JP2002257377A - Dry storage device and method of drying hoardings - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a dry storage device with a high coefficient of performance(COP) and a high dehumidifying capacity (dehumidifying performance) per input of a compressor and a method of drying hoardings. SOLUTION: This device is provided with a storage bin 101 where hoardings 100 are stored, a heating tube 105 that is installed in the storage bin 101 with a fluid circulating inside, a booster 3 raising the pressure of refrigerant, a condenser 4 condensing the refrigerant to heat the fluid inside the heating tube 105, an evaporator 2 evaporating the refrigerant to cool down outside air to the temperature of a dew point or below, the first heat exchanger 51 evaporating the refrigerant at the intermediate pressure between the condensing pressure of the condenser 4 and the evaporating pressure of the evaporator 2 to cool down the outside air, the second heat exchanger 52 condensing the refrigerant at the intermediate pressure to heat the outside air, and air paths connecting the first heat exchange part 51, the evaporator 2, the second heat exchange part 52 and the storage bin 101 in this order.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a dry storage device and a method for drying stored materials, and more particularly to a cooling dehumidifying type dry storage device for drying stored materials such as grains and a drying method.

[0002]

2. Description of the Related Art Conventionally, a dry storage device (dry air generator: DAG) for storing grains and the like, for example, soybeans, onions, garlic, and the like in storage bins, and drying and storing the stored contents in the storage bins by cooling and dehumidification. Are known. FIG. 10 shows the configuration of such a conventional dry storage device. As shown in FIG. 10, the dry storage device includes a storage bin 401 that stores a storage object 400 such as grain, and a dryer 402 that sends dry air into the storage bin 401. The dryer 402 includes a booster 411 that compresses the refrigerant, a condenser 412 that condenses the compressed refrigerant and heats the outside air OA, and a depressurizer 413 that depressurizes the condensed refrigerant,
The evaporator 414 is provided with an evaporator 414 for evaporating the air to cool the outside air OA below the dew point temperature and a blower 415 for sending the outside air OA to the evaporator 414. The evaporator 414 cools the outside air OA below the dew point and removes moisture in the outside air OA. The outside air OA cooled below the dew point is heated by the condenser 412,
It is supplied to the storage bin 401. The booster 411, the condenser 412, the throttle 413, and the evaporator 414 constitute a heat pump HP that pumps heat from the outside air OA flowing through the evaporator 414 to the outside air OA flowing through the condenser 412.

FIG. 11 is a psychrometric chart showing an air conditioning cycle in a conventional dry storage device. In FIG. 11, reference numerals K to M, OA, and EX correspond to the path states denoted by the respective reference numerals in FIG. As shown in FIG. 11, in a conventional dry storage device, outside air OA is sent to an evaporator 414 by a blower 415 (state K).
In the evaporator 414, the outside air OA is cooled to a temperature equal to or lower than the dew point temperature, and the dry bulb temperature is reduced and the absolute humidity is reduced to reach the state L. This state L is on the saturation line in the psychrometric chart. The air in the state L is heated by the condenser 412, the dry bulb temperature rises while maintaining the absolute humidity constant, reaches the state M, and is supplied to the storage bin 401. The dry air supplied to the inside of the storage bin 401 absorbs the moisture of the storage object 400, raises the absolute humidity, lowers the dry bulb temperature by the heat of adsorption, and is exhausted from the upper part of the storage bin 401 (EX). .

[0004] The use of such a dry storage device makes it possible to dry the storage material in the storage bin slowly and without difficulty, and there is a concern that dew condensation in storage drying and a rapid decrease in drying ability in a thick grain layer may occur. There is no. In addition, since the grain can be dried at a temperature that does not alter the starch, the grain can be stored without deteriorating the quality of the grain.

[0005]

However, in the conventional dry storage device, since the amount of cooling to the dew point is large, about half of the refrigeration effect in the evaporator of the heat pump is consumed to deprive the sensible heat load, and compression is performed. Dehumidification capacity per unit input (dehumidification performance) was low.

The amount of heat for reheating the air that has exited the evaporator 414 is the amount of heat released from the condenser 412. Since the amount of heat is not sufficient, the temperature of the air supplied to the storage bin 401 is not so high. The drying capacity was low due to its low relative humidity. Furthermore, the storage 4 such as cereals in the storage bin 401
00 is a process of isenthalpy change, but when the temperature of the supplied air is low, the relative humidity immediately rises, and the drying capacity per unit flow of air is low. It was necessary to increase the amount of air supplied to the air.

The present invention has been made in view of the above-mentioned problems of the prior art, and has a high operating coefficient (COP) and a high dehumidifying capacity per input of a compressor (dehumidifying performance). An object of the present invention is to provide a method for drying an object.

[0008]

SUMMARY OF THE INVENTION In order to solve the problems in the prior art, one aspect of the present invention is to provide a storage bin in which storage items are stored, a storage bin installed in the storage bin, and an internal storage bin. A heat transfer tube through which the fluid flows, a booster that pressurizes the refrigerant, a condenser that condenses the refrigerant and heats the fluid inside the heat transfer tube, and evaporates the refrigerant to lower the external air to a temperature equal to or lower than the dew point. An evaporator for cooling, provided in a refrigerant path connecting the condenser and the evaporator, evaporating the refrigerant at an intermediate pressure between the condensation pressure of the condenser and the evaporation pressure of the evaporator, and external air First heat exchanging means for cooling the condenser, and a refrigerant passage connecting the condenser and the evaporator, wherein the refrigerant is cooled at an intermediate pressure between the condensation pressure of the condenser and the evaporation pressure of the evaporator. Second heat exchange means for condensing and heating external air A dry storage apparatus characterized by comprising an air path for connecting the first heat exchange means and said evaporator and said second heat exchange means and the storage bin in this order.

