such as superheated steam and nitrogen in order to avoid oxidation of the raw material, but may be a gas containing combustion exhaust gas or air. The circulating airflow may contain a gas generated when the raw material is pulverized.

In the present invention, there is a sealed space called a “container” as a path portion common to the first circulation path and the second circulation path.
The raw material is fed from outside the system of the powder production apparatus, but it may be introduced from the raw material supply apparatus provided in the container, or may be introduced into the first circuit, the detour of the first circuit, the second circuit, or the like. Alternatively, the structure may be introduced from outside the system through a raw material supply device provided. Further, the raw material may be introduced into the system together with the carrier gas by transferring the raw material using the same gas as the circulating airflow as a carrier by a raw material supply apparatus installed outside the system. The raw material supply device is not particularly limited as long as the raw material can be supplied quantitatively.

  As raw materials of the powder production apparatus of the present invention, food raw materials such as vegetables, cereals, beans, potatoes, fish, seaweed, tea leaves, medicinal herbs, raw okara, fermented fish residues, tea galley, coffee lees, potato dashigara, Any or a combination of food processing by-products such as apple pomace and liquor, or any combination of biomass such as wood, thinned wood, pruned wood, bamboo, grass, rice straw, and sludge or water There can be any of the wastes or combinations thereof, and any of the chemical products such as chemicals, plastics, rubbers, pharmaceuticals, cosmetics, paints and the like.

Moreover, in the powder manufacturing apparatus of this invention, it becomes the structure by which the grinder was provided in the 1st circulation path.
The configuration of the pulverizer is not particularly limited as long as it has a pulverization function capable of pulverizing the raw material in the presence of the circulating gas. It is preferable that the pulverizer has a blowing function in addition to the pulverizing function. This eliminates the need to separately provide a blower (circulation fan) for circulating the circulating airflow and the raw material along the first circulation path.

  Moreover, in the powder manufacturing apparatus of this invention, it becomes the structure by which the powder collection | recovery apparatus was provided in the circulation path. The powder recovery device is not particularly limited as long as the powder can be collected and recovered from the circulating air current, and a known device can be used. For example, a cyclone recovery device that uses centrifugal force or a bag filter that captures powder can be used.

  Moreover, in the powder manufacturing apparatus of this invention, in order to adjust the temperature of a circulating airflow in a circulation path, it becomes the structure by which the circulating airflow temperature control apparatus was provided. If a part or all of the dry powder is burned and used as fuel in this circulating airflow temperature control device, the heat energy of the recovered powder can be effectively used. In addition, in order to use heat efficiently in the entire apparatus, if the raw material is preheated by introducing at least part of the circulating airflow after the powder has been collected into the raw material preheater, The energy can be effectively used.

  Hereinafter, embodiments of the powder production apparatus of the present invention will be described with reference to the drawings. The present invention is not limited to these examples.

A powder production apparatus 100 according to Example 1 of the present invention will be described.
Example 1 is a structural example in which the raw material is a water-containing raw material containing moisture, and the water-containing raw material is pulverized using superheated steam as a circulating airflow.
FIG. 1 is a block diagram simply showing a configuration example of the entire powder manufacturing apparatus according to the first embodiment of the present invention.

  As shown in FIG. 1, the powder manufacturing apparatus 100 according to the first embodiment of the present invention includes a raw material supply device 10, a pulverization processing device 20, a powder recovery device 30, an exhaust processing device 40, and a circulating airflow temperature adjustment device 50. It has become a preparation.

  The raw material supply device 10 includes a hopper 11 that temporarily stores the raw material and a quantitative supply device 12 that is provided at the lower end of the hopper. The outlet of the quantitative supply device 12 is connected to the raw material inlet 21 e of the container 21. The quantitative supply device 12 is not particularly limited as long as the raw material can be supplied quantitatively, and for example, a screw feeder, a rotary valve, or the like can be used.

The pulverization apparatus 20 includes a container 21 and a pulverizer 22, and the container 21 and the pulverizer 22 are connected by a pipe so that a circulating airflow of superheated steam flows. As shown in FIGS. 2 to 4, the connection between the container 21 and the pulverizer 22 has a plurality of piping patterns. First, the configuration of the container 21 and the pulverizer 22 will be described using the piping pattern of FIG. 2 as an example. Other piping patterns will be described later.
FIG. 2 is a view showing the raw material supply apparatus 10 and the pulverization apparatus 20 in FIG.

  The first discharge port 21a of the container 21 and the suction port of the pulverizer 22 are connected by a pipe 101a, and the discharge port of the pulverizer 22 and the first inlet 21b of the container are connected by a pipe 101b. Thus, the piping 101a and the piping 101b form the first circulation path 101 that circulates through the container 21, the first discharge port 21a, the piping 101a, the pulverizer 22, the piping 101b, and the first inlet 21b. Here, since the pulverizer 22 has a blowing function, a circulating airflow of superheated steam is formed in the first circulation path 101.

  In addition, the second discharge port 21c of the container 21 and the powder recovery device 30 are connected by a pipe 201a, and the powder recovery device 30 and the circulating airflow temperature controller 53 in the circulating airflow temperature control device 50 are connected via the exhaust treatment device 40. The circulating airflow temperature controller 53 and the second inlet 21d of the container 21 are connected by a pipe 201c. As described above, the pipes 201a to 201c form the second circulation path 201 in which the container 21, the powder recovery device 30, the exhaust treatment device 40, the circulating airflow temperature controller 53, and the container 21 are connected in an annular shape in this order. Here, a circulation blower 202 for circulating gas is provided on the pipe 201 b of the second circulation path 201, and a circulating airflow of superheated steam is formed in the second circulation path 201 by the blowing force of the circulation blower 202. Is done.

  The container 21 has a cylindrical shape and includes a support member 60 at the lower part. The support member 60 includes a main body member 61 and a rectifying plate 62, and the rectifying plate 62 has a large number of openings. Further, the second inlet 21d of the container 21 is provided in the lower part of the container 21, and the second outlet 21c is provided in the upper part. The gas (superheated steam) that flows into the container 21 from the second inlet passes through the opening of the rectifying plate 62 and rises inside the container 21.

  The first inflow port 21 b into which the air blown from the pulverizer 22 is sent is provided in a direction along the inner wall surface of the container at a position above the support member 60. Since the first inflow port 21b is provided in a direction along the inner wall surface of the container 21, the circulating air flow sent from the first inflow port 21b to the inside of the container 21 is swirled along the inner wall surface of the container 21. It rises.

  Further, a first discharge port 21a serving as a path for circulation to the pulverizer 22 is provided in a direction along the inner wall surface of the container 21 at a position below the second discharge port 21c. Since the first discharge port 21a is provided in the direction along the inner wall surface of the container 21, the circulating airflow swirling along the inner wall surface in the container 21 is easily guided to the pulverizer 22 from the first discharge port 21a. It is configured as follows.

  Thus, in the container 21, the 1st discharge port 21a and the 1st inflow port 21b are provided in the direction in alignment with the inner wall face of the container 21, Therefore The 1st circulation path 101 is made into the ventilation force of the grinder 22. Thus, a swirling flow of superheated steam is formed inside the container 21.

As shown in FIG. 5, the pulverizer 22 includes a casing 70 provided with a suction port 71 and a discharge port 72, an impeller 73 installed in the casing, an electric motor 75 that rotates the screen 74 and the impeller 73. I have.
The screen 74 is a cylindrical member made of a metal material such as stainless steel and having a large number of openings.

