JP2000356481A - Heat exchanger, heat pump and dehumidifier - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a heat exchanger having high heat exchanging efficiency and small size for its heat exchanging quantity, a compact heat pump and a dehumidifier arranged compactly. SOLUTION: The heat exchanger comprises a first section 310 for supplying a first fluid A, a second section 320 for supplying a second fluid B, first fluid channels 251A, B, C for supplying a third fluid exchanging heat with the first fluid A flowing through the first section 310, and second fluid channels 252A, B, C for supplying a third fluid exchanging heat with the second fluid B flowing through the second section 320. The third fluid flows from the first fluid channels 251A, B, C through the second fluid channels 252A, B, C and evaporates, at a specified pressure, on the channel side heat transfer surface of the first fluid channels 251A, B, C and condensates, at a specified pressure, on the channel side heat transfer surface of the second fluid channels 252A, B, C. The third fluid condensed in the second fluid channels 252A, B, C can be supplied reversely between the first fluid channels 251A, B, C and the second fluid channels 252A, B, C.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a heat exchanger, a heat pump, and a dehumidifier, and more particularly to a heat exchanger for exchanging heat between two fluids via a third fluid, and comprising such a heat exchanger. The present invention relates to a heat pump and a dehumidifier using such a heat pump and using a desiccant.

[0002]

2. Description of the Related Art To exchange heat between a large amount of fluids having relatively small temperature differences, for example, between processing air for air conditioning and outside air for cooling, a cross-flow type heat exchanger 3 as shown in FIG. Large volume rotary heat exchangers were used. Such a heat exchanger has been used, for example, in a desiccant air-conditioning system in which process air to be introduced into a room is preliminarily cooled by outside air before being introduced into the room.

[0003]

According to the above-mentioned conventional heat exchanger, the heat cannot be sufficiently utilized because the volume is very large, the installation area is too large, and the heat exchange efficiency is poor. In addition, in a heat pump or a dehumidifier using a conventional heat exchanger, the system configuration is difficult, and as a result, the system must be increased in size.

Accordingly, an object of the present invention is to provide a heat exchanger, a heat pump, and a dehumidifier that are small in size for heat exchange, have high heat exchange efficiency, have a high COP, and are compact.

[0005]

In order to achieve the above object, a heat exchanger according to the first aspect of the present invention is, for example, shown in FIG.
As shown in FIG. 1, a first section 31 through which a first fluid A flows
0; a second section 320 through which the second fluid B flows; and a third section which passes through the first section 310 and exchanges heat with the first fluid A.
First fluid flow paths 251A, B, and C through which fluid flows;
A second fluid flow path 252A, B, C for flowing a third fluid that exchanges heat with the second fluid B, penetrating through the section 320 of the first fluid flow path. 252A, B,
C flows through the second fluid flow paths 252A, B, and C, and the third fluid evaporates at a predetermined pressure on the flow-side heat transfer surfaces of the first fluid flow paths 251A, B, and C; The third fluid is configured to condense substantially at the predetermined pressure on the channel-side heat transfer surfaces of the second fluid channels 252A, B, and C; the first fluid channels 251A, B, and C And the second fluid flow path 252A, between the second fluid flow path 252A,
The third fluid condensed by B and C is configured to flow backward.

[0006] Typically, the first fluid flow path 251A,
B and C and the second fluid flow path and 252A, B and C are configured as an integrated flow path, and the third fluid, for example, the refrigerant flows from the first fluid flow path to the second fluid flow path. All flow in one direction DR1 (FIG. 2). The backflow flows in the direction DR2, which is opposite to the direction, from the second fluid flow path to the first fluid flow path inside these flow paths. Backflow is, for example, the transport of fluid using capillary action. The backflow flows along the heat transfer surfaces of the first and second fluid flow paths, and flows along the tube wall of the tube if the fluid flow path is a tube. It is preferable that the second fluid flowing through the second compartment be configured to contain moisture.

[0007] With this configuration, the third fluid condensed in the second fluid flow path is caused to flow back between the first fluid flow path and the second fluid flow path. Therefore, the amount of heat exchange in the heat exchanger determined by the product of the latent heat of the third fluid and the flow rate increases.

Further, the second fluid passages 252A, 252B, 252C extend through the second section 320.
And a third fluid flow path 252D (FIG. 11) arranged in parallel with the second fluid B for flowing a third fluid that exchanges heat with the second fluid B. The third fluid flow path 252D has substantially the third fluid flow path 252D. The third fluid may be supplied so as to bypass the one section 310.