In another aspect of the present invention, a storage bin in which stored items are stored, a booster for increasing the pressure of a refrigerant, a condenser for condensing the refrigerant and heating external air, and evaporating the refrigerant. An evaporator that cools the external air to a temperature equal to or lower than the dew point, and is provided in a refrigerant path connecting the condenser and the evaporator, and is provided between the condensation pressure of the condenser and the evaporation pressure of the evaporator. A first heat exchange means for evaporating the refrigerant at a pressure to cool the external air and a refrigerant path connecting the condenser and the evaporator, and Second heat exchange means for condensing the refrigerant at a pressure intermediate to the evaporation pressure and heating the external air;
A dry storage device comprising: a heat exchange means, an evaporator, a second heat exchange means, an air path connecting the condenser and the storage bin in this order.

[0010] Further, another aspect of the present invention is to store a stored product in a storage bin, flow a fluid through a heat transfer tube installed in the storage bin, pressurize the refrigerant, and store the stored product in a condenser. Condensing the refrigerant to heat the fluid inside the heat transfer tube, evaporating the refrigerant in an evaporator to cool the external air to a temperature equal to or lower than the dew point, The refrigerant is evaporated at an intermediate pressure between the condensation pressure of the evaporator and the evaporation pressure of the evaporator to cool the external air, and the second heat exchange means converts the condensation pressure of the condenser to the evaporation pressure of the evaporator. The refrigerant is condensed at an intermediate pressure to heat the external air, and the first heat exchange means, the evaporator, the second heat exchange means, and the storage bin are connected in this order by an air path. Is heated in the second heat exchange means. A method for drying a storage, comprising supplying external air to the storage bin, supplying a fluid inside the heat transfer tube heated in the condenser to the storage bin, and drying the storage. is there.

According to another aspect of the present invention, a storage object is stored in a storage bin, the pressure of the refrigerant is increased, and
The refrigerant is condensed to heat the external air, and in the evaporator, the refrigerant is evaporated to cool the external air to a temperature below the dew point. In the first heat exchange means, the condensing pressure of the condenser and the evaporation The refrigerant is evaporated at a pressure intermediate to the evaporation pressure of the condenser to cool the external air, and the second heat exchange means converts the refrigerant at a pressure intermediate between the condensation pressure of the condenser and the evaporation pressure of the evaporator. The external air is heated by condensing, and the first heat exchange means, the evaporator, the second heat exchange means, and the condenser are connected in this order by an air path, and the heat is heated in the condenser. A method for drying a stored product, comprising supplying the stored external air to the storage bin and drying the stored product.

According to the present invention, of the heat quantity for cooling the air, in the cooling step up to the dew point, heat is exchanged with the air after dehumidification, so that most of the heat quantity cooled in the evaporator is used for the dehumidification step. Therefore, the dehumidifying capacity per input of the compressor is increased.

Further, since the high heat source of the heat pump is also used as a heating source during the drying process, the drying process does not become an isenthalpy process, but is close to an isothermal process. Therefore, since the rise in the relative humidity of the air during the drying step is small, the drying action is continued, and the amount of air to be blown can be reduced. Also,
Since the maximum temperature of the air can be lowered for the same amount of heat, the condensation temperature of the heat pump can be lowered. Therefore, the compression ratio of the heat pump is reduced, and the operating coefficient (COP) is improved, so that power costs can be saved.

Further, when the heat exchanging means is used as a pre-cooling / pre-heating heat exchanger, the working medium of the heat exchanging means and the working medium of the heat pump become the same, and the refrigerant charging process can be commonized. Manufacturing costs and maintenance are low. In addition, since the pre-cooling / pre-heating heat exchanger can be manufactured as a single unit, and without the need for the internal wick of the heat pipe, it can be manufactured using ordinary air / refrigerant heat exchanger coil production equipment without an internal wick. , Low manufacturing cost.

The multi-economizer effect of the heat pump reduces the enthalpy of refrigerant at the inlet of the evaporator and increases the refrigeration effect of the refrigerant per unit flow rate, thereby increasing the dehumidifying effect and energy efficiency.

In a preferred aspect of the present invention, the first heat exchanging means and the second heat exchanging means are configured such that air flowing through each heat exchanging means flows opposite to each other. The refrigerant path is formed in the first heat exchange means and the second heat exchange means in at least a pair of first penetration portions in a first plane substantially orthogonal to the flow of air. A first surface and a second surface substantially perpendicular to the air flow different from the first surface. 1
An intermediate stop is provided at a position where the intermediate stop moves from within the plane to the second plane.