The pulverizer 22 has a pulverization function and an air blowing function.
Regarding the pulverization function, when the impeller 73 is rotated by the electric motor 75, the raw material is sucked together with the gas from the suction port 71. The raw material in the pulverizer is surrounded by the screen 74 by the impeller 73. It is pulverized by hitting, colliding with the inner peripheral surface of the screen 74, shearing between the impeller 73 and the inner peripheral surface of the screen 74, collision between raw materials, scraping when passing through the aperture of the screen 74, and the like.
Regarding the air blowing function, the raw material pulverized by the pulverization function passes through the opening of the screen 74 together with the gas, and is discharged together with the gas from the discharge port 72 at a high speed (for example, 15 m / s to 30 m / s). The electric motor 75 is preferably one that can be operated at a variable speed by inverter control.

Here, the point which can obtain a big air current in the container 21 in the powder manufacturing apparatus 100 of this invention is demonstrated.
Among raw materials handled by the powder manufacturing apparatus 100 of the present invention, raw materials containing a lot of moisture, for example, food raw materials are heavy and contain a lot of moisture even if they are cut to an appropriate size. Even by-products (such as okara, tea husk, and coffee candy) are small, they are clumpy due to their stickiness and are heavy. A large air flow is required to flow these heavy materials.

The circulating airflow of the first circulation path 101 and the circulating airflow of the second circulation path 201 from the first inlet 21 b and the second circulation path 201 flow into the container 21 of the powder manufacturing apparatus 100 of the present invention from the first inlet 21 b and merge in the container 21. To do.
For example, the amount of the second circulating airflow flowing in from the second inlet 21d is “1 air flow rate”, and the amount of the first circulating airflow flowing in from the first inlet 21b is “twice the amount of the second circulating airflow”. In the case of “two air flow rates”, the circulation air flow rate in the space between the first inlet 21d and the second discharge port 21a in the container 21, that is, the space in which the raw material is swirling and rising, is “1 air flow rate” + “2 air flow rates”. “=“ 3 air flow rate ”.
Here, if the three-air flow rate is required for the flow rise in the raw material container 21 and there is no inflow of airflow from the first inflow port 21b, that is, if there is no first circulation path 101, the second inflow port. The inflow air flow rate from 21d needs “3 air flow rates”. In other words, the flow rate of the inflowing air from the second inlet 21d can be reduced to 1/3 by having the first circulation path 101.

  An amount of circulating airflow that corresponds to the amount of circulating air flowing in from the second inlet 21d is discharged from the second outlet 21c and circulates in the second circulation path 201. This means that by having the first circulation path, the circulation air flow rate of the second circulation path 201 can be reduced, and thereby, the powder recovery device 30 on the second circulation path 201, the circulation This means that the blower 202 and the circulating airflow temperature adjusting device 50 can be downsized, and the power consumption of the circulating blower 202 can be greatly reduced.

Next, the point which improves the energy efficiency of the whole apparatus by the 2nd circulation path 201 is demonstrated.
When there is no second circulation path 201, the gas flowing in from the second inflow port 21d of the container is discharged to the atmosphere after the powder is collected by the powder collecting device 30. Here, by providing the second circulation path 201, the airflow after the powder recovery by the powder recovery device 30 can be circulated to the second circulation path 201, and the gas after the powder recovery can be circulated without being released to the atmosphere as it is. Thus, the energy held by the gas is effectively used, and energy loss can be reduced.

Next, the progress of the drying process of the water-containing raw material in the pulverizer 22 will be described.
The pulverizer 22 has a pulverizing function and a blowing function, sucks the raw material together with the airflow from the suction port, and sends the pulverized raw material from the discharge port. The hydrous raw material introduced into the first circulation path 101 from the raw material supply apparatus 10 is mixed with the pulverized material in the circulating airflow that has already circulated through the first circulation path 101 and is in a dry state. The average moisture content of the mixture is lower than the moisture content of the water-containing raw material itself. Thus, the average moisture content decreases as the pulverization process proceeds by circulating through the first circulation path 101 and being sucked by the pulverizer 22. Thus, even a water-containing raw material can be operated without the raw material adhering to the wall surface in the apparatus or causing clogging in the apparatus.
That is, the water-containing raw material supplied by the raw material supply apparatus 10 circulates in the first circulation path 101 together with the circulating airflow (superheated steam), and is pulverized by the pulverizer 22 repeatedly, dried, and pulverized to a predetermined size. The first circulation path 101 is circulated until it becomes powder. Thereby, a raw material can be made into a fine powder.

Moreover, the surface area is expanded by grinding the raw material. Due to the increase in surface area, the water-containing raw material is rapidly dried. This enables highly efficient drying, and the water-containing raw material can be dried without using a large dryer.
Of course, even if the raw material has a low moisture content but a large size and a heavy weight, it can be pulverized without any problem.

Next, the progress of the pulverization process of the hydrous raw material in the pulverizer 22 will be described.
The powder manufacturing apparatus 100 of the present invention can form a swirling flow of a circulating air flow in the container 21 and classify the raw materials by a centrifugal force and a circulating air flow by the swirling flow. Only the powder pulverized to a predetermined size by classification is discharged from the first discharge port 21a of the container 21 together with the circulating air current and led to the second circulation path 201, and the raw material not yet classified to the predetermined size is Subsequently, the first circulation path 101 is circulated.

A swirling flow of a circulating airflow is formed inside the container 21 by the blowing force of the pulverizer 22, and the raw material being crushed is swirled by the swirling flow and receives a centrifugal force. Heavy raw materials that have not yet been crushed are outside the container 21, that is, near the inner wall surface of the container 21, and light pulverized raw materials that have been pulverized are inside the container 21, that is, near the center of the container 21. Turn. The powdered raw material swirling around the center side of the container 21 rises in the container 21 together with the swirling flow, and is discharged together with the circulating air flow from the second discharge port 21c at the top of the container 21. On the other hand, the heavy raw material that has not yet been crushed is circulated through the first circulation path again and sucked by the pulverizer 22 for further classification.
In this way, the raw material was classified to a desired size by appropriately controlling the flow rate of the circulating airflow in the first circulation path and the second circulation path without providing any special classification mechanism and mechanical classifier. It can be a product powder.

Although the piping configuration of the container 21 and the pulverizer 22 has been described based on the example of FIG. 2, another pattern will be described as the piping configuration of the container 21 and the pulverizer 22.
First, in the configuration shown in FIG. 3, the second discharge port 21c connected to the pipe 201a of the second circulation path 201 is provided in the upper part of the container 21, and the pipe of the first circulation path 101 is provided on the inner wall surface of the container below that position. A first inflow port 21b connected to 101b is provided, and a second discharge port 21d connected to the pipe 201c of the second circulation path 201 is provided on the inner wall surface of the container below that position on the inner wall surface of the container 21. The 1st discharge port 21a connected to the piping 101a of the 1st circuit 101 is provided in the lower part of this. The first inlet 21b and the second inlet 21d are provided in a direction along the inner wall surface of the container 21a.

As shown in FIG. 3, the airflow formed in the container 21 is a swirling flow that descends below the first inlet 21b and rises above the first inlet 21b. Is formed.
The raw material introduced into the container 21 rides on the circulating airflow circulating through the first circulation path 101 and is discharged from the first discharge port 21a at the lower part of the container 21 together with the raw material already being pulverized, and sucked into the pulverizer 22. After being crushed, it flows into the container 21 from the first inlet 21 b and circulates through the first circulation path 101. The powder pulverized and dried to a predetermined size in the circulation process of the first circulation path 101 rises higher than the first inflow port 21b because it is light, and is second circulated by the rising swirling airflow toward the second discharge port 21c. It is discharged to the pipe 201 a of the path 201 and leaves the first circulation path 101 and moves to the second circulation path 201. On the other hand, the raw material that has not yet been pulverized to a predetermined size in the process of circulation in the first circulation path 101 is in a heavy state, descends with a downward swirling flow, and circulates again through the first circulation path 101.
Here, the amount of the circulating airflow in the first circulation path 101 in the container 21 is preferably larger than the amount of the circulating airflow in the second circulation path flowing in from the second inlet 21d, for example, 1.5 times, Is preferably twice or more.