According to the third aspect of the present invention, in the heat exchanger of the second aspect, the first fluid flow paths 251A, B, and C are provided with:
The third fluid mainly in the liquid phase may be supplied, and the third fluid channel 252D may be supplied mainly with the third fluid in the gas phase. With this configuration, the heat transfer amounts of the first fluid passage and the second fluid passage can be made uniform.

In order to achieve the above object, a heat exchanger according to a fourth aspect of the present invention includes a first section 310 through which a first fluid A flows, as shown in FIG. B, a second section 320 for flowing B; a first fluid flow path 251A, B, C for flowing a third fluid that exchanges heat with the first fluid A, penetrating the first section 310; A second fluid flow path 252A, B, C for flowing a third fluid that exchanges heat with the second fluid B through the compartment 320; said third fluid being a first fluid flow path 251A. , B, and C flow through the second fluid flow paths 252A, B, and C, and on the flow-side heat transfer surfaces of the first fluid flow paths 251A, B, and C, the third fluid is supplied at a predetermined pressure. Evaporates and the second fluid flow paths 252A, B,
The third fluid is configured to condense substantially at the predetermined pressure on the channel-side heat transfer surface of C; the first fluid channels 251A, B, C and the second fluid channels 252A, B , C, the third fluid condensed in the second fluid flow paths 252A, B, C is configured to flow back;
A plurality of first fluid flow paths 251A, 251B, and 251C are provided, and the predetermined pressures in the plurality of fluid flow paths are different from each other. here,
It is not necessary for each of the plurality of fluid flow paths to have a different pressure, and it is sufficient that the fluid flow paths are divided into a plurality of groups, and the groups have different pressures.

[0011] To achieve the above object, a heat pump HP1 according to the invention according to claim 5 is, for example, as shown in Fig. 3, a heat exchanger 300 according to any one of claims 1 to 3. A pressurizer 260 for pressurizing the gaseous third fluid; and removing heat from the gaseous third fluid pressurized by the pressurizer 260 with a high-temperature fluid to convert the third fluid to a first pressure. A condenser 220 for condensing underneath; a condenser 22
A first throttle 230 for reducing the third fluid condensed at 0 to the predetermined pressure; a second throttle 240 for reducing the third fluid to a second pressure after condensing in the heat exchanger 330
And applying heat from the cryogenic fluid A under the second pressure to produce the second
And an evaporator configured to evaporate the third fluid depressurized by the throttle 240. Here, typically, the first pressure is a condensing pressure, the second pressure is an evaporation pressure, and the predetermined pressure is a pressure intermediate between the first and second pressures. Heat pump H
P1 pumps heat from evaporator 210 to condenser 220.

The booster is, for example, a compressor, and the pressure is increased by compressing the gas with the compressor. However, as in an absorption heat pump, a combination of an absorber that absorbs a refrigerant with an absorbing liquid, a regenerator that regenerates the absorbing liquid, and a pump that pressurizes the absorbing liquid that has absorbed the refrigerant and sends it from the absorber to the regenerator. It may be.

The heat pump HP3 according to claim 6
8, for example, as shown in FIG. 8, a heat exchanger 300c according to claim 4, a pressure booster 260 for raising the pressure of the third fluid in a gas phase, and a third pressure of the gas phase boosted by the pressure booster 260. A condenser 220 that removes heat from the fluid by a high-temperature fluid to condense the third fluid under a first pressure; and a plurality of first fluid flow paths 251A that condense the third fluid in the condenser 220. ,
A plurality of first throttles 230A, B, C for reducing the pressure to the predetermined pressure corresponding to B, C (FIG. 7); heat exchanger 300c
A second throttle 240A, B, and C for reducing the third fluid to a second pressure after being condensed in the second throttle 240A, and applying heat from the low temperature fluid A under the second pressure. An evaporator configured to evaporate the third fluid decompressed in B and C is provided. The heat pump HP3 pumps heat from the evaporator 210 to the condenser 220.

Typically, the second fluid flow path is provided as a plurality of flow paths corresponding to the plurality of first fluid flow paths,
A plurality of second throttles are provided corresponding to the plurality of second flow paths. For convenience, a plurality of second stops corresponding to the plurality of first stops are provided.

In order to achieve the above object, a dehumidifier according to the invention according to claim 7 comprises, as shown in FIG. 3, for example, a moisture adsorber 103 having a desiccant for adsorbing moisture in the processing air A; The processing air cooler 3 provided on the downstream side of the flow of the processing air A with respect to the adsorption device 103
00, the processing air A to which water has been adsorbed by the desiccant is cooled by evaporation of the refrigerant, and the evaporated refrigerant flows in the processing air cooler 300 as a whole in one direction DR1 (FIG. 2) and A processing air cooler 300 configured to be cooled and condensed by the cooling fluid B; and the condensed refrigerant liquid is processed in the processing air cooler 300 so as to be subjected to evaporation in the processing air cooler 300. It is characterized in that it is configured to flow backward (in the direction DR2) with respect to the flow in the direction DR1.