With this configuration, from the viewpoint of heat exchange between the air, since it is counter-flow heat exchange, high heat exchange efficiency can be achieved. A second surface having at least a pair of first through portions and a second through portion in the first surface, forming a pair of refrigerant paths, and being substantially orthogonal to a flow of regenerated air different from the first surface; Since the heat exchanger has at least a pair of first through portions and a second through portion in the plane and forms a pair of refrigerant paths, the heat exchanger can be formed as a small and compact as a whole. In addition, since an intermediate throttle is provided at a position where the inside of the first surface moves into the second surface, the pressure of evaporation or condensation of the first and second penetration portions in the second surface is reduced by the first surface. Can be set to a value lower than the pressure of the evaporation or condensation of the first and second through-portions, so that the heat exchange between the air flowing through the respective through-portions can be close to the counter-flow heat exchange, Heat exchange efficiency can be increased. Note that the shapes of the first surface and the second surface are typically rectangular planes.

[0018]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, a first embodiment of a dry storage device according to the present invention will be described in detail with reference to FIGS. FIG. 1 is a diagram schematically showing a flow in the drying storage device according to the first embodiment of the present invention, and FIG. 2 is a diagram showing a configuration example of a dryer of the drying storage device of FIG. The dry storage device according to the present embodiment cools and dehumidifies outside air below its dew point temperature and heats circulating water with a condenser, and includes a heat pump HP1 inside. The outside air whose humidity has been reduced by the dry storage device and the heated circulating water are respectively supplied to the storage bins to dry-store the stored items.

As shown in FIG. 1, the drying storage device includes a storage bin 101 for storing a storage object 100, and a dryer 102 for supplying dry air and hot water to the storage bin 101. As shown in FIGS. 1 and 2, this dryer 102 is a blower 1 for introducing air OA from outside.
A refrigerant evaporator 2 that heats and evaporates the refrigerant, a booster 3 that compresses a refrigerant that has been evaporated and gasified in the evaporator 2,
The apparatus includes a refrigerant condenser 4 for cooling and condensing the refrigerant, and a heat exchanger 5 acting as an economizer. Heat exchanger 5
Performs indirect heat exchange between the air before and after flowing into the evaporator 2 via a refrigerant, a first heat exchange unit 51 that evaporates the refrigerant and cools the air, And a second heat exchange section 52 for condensing the air and heating the air. These devices are housed inside a cabinet 10, and the cabinet 10 is formed as, for example, a rectangular parallelepiped case made of a thin steel plate.

An intake port 11 is opened at the uppermost part of the front surface of the cabinet 10, and external air OA is introduced into the dryer 102 through the intake port 11. Inlet 11
A filter 12 is provided in the vicinity of to prevent dust from entering the apparatus from the outside. In the cabinet 10, an air path through which air flows is formed by a partition plate extending in the horizontal or vertical direction, and the air OA introduced from the intake port 11 passes through the uppermost air path 13a and passes through the middle air path. 13b, and flows from the middle air path 13b to the lowermost air path 13c. The air flowing into the lowermost air path 13c is supplied to the storage bin 101 from a supply port 16 formed at the lowermost portion of the rear surface of the cabinet 10.

In the above-described middle air path 13b, the first heat exchange section 5 of the heat exchanger 5 is arranged along the flow direction of air.
1, a blower 1 and an evaporator 2 are arranged in this order. Here, the evaporator 2 cools the air introduced from the outside to a temperature lower than its dew point and recovers moisture in the air as dew condensation water. A drain pan 14 is provided below the evaporator 2. A drain tank 15 is disposed in the lowermost air path 13 c located below the drain pan 14, and the moisture in the outside air OA condensed by the evaporator 2 is collected by the drain pan 14 and enters the drain tank 15. Stored. The drain pan 14 is preferably provided so as to cover not only the evaporator 2 but also the lower part of the heat exchanger 5. In the first heat exchange section 51 of the heat exchanger 5, air is mainly pre-cooled. However, since a part of moisture may be condensed here, it is particularly preferable to provide the air below the first heat exchange section 51. .

In the lowermost air path 13c, a drain tank 15 and a second heat exchange section 52 of the heat exchanger 5 are sequentially arranged along the flow direction of air. In addition, a room 13 d containing a booster 3, a condenser 4, a water tank 17 storing circulating water, and a pump 18 for pumping circulating water from the water tank 17 to the condenser 4 is provided in the upper rear part of the cabinet 10. Are formed. A flange 19 for connecting a pipe is provided on the rear surface of the room 13d.

The storage bin 101 is provided with a floor mesh 103 having a plurality of ventilation holes. A storage 100 is stored above the floor mesh 103, and a preheating chamber 104 is formed below the storage mesh 100. A detoured heat transfer tube 105 is provided inside the storage bin 101. The heat transfer tube 105 is connected to the flange 19 of the dryer 102, and inside the heat transfer tube 105, hot water heated by the condenser 4 of the dryer 102 flows. The heated hot water is supplied to the storage bin 101 via the heat transfer tube 105. The heat transfer tube 1 according to the present embodiment
Although water is allowed to flow through the interior of 05, the invention is not limited to this, and other fluids may flow.

As shown in FIG. 1, the refrigerant path in the dryer 102 includes a path 40 connecting the evaporator 2 and the booster 3 and a path 41 connecting the booster 3 and the condenser 4. And a path 42 connecting the condenser 4 and the heat exchanger 5
And a path 43 connecting the heat exchanger 5 and the evaporator 2. In the heat exchanger 5, the refrigerant path passes through the first heat exchange unit 51 and the second heat exchange unit 52, respectively, and the refrigerant is evaporated in the first heat exchange unit 51. Thus, an evaporating section 61 for cooling the air OA flowing through the first heat exchange section 51 is formed, and the air R flowing through the second heat exchange section 52 by condensing the refrigerant in the second heat exchange section 52 is formed. A condensing section 62 is formed for heating. A throttle 48 is arranged in the refrigerant path 42 on the upstream side of the first heat exchange section 51 of the heat exchanger 5, and a throttle 49 is arranged in the refrigerant path 43 on the downstream side of the second heat exchange section 52. ing. These apertures 48, 49
For example, an orifice, a capillary tube, an expansion valve, or the like can be used.