  Next, in the configuration illustrated in FIG. 4, the container includes a lower container 21A and an upper container 21B. The lower container 21A is the same as the container 21 shown in FIG. 2, but the upper container 21B is attached concentrically to the lower container 21A and is connected via a vent path 21f. The structure of the upper container 21B is a so-called cyclone separator structure.

Next, in the piping configuration shown in FIG. 4, as the circulation path, the first circulation path 101A formed by the lower container 21A and the first pulverizer 22A, the first container formed by the upper container 21B and the second pulverizer 22B. A circulation path 101B is provided.
The piping of the lower container 21A is substantially the same as the piping of the container 21 shown in FIG. 2, but the ventilation path corresponding to the second discharge port is a container above the container 21A in view of the second circulation path 201. It becomes the ventilation path 21f connected to 21B.
As piping of the upper container 21B, the first inflow port 21h is provided in a direction along the inner wall surface of the container at a position above the container 21B. Further, a portion corresponding to the first discharge port is provided as 21 g on the upper portion of the lower container 21 </ b> A. Considering the second circulation path 201, the portion corresponding to the second inlet is a portion corresponding to the air passage 21f with the lower container 21A. The second discharge port 21i is provided at a position on the center line of the container 21B in a state where the lower part is inserted into the container 21B.

  The water-containing raw material containing moisture introduced into the container 21A by the raw material supply apparatus 10 is mixed with the raw material that has already been pulverized and dried in the first circulation path 101A to become a mixture and circulate in the first circulation path 101A. At each circulation, the raw material pulverized by the first pulverizer 22A and dried by the first circulation path 101A and having a predetermined lightness rises with the upward swirling flow formed in the upper part of the container 21A. Through the second air outlet 21g of the container 21A and is sucked into the second pulverizer 22B having a pulverizing function and an air blowing function.

The raw material circulated through the first circulation path 101A of the lower container 21A and finely pulverized by the first pulverizer 22A is sent to the upper container 21B.
It circulates through the first circulation path 101B of the upper container 21B and is finely pulverized by the second pulverizer 22B. The raw material further finely pulverized by the second pulverizer 22B flows into the container 21B together with the air current from the first inlet 21h of the container 21B, and the space between the inner wall surface inside the container 21B and the outer wall of the second outlet 21i. Go down while turning. The raw material to which the pulverization process proceeds is pulverized to a predetermined size and flows into the top of the container 21A through the air passage 21f until it is dried, merges with the rising air flow that has risen up the container 21A, and again from the second discharge port 21g. It is sucked by the second pulverizer 22B and circulates again in the first circulation path 101B together with the circulating airflow.
While circulating through the first circulation path 101B, the powder that has been pulverized to a predetermined size and dried is light, and therefore is drawn into the rising air current generated in the second outlet 21i disposed in the central portion inside the container 21B. Then, it is discharged from the pipe 201a of the second circulation path 201 through the second discharge port 21i. Such a so-called cyclone-type centrifugal separation function makes it possible to classify powder with higher accuracy and to produce fine powder.

  The circulation air flow rate of the first circulation path 101B in the container 21A is preferably equal to or more than the circulation air flow rate of the pipe 201B of the second circulation path 201 flowing in from the second inlet 21d. The circulatory flow rate of the first circulation path 101A is not less than the circulation flow rate of the first circulation path 101B and is preferably 1.5 times or more, preferably 2 times or more of the circulation air flow rate of the second circulation path.

  By providing a two-stage pulverization treatment by two first pulverizers 22A and 22B, and two first circulation paths 101A and first circulation paths 101B, a raw material having a large size and a high moisture content can be obtained. Even a massive heavy material having a high viscosity and a high water content can be pulverized and dried to obtain a finer powder.

  In the configuration example shown in FIGS. 2, 3, and 4, the containers 21 are arranged in a vertical shape, but are not limited to a vertical arrangement, and may be arranged in a horizontal arrangement. It is only necessary that a swirl airflow is formed in the container for both the first circulating airflow and the second circulating airflow, and the raw material to be pulverized is subjected to centrifugal force and classified.

Next, returning to FIG. 1, the description of other components will be continued.
The powder recovery apparatus 30 separates and recovers the powder pulverized to a predetermined size in the container 21 from the circulating airflow.
The powder recovery apparatus 30 includes a cyclone separator 31. The powder centrifuged in the cyclone separator 31 falls into the powder hopper 32 and is stored. The circulating airflow after the powder separation is discharged from the discharge port of the cyclone separator 31.
In the configuration of FIG. 1, the configuration of one cyclone separator 31 is used, but other configurations are possible. For example, a combination of a cyclone separator 31 and a multicyclone may be used. Further, a bag filter may be used instead of the cyclone separator 31. Furthermore, the structure which combined the cyclone separator 31 and the bag filter etc. may be sufficient.

Next, the circulating airflow temperature adjusting device 50 will be described.
The circulating airflow temperature adjusting device 50 is for holding the temperature of the circulating airflow at a predetermined temperature in the second circulation path 201. If the circulating airflow is superheated steam, it will condense when the temperature decreases, so even if the temperature of the circulating airflow is in a state where the energy is released to dry the raw material in the pulverization processing device 20 and the temperature is lowered, It is necessary to keep the temperature above the saturation temperature. Therefore, the circulating airflow temperature adjusting device 50 is provided in the path of the second circulation path 201 to keep the temperature of the circulating airflow at a predetermined temperature equal to or higher than the saturation temperature.

  In the configuration example of FIG. 1, the temperature of the superheated steam that is the circulating airflow is detected by the temperature controller 501 provided on the pipe 201 b connected to the discharge port of the powder recovery device 30, and the circulating airflow temperature adjusting device 50. The fuel control valve 601 and the combustion air control valve 602 are operated for the fuel amount and the combustion air amount in the heating furnace 51, respectively, and the circulating air flow (superheated steam) is heated by the circulating air flow temperature controller by the heat generated by combustion of the fuel, and the raw material is dried. The necessary energy is added to the circulating airflow to form high-temperature superheated steam, and the energy is released to dry the raw material by the pulverization processing device 20 so that the temperature is maintained at a predetermined temperature equal to or higher than the saturation temperature even when the temperature is lowered. It has become. The superheated steam temperature in the container 21 of the pulverization apparatus 20, that is, the raw material processing temperature changes in conjunction with the set temperature of the temperature controller 501. If the set temperature is increased, the temperature in the pulverizing apparatus is also increased, and if the set temperature is decreased, the temperature is decreased. The temperature in the pulverization apparatus 20 can be set to an arbitrary predetermined temperature by the set temperature of the temperature controller 501.

  By adjusting the temperature of the superheated steam in the container 21, the raw material can be processed in addition to pulverization and drying. For example, if the temperature of the superheated steam in the container 21 is 110 ° C., the raw material can be sterilized. Moreover, if it is set to higher temperature, it will become the heat-cooked powder. Furthermore, if the temperature is around 200 ° C., a roasted powder obtained by roasting the raw material can be obtained.

In the configuration example of FIG. 1, the circulating airflow temperature adjusting device 50 is an example of a vertical heating furnace, but may be a horizontal type.
In addition, the circulating airflow temperature adjusting device 50 shown in FIG. 1 is a heating furnace type that burns fuel, but the fuel used in the circulating airflow temperature adjusting device 50 is not limited and may be any of liquid, gas, and solid fuel. Also good.