FIG. 3 is an enlarged view showing a refrigerant path in the heat exchanger 5 of the dryer of FIG. The refrigerant path including the evaporating section 61 and the condensing section 62 is the first refrigerant path.
The heat exchange part 51 and the second heat exchange part 52 are alternately and repeatedly penetrated. That is, as shown in FIG. 3, the refrigerant paths in the heat exchanger 5 are sequentially arranged from the condenser 4 side to the evaporating section 6.
1a, condensation section 62a, condensation section 62b,
Evaporation section 61b, evaporation section 61c, condensation section 62c, condensation section 62d, evaporation section 61d, evaporation section 61e, condensation section 62
e.

Here, the air OA before passing through the evaporator 2
The first heat exchange unit 51 for flowing the air R and the second heat exchange unit 52 for flowing the air R after passing through the evaporator 2 are accommodated in separate rectangular parallelepiped spaces. In these rectangular parallelepiped spaces, a plurality of heat exchange tubes are arranged in parallel on a plane orthogonal to the flow of air as refrigerant paths. The first heat exchange part 51 and the second heat exchange part 52 are provided with a partition wall 510 and a partition wall 520 adjacent to each other, and a heat exchange tube is provided through the two partition walls 510 and 520. Have been. As another form, the heat exchanger 5 divides one rectangular parallelepiped space by one partition, and a heat exchange tube penetrates the partition to connect the first heat exchange part and the second heat exchange part. You may comprise so that it may penetrate alternately.

The evaporating section 61b and the evaporating section 6
End 1c, evaporating section 61d and evaporating section 6
Each end of 1e is a U-tube (YouTube) 63
Connected by Similarly, condensing section 62
a and end of condensing section 62b, condensing section 62
c and the ends of the condensation section 62d are also connected by U-tubes 64, respectively. With such a configuration, in the refrigerant path 42, the refrigerant flowing from the evaporating section 61a toward the condensing section 62a is guided to the condensing section 62b by the U-tube 64. The refrigerant guided to the condensing section 62b further flows into the evaporating section 61b, is introduced into the evaporating section 61c by the U-tube 63, and further flows into the condensing section 62c. As described above, the refrigerant path in the heat exchanger 5 is formed by the meandering small tube group, and the small tube group passes through the inside of the first heat exchange unit 51 and the second heat exchange unit 52 while meandering, and has a high temperature. It comes into contact with air and cold air alternately.

Next, the flow of the refrigerant between the devices in the dryer 102 will be described with reference to FIGS. The refrigerant gas compressed by the booster 3 is guided to the condenser 4 via a refrigerant gas pipe 41 connected to a discharge port of the booster 3. In the condenser 4, the refrigerant gas compressed by the booster 3 is supplied from a water tank 17 by a pump 18 to the condenser 4.
Is cooled and condensed by the circulating water supplied to the heater, and the circulating water is heated by the refrigerant.

The refrigerant liquid that has exited the condenser 4 is decompressed and expanded by the throttle 48 and a part of the refrigerant liquid evaporates (flashes).
The refrigerant in which the liquid and the gas are mixed reaches the evaporating section 61a of the first heat exchange section 51, where the refrigerant liquid flows so as to wet the inner wall of the tube of the evaporating section 61a. The refrigerant liquid is heated and evaporated by the air OA introduced from the outside while flowing through the evaporating section 61a, and the air OA before flowing into the evaporator 2 is cooled (precooled). At this time, the refrigerant itself is heated to increase the gas phase.

As described above, since the evaporating section 61a and the condensing section 62a are constituted by a series of tubes, the refrigerant gas evaporated in the evaporating section 61a (and the non-evaporated refrigerant liquid) flows into the condensing section 62a. I do. In the condensing section 62a, the air R that has been cooled and dehumidified in the evaporator 2 and has a lower temperature than the air in the evaporating section 61a is heated (reheated). It flows into the next condensation section 62b. The refrigerant is further deprived of heat by the low-temperature air R while flowing through the condensing section 62b, and condenses the gas-phase refrigerant.

The condensed refrigerant liquid flows into the next evaporating section 61b and the following evaporating section 61c,
In the same manner as described above, the air OA before flowing into the evaporator 2 is cooled (precooled). Further, the refrigerant gas flows into the condensing sections 62c and 62d to heat the air R. As described above, the refrigerant flows through the refrigerant path in the heat exchanger while repeating the phase change between the gas phase and the liquid phase, and the air OA before being cooled by the evaporator 2 and the absolute humidity by being cooled by the evaporator 2. Heat exchange is performed indirectly with the reduced air R.

The refrigerant liquid condensed in the last condensing section 62e is decompressed and expanded by the throttle 49 arranged downstream of the second heat exchange section 52 to lower the temperature. And
The refrigerant reaches the evaporator 2 and evaporates in the evaporator 2. The air Q that has passed through the first heat exchange unit 51 is cooled by the heat of evaporation of the refrigerant. The refrigerant evaporated and gasified by the evaporator 2 is guided to the suction side of the booster 3. Then, the above-described cycle is repeated.

Next, the operation of the heat pump HP1 included in the dry storage device according to the present embodiment will be described.
FIG. 4 shows a heat pump HP included in the dry storage device of FIG.
1 is a refrigerant Mollier diagram of FIG. In the diagram shown in FIG. 4, HFC134a is used as the refrigerant, and the enthalpy is plotted on the horizontal axis and the pressure is plotted on the vertical axis. HFC13
In addition to HFC134a, HFC407C and HFC410A can also be used as refrigerants. When these refrigerants are used, the operating pressure range shifts to a higher pressure side than in the case of HFC134a.

In FIG. 4, point a indicates the state of the refrigerant evaporated in the evaporator 2 in FIG. 1, and the refrigerant at this time is in a saturated gas state. The pressure of the refrigerant is 0.30 MPa, the temperature is 1 ° C., and the enthalpy is 399.2 kJ / kg. Point b indicates a state in which this gas is sucked and compressed by the pressure booster 3, that is, a state at the discharge port of the pressure booster 3. At this time, the refrigerant has a pressure of 1.89 MPa and is in a superheated gas state. .

The refrigerant gas in the state at the point b is cooled in the condenser 4 and reaches the state shown at the point c. At this time, the refrigerant is in a saturated gas state, and its pressure is 1.89MPa.
a, The temperature is 65 ° C. The refrigerant is further cooled and condensed under this pressure to reach the state indicated by point d. At this time, the refrigerant is in a saturated liquid state, and its pressure and temperature are the same as the pressure and temperature at point c. The enthalpy at this time is 295.8 kJ / kg.

This refrigerant liquid is decompressed by the throttle 48,
Flows into the evaporating section 61a of the heat exchange section 51. The state at this time is indicated by a point e, in which a part of the liquid is evaporated and the liquid and the gas are mixed. The pressure at this time is an intermediate pressure between the condensing pressure of the condenser 4 and the evaporating pressure of the evaporator 2, and in this embodiment, 0.30 MPa and 1.8.
The value is between 9 MPa.

In the evaporating section 61a, the coolant evaporates under the above-mentioned intermediate pressure, and the state becomes a point f1 located at the middle of the saturated liquid line and the saturated gas line at the same pressure. In this state, a part of the liquid has evaporated, but a considerable amount of the refrigerant liquid remains.
Then, the refrigerant in the state indicated by the point f1 flows into the condensation sections 62a and 62b. Condensing section 62a
At 62b and 62b, the refrigerant is deprived of heat by the low-temperature air R flowing through the second heat exchange section 52, and reaches the state at the point g1.

The refrigerant in the state at the point g1 is supplied to the evaporating section 6
1b and 61c, where heat is deprived and the liquid phase is increased to reach the state at point f2.
And 62d. Condensing sections 62c and 62
At d, the refrigerant increases its liquid phase and reaches the state of point g2. The point g2 is located on the saturated liquid line in the Mollier diagram. At this time, the temperature of the refrigerant is 15 ° C., and the enthalpy is 22 °.
0.5 kJ / kg. Similarly, evaporation and condensation in the evaporating sections 61d and 61e and the condensing section 62e are repeated, but in the Mollier diagram of FIG. 4, the evaporating sections 61d and 61e and the condensing section 62e are omitted, and the condensing section 62d is Are shown as connected.

The refrigerant liquid in the state of the point g2 is reduced in pressure by the throttle 49 to 0.30 MPa which is a saturation pressure at a temperature of 15 ° C., and reaches a state shown by a point h. The refrigerant in the state at the point h reaches the evaporator 2 as a mixture of a refrigerant liquid and a gas at 1 ° C., where it takes heat from the air Q and evaporates to become a saturated gas in the state indicated by the point a. This saturated gas is again supplied to the booster 3
And the above-described cycle is repeated.

As described above, in the heat exchanger 5, the refrigerant changes its evaporation state in the evaporating section 61 from point e to point f1 or from point g1 to point f2.
In the condensing section 62, the state of condensation changes from point f1 to point g1 or from point f2 to point g2, and the heat transfer coefficient is very high because evaporation heat transfer and condensation heat transfer are performed. High heat exchange efficiency.

Here, the booster 3, the condenser 4, the throttle 48,
Considering the compression heat pump HP1 including the evaporator 49 and the evaporator 2, when the heat exchanger 5 according to the present invention is not provided, the refrigerant at the point d in the condenser 4 is returned to the evaporator 2 via the throttle. Therefore, the enthalpy difference available in the evaporator 2 is only 399.2-295.8 = 103.4 kJ / kg. However, when the heat exchanger 5 according to the present invention is provided, 399.2-2205 = 178.7 kJ / kg, and the amount of gas circulated to the booster for the same cooling load and, consequently, the required power are reduced by 42. % (= 1-103.4 / 1)
78.7) can also be reduced. That is, the same operation as in the subcool cycle can be provided. As described above, the dry storage device of the present invention includes the heat pump HP1
Due to the economizer effect, the refrigerant enthalpy at the inlet of the evaporator 2 is reduced, and the refrigerant refrigeration effect per unit flow rate is high, so that the dehumidifying effect and the energy efficiency are increased.