  The circulating airflow temperature adjusting device 50 is not limited to a heating furnace type that burns fuel. For example, an electric heater may be used. In the case of a raw material having a low water content, less energy is required for heating the circulating airflow by the circulating airflow temperature adjusting device 50, so that an electric heater can be applied.

Next, the exhaust treatment device 40 will be described.
The exhaust treatment device 40 is a mechanism that discharges a part of the circulating airflow to the outside of the system, and is connected to the pipe 201b via the pipe 301.
The superheated steam circulation airflow after the powder is recovered contains vaporized or vaporized gas from the raw material moisture. Unless these gases are released outside the system, the pressure in the circulation path (first circulation path 101, second circulation path 201) will increase. The exhaust treatment device 40 detects the pressure by the pressure regulator 502 provided on the pipe 201, operates the pressure adjustment valve 603 provided on the pipe 301, and the amount of vapor or gas evaporated from the raw material moisture The pressure of the superheated steam in the circulation path is maintained at a predetermined pressure by extracting an amount of superheated steam corresponding to. The extracted superheated steam is cooled by the cooler 41, condensed, and discharged out of the system. Further, the non-condensed gas is introduced into the heating furnace 51 through the pipe 302, decomposed and burned, and released.

  If gas vaporized from the raw material accumulates in the circulating superheated steam and the concentration of these vaporized gases in the circulating superheated steam increases and may affect the product powder, a gas analysis controller 503 is installed on the pipe 201b. It is preferable to detect the gas concentration, operate the gas introduction control valve 604, introduce steam from outside the system, and maintain the gas concentration below a predetermined concentration. In this case, the amount of steam introduced from the control valve 604, steam evaporated from the raw material moisture, and superheated steam in an amount corresponding to the amount of gas evaporated are extracted from the circulation path by the pressure control valve 603.

  In addition, when a useful component is contained in the liquid condensed with the cooler 41, condensed water can also be used effectively. The cooling medium used for the cooler 41 may be cooling water or air. If the cooling medium is supplied water and is supplied as warm water outside the system, the heat energy in the apparatus can be used effectively.

  Here, in the case of a raw material containing a lot of moisture, for example, a raw material having a moisture content of 75% or more, the energy of superheated steam extracted from the circulation path becomes large. Therefore, if a raw material predrying device is provided instead of the exhaust treatment device 40 and the superheated steam extracted from the pressure control valve 603 is introduced into the raw material predrying device, the raw material can be preheated and predried. In the raw material pre-drying apparatus, the pre-heated and pre-dried raw material having a reduced water content is introduced into the pulverization apparatus 20, whereby the fuel consumed in the entire powder manufacturing apparatus 100 can be reduced.

  On the other hand, in the case of a raw material with a low water content or a raw material with a strong odor, the superheated steam extracted from the regulator valve 602 may be released as it is without providing the cooler 41.

Next, the circulation blower 202 will be described.
In the configuration example of FIG. 1, a circulation blower 202 is installed on a pipe 201b. A circulating air flow is formed in the second circulation path 201 by the circulation blower 202. The circulation blower 202 is preferably driven by an inverter motor so that the air volume can be easily adjusted.

  The superheated steam that has passed through the exhaust treatment device 30 is introduced into the heating furnace 51 of the circulating airflow temperature control device 50. The circulating steam is heated to a predetermined temperature by the combustion of the fuel adjusted by the temperature controller 501, and is introduced into the container 21 through the pipe 201c connecting the discharge port of the heating furnace 51 and the second inlet 21d of the container 21. And circulates through the second circulation path 201.

  As described above, as Example 1, a configuration example in which a raw material containing moisture is pulverized using superheated steam as a circulating airflow has been shown. According to the powder manufacturing apparatus 100 of the first embodiment, by providing the two first circulation paths 101 and the second circulation path 201, the container becomes a combined airflow in which the two circulating airflows merge and is heavy including moisture. Even if it is a raw material or a blocky heavy raw material having adhesiveness, it can flow through the container 21 using superheated steam and circulate through the first circulation path 101 to perform an appropriate pulverization process. Recovery and effective use of thermal energy can be made.

The powder manufacturing apparatus 100a according to the second embodiment has a configuration suitable for pulverizing a dry raw material having a low moisture content as a raw material using superheated steam as a circulating air flow.
By pulverizing the dried raw material in a closed system in which oxygen in the atmosphere is blocked, it is possible to produce a high-quality powder with very little quality deterioration due to oxidation of the raw material.

  FIG. 6 is a diagram showing the configuration of the powder production apparatus 100a of the second embodiment. In the configuration example of FIG. 6, illustration of the same part as that of the configuration example of FIG. 1 is omitted, and different portions are mainly illustrated. As shown in FIG. 6, the powder manufacturing apparatus 100a of Example 2 is configured to include a raw material supply apparatus 10, a pulverization processing apparatus 20, a powder recovery apparatus 30, an exhaust processing apparatus 40a, and a circulating airflow temperature adjustment apparatus 50a. ing. Compared to the components of the first embodiment, the components of the exhaust treatment device 40a and the circulating airflow temperature control device 50a are different.

  In Example 2, a dry raw material is handled, but since the dry raw material has a low water content, the amount of vaporized vapor and vaporized gas of the raw material water generated in the pulverization process is small. Accordingly, since the amount of superheated steam extracted by the pressure control valve 502 in the circulation path 201 is small, the superheated steam is released to the atmosphere as it is. If the superheated steam released to the atmosphere has an odor, the cooler 41 (preferably a small one) shown in FIG. 1 is provided, the steam is condensed and drained, and the uncondensed gas passes through, for example, a deodorizer using activated carbon. It is preferable to release the air after deodorizing.

  When vaporized gas generated from the dry raw material is accumulated in the circulation path, and the concentration of these gases in the circulating steam may increase, resulting in quality deterioration of the dry powder or the like, as shown in FIG. The concentration controller 503 detects the concentration of the gas in the circulating superheated steam in the second circulation path 201 and adjusts the gas introduction so that the gas concentration in the circulating superheated steam in the second circulation path 201 is kept below a predetermined concentration. The valve 604 may be operated to introduce steam into the second circulation path 201 from outside the system. In this case, the pressure control valve 603 extracts steam generated from the raw material, vaporized gas, and superheated steam in an amount corresponding to the amount of steam introduced from the gas introduction control valve 604.

  High-quality powders that do not oxidize or heat-treated with superheated steam can be produced from dried raw materials. In addition, when the raw material is food, roasted powder can be produced. When producing roasted powder, it is preferable to mix oxygen in the circulating steam. For this reason, a small amount of air is introduced into the second circulation path 201 from the air control valve 605. It is preferable that the oxygen concentration in the second circulation path 201 is detected by the gas concentration controller 503, and the air control valve 605 is operated to maintain the oxygen concentration at a predetermined level.

When processing a dry raw material, the calorie | heat amount required for drying is not required compared with the case where a hydrous raw material is processed. Therefore, the amount of heat added to the circulating steam by the circulating airflow temperature adjusting device 50 is mainly supplemented with the amount of heat radiated from the outer wall of the device to the outside of the system.
In addition, since part of the power consumption of the pulverizer 22 and the circulation blower 202 becomes the heating energy of the circulation steam, the circulation air temperature controller 50 may have a small heating capacity, and an electric heater 59 can be used. Moreover, the small heater (same as Example 1) which burns fuel and heats it with combustion gas may be sufficient.

  In a high-strength raw material that requires a large amount of power for pulverization, the thermal energy applied to the steam by the pulverizer 22 and the circulation blower 202 may be greater than or equal to the heat radiation from the outer wall of the apparatus. In such a case, it is preferable to provide a heater and a cooler in the circulating airflow temperature controller. The cooling medium is preferably air.