FIG. 5 is a psychrometric chart showing an air conditioning cycle in the dry storage device of FIG. In FIG. 5, reference numerals P to T, OA, and EX correspond to the states of air denoted by the respective reference numerals in FIG. The air OA introduced from the outside passes through the uppermost air path 13 a in FIG. 2 and is sent to the first heat exchange unit 51 of the heat exchanger 5 (air P), and is cooled by the refrigerant evaporated in the evaporation section 61. It cools down to some extent and lowers the dry bulb temperature while keeping the absolute humidity constant (air Q). This is a pre-cooling before the evaporator 2 cools down to the dew point temperature or lower, so it can be called pre-cooling.

In the evaporator 2, the air Q is cooled to a temperature below its dew point temperature by the refrigerant evaporating at a low temperature, and while the moisture is deprived, the absolute humidity is reduced to 5 g / kg DA and the dry bulb temperature is reduced to 5 ° C. (Air R). DA in the unit of absolute humidity indicates dry air.

The air R (absolute humidity 5 g / kg DA, dry bulb temperature 5 ° C.) flows into the second heat exchange section 52 of the heat exchanger 5 and is heated to a certain extent by the refrigerant condensing in the condensing section 62. , The dry bulb temperature (5
(Air S) to a temperature between 60 ° C and 60 ° C. Since this is preliminary heating before heating in the preheating chamber 104 in the storage bin 101, it can be referred to as preheating.

The hot water heated in the condenser 4 is sent to the preheating chamber 104 of the storage bin 101 by the pump 18, and the air S exiting the second heat exchange section 52 is heated in the preheating chamber 104. The dry bulb temperature is further raised to 60 ° C. while keeping the absolute humidity constant (air T). The air T blows out upward through the ventilation holes of the floor mesh 103, deprives the water contained in the storage objects 100 in the storage bin 101, raises the absolute humidity of itself, and is exhausted from the upper part of the storage bin 101. (EX).

Here, in the cycle on the air side shown in the psychrometric chart of FIG. 5, the heat quantity ΔQ obtained by heating the air S in the preheating chamber 104 is heating by utilizing waste heat, and the air Q is The amount of heat Δi cooled is the dehumidifying cooling effect, and the heat recovery by the heat exchanger as an economizer is ΔH.

As described above, in the heat exchanger 5, the air OA introduced from the outside is pre-cooled by the evaporation of the refrigerant in the evaporating section 61, and the air R is heated by the condensation of the refrigerant in the condensing section 62. The refrigerant evaporated in the evaporation section 61 is condensed in the condensation section 62. As described above, the heat exchange between the air before and after being cooled by the evaporator 2 is indirectly performed by the same evaporation and condensation of the refrigerant.

As described above, in the dry storage device according to the present invention, the heat exchanger 5 is used as a pre-cooling / pre-heating heat exchanger, and the working fluid of the heat exchanger 5 and the working fluid of the heat pump HP1 are the same. Since the refrigerant charging process can be shared, the manufacturing cost and the maintenance cost are low. In addition, the pre-cooling / pre-heating heat exchanger can be manufactured as a single unit, and does not require the internal wick of the heat pipe, and can be manufactured using ordinary air / refrigerant heat exchanger coil production equipment without an internal wick. Therefore, the manufacturing cost is low.

Furthermore, since the pre-cooling of the air and the heating of the air after dehumidification are performed by using the internal working medium using the heat pump HP1, the apparatus is simple, and most of the cooling capacity of the heat pump is reduced to the air. Since it can be used to condense water, the dehumidifying ability is high.

In the case of cooling and dehumidifying air, if the air is cooled to the dew point as it is, a large amount of cooling is required. Therefore, a considerable part of the cooling effect of the heat pump is consumed for that purpose, and the dehumidifying capacity (input dehumidifying performance) per compressor input is low. . Therefore, an air / air heat exchanger 5 was provided before and after the evaporator 2 to perform pre-cooling and reheating (pre-heating) of the air to reduce the sensible heat ratio and reduce the amount of cooling to the dew point.

Next, a second embodiment of the dry storage device according to the present invention will be described in detail with reference to FIGS. FIG. 6 is a diagram schematically showing a flow in the dry storage device in the second embodiment, and FIG. 7 is a refrigerant Mollier diagram of the heat pump HP2 included in the dry storage device of FIG.
Members or elements having the same functions or functions as the members or elements in the above-described first embodiment are denoted by the same reference numerals, and parts that are not particularly described are the same as those in the first embodiment.

In the heat exchanger 150 in the dryer 202 according to the present embodiment, the condensing section 1 is provided between the condensing sections 162a and 162b of the second heat exchanging section 152.
Between 62c and 162d, the intermediate aperture 163,
164 is different from the first embodiment described above. Other configurations are the same as those of the first embodiment. Such an intermediate throttle is provided by the first heat exchanger 15.
It can also be provided on the side of one evaporating section.

In FIG. 7, points a to e are the same as those in the first embodiment shown in FIG. The evaporating section 16 of the heat exchanger 150
As described with reference to FIG. 4, the refrigerant in the state of the point e that has flowed into 1a is in a state where a part of the liquid has evaporated and the liquid and the gas have been mixed.