  The heater is heated so that the superheated steam reaches a predetermined temperature at the start of operation of the apparatus, or is heated during the operation of the apparatus to prevent the temperature of the superheated steam from decreasing due to an increase in the amount of heat released from the outer wall of the apparatus. Use when.

  As described above, according to the powder manufacturing apparatus 100a according to the second embodiment, a dry raw material is pulverized in a closed system in which oxygen in the atmosphere is blocked, thereby producing a high-quality powder with very little quality deterioration due to oxidation of the raw material. Can do.

The powder manufacturing apparatus 100b according to the third embodiment has a configuration suitable for pulverizing a hydrous raw material containing moisture as a raw material using an inert gas such as heated nitrogen as a circulating air flow.
The powder production apparatus 100b according to the third embodiment is a closed system in which oxygen in the atmosphere is shut off. Compared to the first embodiment, the quality degradation due to oxidation or the quality degradation due to heating in a lower temperature range, for example, 60 to 90 ° C. Can produce high-quality powders with very little.
Particularly for food raw materials such as vegetables, beans, grains, seaweeds, medicinal herbs, etc., it is possible to produce high quality powders that maintain the quality (color, fragrance, etc.) of the raw materials.

  FIG. 7 is a diagram showing the configuration of the powder manufacturing apparatus 100b of the third embodiment. In the configuration example of FIG. 7, illustration of the same parts as those of the configuration example of FIG. As shown in FIG. 7, the powder production apparatus 100b of the third embodiment includes a raw material supply apparatus 10, a pulverization apparatus 20, a powder recovery apparatus 30, an exhaust treatment apparatus 40b, and a circulating airflow temperature adjustment apparatus 50. However, the components of the exhaust treatment device 40b are different from those of the first embodiment.

  In Example 3, a raw material containing moisture is handled. The wet raw material containing moisture is pulverized while circulating through the first circulation path 101 together with an inert gas such as heated nitrogen (hereinafter, these are represented by heated nitrogen). Processed into powder. The powder is classified in the container 21, discharged from the container 21 together with heated nitrogen containing evaporated moisture and vaporized gas of the raw material generated by drying, and recovered by the powder recovery device 30. The circulating heated nitrogen after powder recovery discharged from the powder recovery device 30 contains evaporated water and vaporized gas of the raw material. Therefore, unless these gases are extracted outside the system, the pressure of heated nitrogen in the system will increase.

Here, since nitrogen is a gas at room temperature, in order to remove evaporated moisture from the raw material, the entire amount of heated nitrogen after powder recovery is introduced into the cooler 41b shown in FIG. 7 and cooled to condense evaporated moisture, Remove by releasing out of the system.
For vaporized components that do not condense due to cooling, the pressure regulator 502 detects the pressure of the second circulation path 201 and operates the pressure control valve 603 to contain nitrogen containing vaporized components in an amount commensurate with the amount of vaporized components that do not condense. Withdrawing from the second circulation path 201 through the pressure control valve 603, the pressure of the heated nitrogen in the second circulation path 201 is maintained at a predetermined pressure. The extracted nitrogen containing vaporized components is introduced into the heating furnace 51 of the circulating airflow temperature control device 50 and decomposed and burned.

The refrigerant used for the cooler 41b is cooling water, but the refrigerant may be air. The temperature of nitrogen discharged from the cooler 41b is maintained at a predetermined temperature by operating the amount of cooling water with the temperature control valve 606.
The nitrogen discharged from the cooler 41b includes saturated water vapor having a temperature set by the temperature controller 504.
When a higher quality powder can be produced by reducing the amount of water vapor in the nitrogen, cold water having a lower temperature may be used as the refrigerant, and the temperature of the circulating nitrogen coming out of the cooler 41b may be set to a lower temperature. By lowering the temperature of the circulating nitrogen coming out of the cooler 41b, the temperature of the heated circulating nitrogen in the pulverization processing device 20 and the first circulation path 101 can be lowered, and the quality of the high-quality powder with little quality deterioration due to temperature can be reduced. Production is possible.

The circulation blower 202 is installed on a pipe 201b that connects the outlet of the cooler 41b and the inlet of the heater 51. The installation place of the circulation blower 202 may be any place on the second circulation path 201.
As the operation progresses, gases other than water vaporized from the raw material accumulate in the circulating nitrogen, and the concentration of the vaporized gas in the circulating nitrogen may increase. For the production of high quality powder, it is preferable to keep the concentration of these vaporized gases low. Therefore, the gas analysis controller 503 detects the vaporized gas concentration or nitrogen concentration from the raw material contained in the circulating nitrogen of the second circulation path 201, and the vaporized gas concentration from the raw material contained in the circulating nitrogen is less than a predetermined concentration. The gas introduction control valve 604 is operated to introduce nitrogen from outside the system. The amount of nitrogen introduced from outside the system and the circulating nitrogen corresponding to the amount of vaporized gas evaporated from the raw material are extracted from the second circulation path 201 through the pressure control valve 603.

  The circulating nitrogen discharged from the cooler 41b of the exhaust treatment device 40b is introduced into the circulating airflow temperature adjusting device 50 through the pipe 201b, heated to a predetermined temperature, introduced into the powder processing apparatus 20 through the pipe 201c, and the second circulation path. Circulate.

  In the present embodiment, the hydrated food material may be sterilized or the cooked powder of the hydrated food material may be produced by setting the temperature controller 501 at a higher temperature, for example, 80 ° C. or higher. it can.

As Example 4, the raw material is a reaction product containing unreacted raw material (monomer) and solvent in the petrochemical industry, pharmaceutical industry, cosmetics industry, etc., and its powdering treatment, purification treatment, recovery of unreacted monomer and solvent The processing will be described.
The configuration itself of the powder production apparatus of Example 4 may be the same as that of the powder production apparatus 100b of Example 3, and illustration thereof is omitted here. Heated nitrogen is used as the circulating air flow.

  In the powder manufacturing apparatus 100b, the reactive product supplied as a raw material to the first circulation path 101 is crushed and pulverized while circulating through the circulation path 101 together with heated nitrogen. Moreover, the unreacted monomer, solvent, etc. contained in the product are heated by heated circulating nitrogen to become a vaporized gas.

  Unreacted monomer, solvent, and the like are vaporized and removed, and the reaction product formed into uniform particles by the classification function in the container 21 is supplied to the second outlet 21c of the container 21 together with the circulating heated nitrogen containing the vaporized unreacted monomer and solvent. And is introduced into the powder recovery device 30.

  In the powder recovery apparatus 30, the reaction product is separated and recovered from the circulating heated nitrogen. The circulating heated nitrogen after collecting the reaction product is introduced into the cooler 41b of the exhaust treatment device 40b and cooled. By cooling, unreacted monomers and solvent in the circulating nitrogen are liquefied, recovered, and sent to the reaction system. Similarly, in order to maintain the circulating nitrogen concentration, the amount of circulating heated nitrogen corresponding to the amount introduced from the regulating valve 604 and the amount of vaporized gas emitted from the raw material reactive organism not liquefied by the cooler 41b is extracted through the pressure regulating valve 603. And sent to the reaction system.

The exhaust treatment device 40b may be installed in a reaction system outside the system, or the circulating heated nitrogen after powder recovery may be transferred to a treatment device outside the system, and the treated circulating nitrogen may be supplied and circulated.
The nitrogen gas from which the unreacted monomer and the solvent are removed by the cooler 41b is introduced into the circulating airflow temperature adjusting device 50, heated to a predetermined temperature, and the heated nitrogen is introduced into the container 21 of the pulverization processing device 20. And circulates in the circulation path (first circulation path, second circulation path).