This refrigerant evaporates in the evaporating section 161a, and reaches a state indicated by a point f1 in the Mollier diagram of FIG. 7 which approaches the saturated gas line in the wet area. The refrigerant in this state enters the condensing section 162a, where it is condensed and reaches the state shown by point g1a. The refrigerant in the state of the point g1a is depressurized through the intermediate throttle 163, and reaches the state shown by the point g1b. That is, it flows from the condensing section 162a to the condensing section 162b via the throttle 163.

The refrigerant flowing into the condensing section 162b is condensed here, and reaches a state indicated by a point h1, which is in the wet area but close to the saturated liquid line. Then, evaporation section 1
61b, where it is condensed and reversed by a U-tube to enter the evaporating section 161c where it is further condensed and reaches the state indicated by point f2.

Thereafter, the refrigerant is supplied to the condensing section 162.
c, via the intermediate throttle 164 and the condensing section 162d, to the state shown by the points g2a, g2b and h2, and further via the evaporating sections 161d, 161e and the condensing section 162e to the points f3 and h3. It reaches the state shown by. This point h3 is on the saturated liquid line in the Mollier diagram, the temperature is 11 ° C., and the enthalpy is 215.0.
kJ / kg.

Similar to the first embodiment, the refrigerant liquid at the point h3 is supplied to the throttle 49 at a saturation pressure of 0.3 ° C. at a temperature of 1 ° C., as in the first embodiment.
The pressure is reduced to 0 MPa, the state at the point i is reached, and a mixture of the refrigerant liquid and the gas at 1 ° C. reaches the evaporator 2 where the air Q
And evaporates to become a saturated gas in the state shown by the point a on the Mollier diagram. This saturated gas is sucked into the booster 3 again, and the above-described cycle is repeated.

Here, the booster 3, the condenser 4, the throttle 48,
Considering the compression heat pump HP2 including the heat exchangers 49, 163, and 164 and the evaporator 2, the heat exchanger 15 according to the present invention is used.
When 0 is not provided, the refrigerant in the state of the point d in the condenser 4 is returned to the evaporator 2 through the throttle, so that the enthalpy difference available in the evaporator 2 is 399.2-295.8 = 1.
There is only 33.4 kJ / kg. However, when the heat exchanger 150 according to the present invention is provided, 399.2-215.
0 = 184.2 kJ / kg, and the amount of gas circulating to the booster for the same cooling load, and consequently the required power, is reduced by 44
% (= 1-103.4 / 184.2) can also be reduced. That is, the same operation as in the subcool cycle can be provided.

FIG. 8 shows a heat exchanger 15 according to this embodiment.
1 shows an example of the structure of 0. 8A is a front view as viewed in the air flow direction, FIG. 8B is a side view as viewed from a direction perpendicular to the air flow, and FIG. 8A is FIG. 8B.
FIG. In FIG. 8A, the air OA
Flows from the near side of the paper to the front, and the air R flows from the front to the near side. The tubes in the heat exchanger 150 are arranged in eight rows in four planes orthogonal to the flow of air. That is, they are arranged in four rows and eight columns along the flow of air. In FIG. 1 and FIG. 6, for convenience, the heat exchange tubes are described as having one row and one column, but typically each row includes a plurality of tube rows.
In addition, such heat exchangers may be arranged in parallel with the flow of air or in series, depending on the flow rate of the air.

Such a heat exchanger is inexpensive and is economical if used instead of an expensive heat pipe. Further, unlike the heat pipe, the working fluid can be made the same as that of the heat pump, so that maintenance is not required.

Although one embodiment of the present invention has been described above, the present invention is not limited to the above-described embodiment, and may be embodied in various forms within the scope of the technical idea. For example, the number of evaporating sections in the first heat exchanging section and the number of condensing sections in the second heat exchanging section of each refrigerant path are not limited to those shown.

In the above embodiment, the condenser 4
To heat the circulating water and supply it to the storage bin 101. However, the air heated in the second heat exchange section is directly heated by the condenser and supplied to the storage bin 101 to supply the storage bin 101 with the air. The storage 100 in 101 may be dried. FIG. 9 shows a configuration in the case where the air heated in the second heat exchange unit 52 is heated by the condenser 4 and supplied to the storage bin 101 in the dry storage device of the first embodiment described above. Here is an example. In the case of the dryer 302, the flange of the dryer (reference numeral 19 in FIGS. 1 and 6) is used.
, A pump (indicated by reference numeral 18 in FIGS. 1 and 6) and a heat transfer tube (indicated by 104 in FIGS. 1 and 6) are not required.

[0063]

As described above, according to the present invention, the air can be pre-cooled by the first heat exchange means before cooling in the evaporator, and the pre-cooled heat is removed from the air once cooled in the evaporator. It is possible to provide a dry storage device provided with a heat pump that can be recovered and has a high operation coefficient. Further, a dry storage device having a high dehumidifying capacity per energy consumption can be provided.

[Brief description of the drawings]

FIG. 1 is a diagram schematically showing a flow in a dry storage device according to a first embodiment of the present invention.

FIG. 2 is a diagram showing one configuration example of a dryer of the drying storage device of FIG.

FIG. 3 is an enlarged view showing a refrigerant path in a heat exchanger of the dry storage device of FIG. 1;

FIG. 4 is a refrigerant Mollier diagram of a heat pump included in the dry storage device of FIG. 1;

FIG. 5 is a psychrometric chart in the dry storage device of FIG. 1;

FIG. 6 is a diagram schematically showing a flow in a dry storage device according to a second embodiment of the present invention.