The powder manufacturing apparatus 100b may be a single system incorporated in the reaction system.
The raw material may be introduced into the bypass circuit of the second circulation path 201 by the raw material supply apparatus 10 and introduced into the first circulation path 101 using the circulating airflow as a carrier by the bypass circuit.

  As described above, according to the powder manufacturing apparatus 100b shown in Example 4, the reaction product can be purified with high efficiency and low cost by the closed system in which oxygen in the atmosphere is cut off, and high quality powder production is possible. In addition, it is possible to efficiently recover unreacted monomers, solvents, and the like.

As Example 5, the raw material is a dry raw material with a low water content, particularly health food, Chinese medicine, plastics other than organic substances, rubber, pharmaceuticals, cosmetics, etc., and a configuration suitable for the powdering treatment will be described.
Since it is ground in a closed system in which oxygen in the atmosphere is cut and pulverized in a low temperature range close to room temperature, it is possible to produce a high quality powder with very little quality deterioration due to oxidation and heating.

The powder manufacturing apparatus 100 according to the fifth embodiment may have a configuration excluding the circulating airflow temperature adjusting apparatus 50 according to the configuration example shown in FIG. Nitrogen is used as the circulating air flow.
Since the raw material is a dry raw material, heating for drying is not required, and a heater for heating the circulating nitrogen is not required. Further, the temperature controller 501 is not required.

  Part of the power of the pulverizer 20 and the circulating blower 202 becomes the heating energy of the circulating nitrogen, the circulating nitrogen is heated, the heating energy is accumulated, and the temperature of the circulating nitrogen rises with time. For this reason, the circulating nitrogen is cooled using the cooler 41b used in the third embodiment, the temperature of the circulating nitrogen is detected by the temperature regulator 504, the cooling water regulating valve 606 is operated, and the temperature is kept at a predetermined temperature. It has become. Thus, the cooler 41b plays the role of the circulating airflow temperature adjusting device 50. The refrigerant in the cooler 41b may be air as in the third embodiment. The circulating nitrogen discharged from the cooler 41b is introduced into the container 21 through the second inlet 21d of the container 21 and circulates through the second circulation path.

  When gas is generated from the raw material due to the pulverization treatment of the dry raw material and there is a possibility of accumulation of gas in the circulating nitrogen, the gas concentration or nitrogen concentration is detected as in Example 3, and the circulating nitrogen is kept at a predetermined nitrogen concentration. Nitrogen is introduced from the outside of the system into the second circulation path 201 so as to be maintained, and an amount of circulating nitrogen corresponding to the amount of gas generated from the raw material and the amount of nitrogen introduced from the outside of the system is extracted by the pressure control valve 603 Hold at a pressure of.

  As described above, according to the powder manufacturing apparatus of the fifth embodiment, it is suitable for the production of health foods and herbal medicines, and also can produce fine powders such as plastics, rubbers, pharmaceuticals and cosmetics other than organic substances.

As Example 6, a powder production apparatus 100c suitable for sludge treatment will be described.
The sludge incineration method that has been widely used heretofore introduces sludge with high moisture content and high moisture content into the furnace, and blows up the circulating fluidized sand heated to high temperature by combustion of auxiliary fuel in the furnace together with the combustion gas. The introduced sludge and the circulating fluidized sand collide, and the massive sludge is burned while being divided and dried. The flow of fluid sand, circulation, and sludge mass flow require a large flow rate of hot air flow, which requires a large amount of combustion air and a large amount of auxiliary fuel. More air is required for complete combustion of sludge, the air-fuel ratio is large, the combustion efficiency is poor, and a large amount of combustion exhaust gas is generated. In addition, since the combustion exhaust gas contains ash and evaporated vapor from sludge, the exhaust gas treatment device must be complicated and large-scale. Although it can be a resource if it is dried, forcibly incinerating with auxiliary fuel is a waste of energy.

  On the other hand, the present invention uses superheated steam as a circulating airflow, pulverizes hydrous sludge and hydrous organic waste into dry powder, and uses the obtained dry powder as powder fuel or pellet fuel obtained by molding the powder. It is used effectively as a heating fuel. Further, the steam generated by drying the raw material is also used for preheating and preliminary drying of the water-containing raw material.

  FIG. 8 is a diagram illustrating the configuration of the powder manufacturing apparatus 100c of the sixth embodiment. As shown in FIG. 8, the powder production apparatus 100c of Example 6 includes a raw material preliminary drying apparatus 80 in addition to the raw material supply apparatus 10, the pulverization processing apparatus 20, the powder recovery apparatus 30, and the circulating airflow temperature control apparatus 50c. It has a configuration. Compared to the components of Example 1, there is no exhaust treatment device 40, the components of the powder recovery device 30c and the circulating airflow temperature adjusting device 50c are different, and a raw material pre-drying device 80 is added.

  As shown in FIG. 8, a raw material preliminary drying device 80 is installed between the raw material supply device 10 and the pulverization device 20. The raw material preliminary drying apparatus 80 is an alternative to the exhaust treatment apparatus 40 of FIG.

The circulating airflow temperature control device 50 is of a heating furnace type using powder as fuel.
The raw material supply device 10 introduces the water-containing raw material to the raw material pre-drying device 80, the water-containing raw material is heated by the circulating superheated steam extracted from the second circulation path 201, and a part of the water content is evaporated and removed. The As a result, the thermal energy of the exhaust steam that has been discarded can be recovered and used effectively, and the thermal efficiency is improved.

The raw material pre-drying device 80 has a heating jacket on the outer casing, and has a rotating body such as a scraper and a screw inside, and has a function of dividing and moving the raw material lump by rotation of the rotating body. Is. In addition, an exhaust cooler, an ejector, a vacuum pump, and other vacuum devices for maintaining the internal atmospheric pressure at a weak negative pressure are provided.
The configuration of the raw material pre-drying device 80 is not particularly limited as long as it is an airtight dryer that can dry the water-containing raw material with the superheated steam extracted from the second circulation path 201.

Note that the raw material may be directly introduced into the first circulation path 101 as shown in FIG. In this case, it is necessary to provide the exhaust treatment device 40 shown in FIG.
The raw material from which part of the moisture has been dried and removed by the preliminary drying device 80 is introduced into the container 21 of the pulverization processing device 20 from the raw material supply port 21e. The raw material introduced into the container 21 is circulated through the first circulation path 101 on the circulating superheated steam together with the raw material that has already been pulverized and dried through the first circulation path 101. It is pulverized many times and becomes powder.

Even if there is a sticky sludge containing moisture, it collides with the pulverized material that has already been pulverized and dried in the first circulation path 101, and it is divided into a mixture and sucked into the pulverizer 22. The average moisture content of the mixture is lower than the moisture content of the raw material, and it is pulverized and dried into powder without adhering to the inside of the apparatus or closing the apparatus.
Moisture contained in the raw material becomes steam by drying and is combined with circulating superheated steam.
The powder that has been pulverized and dried to a predetermined size is classified in the container 21, discharged from the second outlet c of the container 21 together with the circulating superheated steam, and passed through the pipe 201 a of the second circulation path 201. 30c.

  In the powder recovery device 30c, the powder is separated from the circulating superheated steam, stored in the powder hopper 32, introduced into the burner 52 by the fuel supply device 56 of the circulating airflow temperature adjusting device 50c via the rotary valve 33 and the conveyance path 401, and the heating furnace. It is burned as 51 fuel.

  Although not shown, a pellet device may be provided, powder may be introduced into the pellet device, molded into a pellet shape, and the molded pellet may be used as the fuel for the heating furnace 51.

  The circulating superheated steam after powder recovery discharged from the powder recovery device 30 includes vaporized vapor from raw material moisture and vaporized gas generated from the raw material. In order to maintain the pressure of the circulation path (first circulation path 101, second circulation path 201) at a predetermined pressure, the pressure regulator 502 provided on the pipe 201b detects the pressure of the second circulation path 201, and the raw material The amount of circulating superheated steam corresponding to the amount of vaporized water vapor and the amount of vaporized gas generated from the raw material is extracted from the second circulation path 201 by operating the pressure control valve 603.

  Superheated steam extracted by the pressure control valve 603 (also referred to as steam generated by drying the raw material in the pulverizing apparatus 20) is introduced into the preliminary dryer 81 of the preliminary drying apparatus 80 through the pipe 302, and used for preliminary drying of the raw material. Used.

  The superheated steam introduced into the preliminary dryer 81 releases and condenses the amount of heat for heating and drying the raw material containing moisture. As a result, the latent heat of evaporation required for water evaporation of the raw material, which occupies most of the thermal energy consumed in the pulverizing apparatus 20, is effectively used for the preliminary drying of the raw material.

Steam and vaporized gas generated from the raw material by preliminary drying of the raw material are cooled by a cooling function (not shown) built in the vacuum device 82, and the steam is condensed.
Condensed water of superheated steam extracted from the pressure control valve 603 and used as a heat source for the preliminary drying of the raw material, and condensed water evaporated from the raw material by the preliminary drying of the raw material and condensed by the cooling function of the vacuum device 82 are taken out of the system. Drained.

  In addition, the non-condensed vaporized gas extracted from the pressure control valve 603 and included in the superheated steam used as the heat source for the preliminary drying of the raw material, or the non-condensed gas generated from the raw material by the preliminary drying of the raw material and not condensed by the cooling function of the vacuum device 82 The condensed vaporized gas is introduced into the heating furnace 51 through the pipe 302 and decomposes and burns.

The installation location of the pressure control valve 603 is not limited to 201b, and may be on the pipe 201c.
The circulating superheated steam is introduced into the circulating airflow temperature controller 53 built in the heating furnace 51 of the circulating airflow temperature adjusting device 50c through the pipe 201b.

In the heating furnace 51, the powder recovered by the powder recovery device 30 is used as fuel. The powder is introduced into the burner 52 by the fuel feeder 56 through the conveying path 401 and burned.
Unlike the conventional method of forcibly combusting a raw material containing moisture as in the sludge treatment, since it is a dry fuel, it can be completely combusted with a smaller amount of combustion air.
Further, since it is a dry fuel, the combustion gas does not contain steam.
The combustion exhaust gas device can be a simple device.

  The powder burns in the lower part of the heating furnace 51 to become a high-temperature combustion gas, and heats the circulating superheated steam in the circulating airflow temperature controller 53. Combustion gas (combustion exhaust gas) that has passed through the circulating airflow temperature controller 53 is discharged from the heating furnace 51, the combustion air is heated by the combustion air preheater, the temperature is further lowered, and the ash content contained by the bag filter 57 is reduced. It is separated and removed, and is discharged from the chimney 55 to the atmosphere.

In the combustion portion at the lower part of the heating furnace 51, non-condensed gas generated from the raw material is introduced through the pipe 302, and decomposes and burns in the heating furnace 53.
The configuration of the heater is not limited to FIG. Although FIG. 8 is a vertical type, it may be a horizontal type. What is necessary is just to have a function which burns powder and heats circulating superheated steam.

  Further, although not shown in the heating furnace 51, it is preferable to provide an auxiliary burner for liquid or gaseous fuel. The auxiliary burner preheats the inside of the heating furnace at the start of operation of the apparatus, and at the start of operation, introduces steam from the outside of the system into the circulation path (first circulation path 101, second circulation path 201), and air in the system. Is replaced with steam, the circulation blower 202 and the pulverizer 22 are started, and the introduced steam is heated and circulated to raise the temperature to a predetermined superheated steam temperature. Moreover, this can be used at the time of trouble of a powder combustion system, and more stable operation can be performed.

  The temperature controller 501 on the pipe 201b detects the temperature of the circulating superheated steam and operates the powder supplier 56 and the combustion air adjustment damper 601 so that the temperature of the circulating superheated steam in the pipe 201b is maintained at a predetermined set temperature. The circulating superheated steam is heated by the circulating airflow temperature controller 53.

The superheated circulating steam heated by the circulating airflow temperature controller 53 is introduced into the container 21 through the pipe 201c and circulates in the circulation path (first circulation path, second circulation path).
Generally, sludge contains 80% of water, but when dried, it has a combustion heat value of 4,000 to 4,500 kcal / kg of dried product. In the case of sludge in food factories, there are some that have a larger calorific value. For example, if 1,000 kg of sludge has a moisture content of 800 kg and a solid content of 200 kg, the amount of heat required to dry the sludge of 1,000 kg (heated sensible heat of the raw material + latent heat of water evaporation) is about 530,000 kcal, When the unit combustion calorific value with a solid content of 200 kg is 4,200 kcal / kg, the combustion calorific value is 840,000 kcal.

  Since the amount of heat required for drying the sludge is about 63% of the combustion calorific value of the solid content, it means that the sludge moisture can be removed and burned by combustion calories from the solid content.

Moreover, in the case of sludge after methane fermentation treatment (called digested sludge), the calorific value of the dried solid is 3,000 to 3,500 kcal / kg, and in the case of 1,000 kg of digested sludge with a water content of 80%, The combustion calorific value with a dry solid content of 200 kg is 640,000 kcal when the unit calorific value is 3,200.
Now, 75% of the moisture of 80% (800 kg), that is, 600 kg of moisture is dried and removed in the pulverization processing device by the combustion heat of the obtained dry solid, and 600 kg of steam generated from the raw material is crushed by the pulverization drying device. A case is assumed where 25% moisture, that is, 200 kg is removed in the preliminary drying. The amount of heat required for drying in the pulverization apparatus is about 370,000 kcal, which corresponds to about 58% of the calorific value of combustion of the dry solid. Moreover, the latent heat of vaporization of 600 kg of steam generated by the powder processing apparatus is about 330,000 kcal, and the amount of heat necessary for heating the raw material in preliminary drying and removing 25% of water is about 180,000 kcal. This is about 55% of the latent heat of vaporization of the vapor in the powder processing apparatus.

  In other words, from the above calculation, even for digested sludge with a low calorific value, the combustion heat generated by the dry solids of the obtained sludge is used as the heat source of the powder processing device, and the steam generated by the powder processing device is used as the raw material. It means that digested sludge can be incinerated by using it for preliminary drying.

  As described above, according to the powder manufacturing apparatus 100c of the sixth embodiment, the sludge powder obtained by the drying / powder processing is effectively used as fuel, and the steam generated by the powder processing apparatus 100c is used for the preliminary drying of the raw material. By this, sludge can be incinerated.

As Example 7, the pulverization process in the case where the raw material is biomass such as thinned wood, pruned wood, and rice straw will be described.
Thinned wood, pruned wood, rice straw, etc. have a low moisture content of about 60%. The amount of heat required to dry the water contained in these materials can be smaller than that of the high water content raw material. When these raw materials are made into dry powder or molded pellets and burned as fuel, a large excess of thermal energy can be obtained in addition to the amount of heat necessary for drying the raw materials.