FIG. 7 is a refrigerant Mollier diagram of a heat pump included in the dry storage device of FIG. 6;

8 is a diagram showing an example of a structure of a heat exchanger of the drying storage device of FIG.

FIG. 9 is a diagram schematically showing a flow in a dry storage device according to another embodiment of the present invention.

FIG. 10 is a diagram schematically showing a flow in a conventional dry storage device.

FIG. 11 is a psychrometric chart of a conventional dry storage device.

[Explanation of symbols]

 DESCRIPTION OF SYMBOLS 1 Blower 2 Evaporator 3 Booster 4 Condenser 5, 150 Heat exchanger 10 Cabinet 11 Intake port 12 Filter 13a, 13b, 13c Air path 14 Drain pan 15 Drain tank 16 Supply port 17 Water tank 18 Pump 19 Flange 51 First Heat exchange section 52 Second heat exchange section 61 Evaporation section 62 Condensing section 63, 64 U tube 40 to 43 Path 48, 49, 163, 164 Restriction 100 Storage 101 Storage bin 102, 202 Dryer 103 Floor mesh 104 Preheating chamber 105 heat transfer tube

──────────────────────────────────────────────────続 き Continued on the front page (51) Int.Cl. ⁷ Identification symbol FI theme coat ゛ (reference) F26B 23/10 F26B 23/10 Z F term (reference) 2B100 AA02 AA07 BB05 BC01 GA04 GA12 3L053 BC02 3L113 AA01 AB02 AB06 AC16 AC22 BA18 DA02

Claims (5)

[The claims] 1. A storage bin for storing a storage object, a heat transfer tube installed in the storage bin, through which a fluid flows, a booster for boosting a refrigerant, and the heat transfer tube for condensing the refrigerant A condenser that heats the fluid inside the evaporator, an evaporator that evaporates the refrigerant and cools the external air to a temperature equal to or lower than the dew point, and is provided in a refrigerant path connecting the condenser and the evaporator, First heat exchange means for evaporating the refrigerant at an intermediate pressure between the condensing pressure of the condenser and the evaporating pressure of the evaporator to cool the external air; and in a refrigerant path connecting the condenser and the evaporator. A second heat exchange means for condensing a refrigerant at an intermediate pressure between the condensation pressure of the condenser and the evaporation pressure of the evaporator to heat external air; and the first heat exchange means The evaporator, the second heat exchange means, and the storage bin Dry storage apparatus characterized by comprising an air path connecting the order. 2. A storage bin in which a storage object is stored, a booster that pressurizes the refrigerant, a condenser that condenses the refrigerant and heats external air, and evaporates the refrigerant to lower the external air below the dew point. An evaporator for cooling to a temperature, provided in a refrigerant path connecting the condenser and the evaporator, and evaporating the refrigerant at an intermediate pressure between the condensation pressure of the condenser and the evaporation pressure of the evaporator. First heat exchange means for cooling external air, provided in a refrigerant path connecting the condenser and the evaporator, and at a pressure intermediate between the condensation pressure of the condenser and the evaporation pressure of the evaporator. A second heat exchange means for condensing a refrigerant to heat external air; a first heat exchange means, the evaporator, the second heat exchange means, the condenser, and the storage bin in this order. Drying storage device comprising an air path for connection Place. 3. The first heat exchanging means and the second heat exchanging means are configured such that air flowing through each of the heat exchanging means flows opposite to each other. Having at least a pair of first and second through-holes in a first plane substantially orthogonal to the flow of air in the heat-exchange means and the second heat-exchange means. At least one pair of the first penetrating portion and the second
3. The dry storage device according to claim 1, further comprising an intermediate throttle at a position where the intermediate throttle moves from the first plane to the second plane. 4. 4. A storage object is stored in a storage bin, a fluid is circulated in a heat transfer tube installed in the storage bin, and a refrigerant is pressurized. In a condenser, the refrigerant is condensed and the refrigerant is condensed. Heating the fluid inside the heat transfer tube, evaporating the refrigerant in the evaporator to cool the external air to a temperature below the dew point, and, in the first heat exchange means, condensing pressure of the condenser and the evaporator. The refrigerant is evaporated at an intermediate pressure with the evaporation pressure to cool the external air, and the second heat exchange means condenses the refrigerant at a pressure intermediate between the condensation pressure of the condenser and the evaporation pressure of the evaporator. The first heat exchange means, the evaporator, the second heat exchange means, and the storage bin are connected in this order by an air path, and the second heat exchange means Storing the external air heated in Supplies to the down, the internal fluid of the heat transfer tube heated in the condenser is supplied to the storage bin, a drying method of storage items, characterized in that drying the reservoir. 5. A storage object is stored in a storage bin, a refrigerant is pressurized, a condenser is condensed to heat the external air, and an evaporator evaporates the refrigerant to evaporate the external air in an evaporator. Cooling to a temperature equal to or lower than the dew point; in the first heat exchange means, evaporating the refrigerant at an intermediate pressure between the condensation pressure of the condenser and the evaporation pressure of the evaporator to cool the external air; In the exchange means, the refrigerant is condensed at an intermediate pressure between the condensation pressure of the condenser and the evaporation pressure of the evaporator to heat the external air, and the first heat exchange means, the evaporator, and the second A heat exchanger connected to the condenser in this order by an air path, supplying external air heated in the condenser to the storage bin, and drying the storage material; Drying method.