  FIG. 9 is a diagram showing the configuration of the powder manufacturing apparatus 100d of the seventh embodiment. As shown in FIG. 9, the powder manufacturing apparatus 100d of the seventh embodiment includes a raw material supply apparatus 10, a pulverization processing apparatus 20, a powder recovery apparatus 30, an exhaust processing apparatus 40, and a circulating airflow temperature adjustment apparatus 50d. However, compared with each component shown in Example 6, the circulating temperature adjusting device 50d has a structure in which a steam generator 58 is installed in the heating furnace 51. Water is supplied to the steam generator 58, and water is heated with surplus thermal energy of the heating furnace 51 to generate steam. That is, in the powder manufacturing apparatus 100d, the steam generator 58 can be effectively used as a highly efficient biomass fuel boiler.

  In particular, some sludge from food factories has a high calorific value. In such sludge treatment, raw sludge is used as dry powder, and the obtained powder is used as fuel, or the powder is formed into pellets as fuel, used as a drying heat source for raw sludge, and sludge is incinerated. Steam can be generated by surplus combustion energy.

  The powder manufacturing apparatus 100d of the seventh embodiment can effectively use the surplus heat amount as a high-efficiency biomass fuel boiler using the sludge having such a high combustion calorific value.

  As mentioned above, although the preferable example in the example of composition of the powder manufacture device of the present invention was illustrated and explained, it will be understood that various changes are possible without departing from the technical scope of the present invention. .

  The powder production apparatus of the present invention can be used as a powder production apparatus for processing food raw materials such as vegetables, seaweed, and medicinal herbs, as well as food processing by-products such as raw okara, brown tea, rice bran, sake lees, and apple pomace.

The block diagram which shows typically the structural example of the whole powder manufacturing apparatus concerning Example 1 of this invention. The figure which shows the example of piping of the raw material supply apparatus 10 and the grinding | pulverization processing apparatus 20 (the 1) The figure which shows the example of piping of the raw material supply apparatus 10 and the grinding | pulverization processing apparatus 20 (the 2) The figure which shows the example of piping of the raw material supply apparatus 10 and the grinding | pulverization processing apparatus 20 (the 3) The figure which shows the structure of the grinder 22 The figure which shows the structure of the powder manufacturing apparatus 100a of the present Example 2. The figure which shows the structure of the powder manufacturing apparatus 100b of the present Example 3. The figure which shows the structure of the powder manufacturing apparatus 100c of the present Example 6. The figure which shows the structure of the powder manufacturing apparatus 100d of the present Example 7. The figure which shows the fluidized-air dryer disclosed by Unexamined-Japanese-Patent No. 2007-78207. The figure which shows the drying system of the water-containing organic waste of the conventional Unexamined-Japanese-Patent No. 2009-154100 publication A diagram showing a conventional apparatus using a circulating fluidized bed furnace described in JP-A-11-37410.

DESCRIPTION OF SYMBOLS 10 Raw material supply apparatus 11 Hopper 12 Fixed supply apparatus 20 Crushing processing apparatus 21 Container 21A Lower container 21B Upper container 21a 1st discharge port 21b 1st inlet 21e Raw material inlet 21c 2nd discharge port 21d 2nd inlet 21g 1st Discharge port 21h 1st inflow port 21i 2nd discharge port 21f Ventilation path 22 Crusher 30 Powder recovery device 31 Cyclone separator 32 Powder hopper 33 Rotary valve 40 Exhaust treatment device 41 Cooler 50 Circulating airflow temperature control device 51 Heating furnace 52 Burner 53 Circulating Airflow Temperature Controller 55 Chimney 56 Fuel Supply 58 Steam Generator 59 Electric Heater 60 Support Member 61 Body Member 62 Rectifier Plate 70 Casing 71 Suction Port 72 Discharge Port 73 Impeller 74 Screen 75 Electric Motor 80 Raw Material Predrying Device 81 Pre-dryer DESCRIPTION OF SYMBOLS 2 Vacuum apparatus 100 Powder manufacturing apparatus 101 1st circulation path 101a piping 101b piping 201 2nd circulation path 201a piping 201b piping 201c piping 202 Circulating blower 301,302 Piping 401 Conveyance path 501 Temperature controller 502 Pressure controller 503 Gas analysis controller 504 Temperature controller 601 Fuel control valve 602 Combustion air control valve 603 Pressure control valve 604 Gas introduction control valve 605 Control valve 606 Temperature control valve

Claims (10)

A powder production apparatus,
A pipe connected from the first discharge port of the container to the suction port of the pulverizer; and a pipe connected from the discharge port of the pulverizer to the first inlet of the container; the container and the pulverizer A first circulation path forming a fluid circulation path therebetween;
A conduit connected to the circulating airflow temperature controller from the second outlet of the container via the powder recovery device and the exhaust treatment device, and a conduit connected to the second inlet of the container from the circulating airflow temperature controller A double fluid circulation path comprising a second circulation path that forms a fluid circulation path between the container, the powder recovery device, the exhaust treatment device, and the circulation airflow temperature controller,
In the first circulation path, the raw material introduced from the outside is circulated between the pulverizer and the container together with the circulating air flow to advance powdering of the raw material,
In the second circulation path, the powder guided from the first circulation path together with the circulating airflow is captured and recovered by the powder recovery device, and the temperature of the circulating airflow after capturing the powder is controlled by the circulating airflow temperature controller. The powder manufacturing apparatus is characterized in that the circulating air flow is circulated through the second circulation path by adjusting the pressure and introducing the second air flow into the second inlet of the container. In the first circulation path, a swirling flow of the circulating airflow is formed in the container, and the raw material is classified by a centrifugal force and the circulating airflow by the swirling flow,
The powder that has been pulverized to a predetermined size by the classification is discharged from the second outlet of the container together with the circulating airflow, and powder that has not yet been pulverized to the predetermined size is discharged from the container. The powder production apparatus according to claim 1, wherein the powder is circulated from the first discharge port to the first circulation path.   The powder production apparatus according to claim 1 or 2, wherein the circulating airflow is any one of superheated steam, nitrogen, and an inert gas.   The circulating airflow is heated by the circulating airflow temperature controller, the raw material is pulverized by the heated circulating airflow, the raw material is dried, the raw material is sterilized, the raw material is cooked, and the raw material is heated. The powder manufacturing apparatus according to any one of claims 1 to 3, wherein any one or a combination of a roasting process and a vaporization process of the liquid containing the raw material is performed.   The pulverizer includes a casing provided with the suction port and the discharge port, an impeller installed in the casing, and a screen, and the impeller sucks the circulating airflow from the suction port. The powder manufacturing apparatus of any one of Claim 1 to 4 sent out to the said discharge outlet.   6. The powder captured and recovered by the powder recovery apparatus, or the powder molded into pellets is used as a fuel for heating the circulating airflow in the apparatus. The powder manufacturing apparatus of any one of Claims.   The powder production apparatus according to claim 6, wherein steam is generated from feed water by the surplus combustion calorific value of the fuel.   The powder manufacturing apparatus according to claim 1, wherein superheated steam is used as the circulating airflow, and an amount corresponding to the steam generated from the raw material is extracted from the circulating airflow and used for preheating and preliminary drying of the raw material. .   Foods such as vegetables, cereals, beans, potatoes, mushrooms, fish, seaweed, tea leaves, medicinal herbs, or raw foods such as raw okara, fermented fish residue, tea galley, coffee candy, strawberry dashigara, apple squeezed potato, sake lees Any one of processing by-products, biomass such as wood, thinned wood, pruned wood, bamboo, grass and rice straw, organic matter such as sludge or water-containing waste, or a combination thereof. The powder manufacturing apparatus of Claim 1.   The powder production apparatus according to any one of claims 1 to 8, wherein the raw material is any one or a combination of chemical products such as chemicals, plastics, rubbers, pharmaceuticals, cosmetics, and paints.

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