[0016] Further, as described in claim 8, claim 7
Evaporator 210 for evaporating the refrigerant condensed in the processing air cooler 300 to further cool the processing air A cooled in the processing air cooler 300;
A booster 260 that pressurizes a refrigerant that has become a gas by evaporation at 0
A condenser 220 that cools and condenses the refrigerant pressurized by the booster 260 with the regeneration air and condenses the refrigerant; and that the refrigerant condensed by the condenser 220 is supplied to the processing air cooler 300. It may be a feature.

Further, as described in claim 9 (for example, FIG.
0), in the dehumidifier of claim 8, the condenser 2
A gas-liquid separator 350 for separating the refrigerant into a refrigerant liquid and a refrigerant gas may be provided between the processing air cooler 20 and the processing air cooler 300d.

[0018]

Embodiments of the present invention will be described below with reference to the drawings. In the drawings, the same or corresponding members are denoted by the same or similar reference numerals, and duplicate description is omitted.

FIG. 1 is a sectional view of a heat exchanger according to a first embodiment of the present invention. In the figure, heat exchanger 300
Is a first section 31 through which processing air A as a first fluid flows.
0 and the second section 320 for flowing the outside air B as the second fluid.
Are provided adjacent to each other with one partition wall 301 interposed therebetween.

A coolant 250 as a third fluid penetrates the first section 310, the second section 320, and the partition 301.
A plurality of heat exchange tubes serving as fluid flow paths are provided substantially horizontally. In this heat exchange tube, a portion penetrating through the first section 310 includes an evaporating section 251 (a plurality of evaporating sections 25
1A, 251B, and 251C), and a portion penetrating the second section 320 is a condensing section 252 (a plurality of condensing sections 252
A, 252B and 252C).

In the embodiment shown in FIG. 1, the evaporating section 251A and the condensing section 252A are formed as one integrated flow path by one tube. The same applies to the evaporating sections 251B, C and the condensing sections 252B, C. Therefore, the first section 310 and the second section 310
The heat exchanger 300 can be formed small and compact as a whole, in combination with the fact that the section 320 is provided adjacently with one partition wall 301 interposed therebetween. Here, the evaporating section 251A and the condensing section 252A, which are constituted by an integral tube, typically have a plurality (251A1, A2, A3,...) In a direction perpendicular to the plane of the drawing.
Provided. The same applies to the sections 251B and 251C.

In the embodiment shown in FIG. 1, the evaporating sections are arranged in the order of 251A, 251B, and 251C from the top in the figure, and the condensing sections are 252A, 252 from the top in the figure.
B, 252C.

On the other hand, the processing air A as the first fluid is
In the figure, it is configured to enter the first section 310 from above through the duct 109 and flow out from below. Also, the second
The outside air B, which is a fluid, is configured to enter the second section 320 from below through the duct 171 in the figure and to flow out from above. That is, the processing air A and the outside air B are configured to flow in directions in which counterflows are formed with each other.

Further, in the second section 320, a sprinkling pipe 325 is disposed above the heat exchange tube constituting the condensing section 252. Nozzles 327 are attached to the watering pipe 325 at appropriate intervals, and are configured to spray water flowing in the watering pipe 325 to heat exchange tubes constituting the condensation section 252.

A vaporizing humidifier 165 is installed at the entrance of the second fluid B in the second section 320. The vaporizing humidifier 165 is made of a material that has a hygroscopic property and a gas permeability, such as a ceramic paper and a nonwoven fabric.

Here, the evaporation pressure in the evaporation section 251 and, consequently, the condensation pressure in the condensation section 252,
That is, the predetermined pressure of the present invention is determined by the temperature of the processing air A and the outside air B.
Temperature. Since the heat exchanger 300 according to the embodiment shown in FIG. 1 utilizes the evaporative heat transfer and the condensed heat transfer, the heat exchanger 300 has a very high heat transfer coefficient and a very high heat exchange efficiency. Further, since the refrigerant as the third fluid flows from the evaporating section 251 to the condensing section 252, that is, is forced to flow in substantially one direction, the heat exchange efficiency is high.

Referring to FIG. 2, one embodiment of a configuration in which the third fluid flows between the evaporating section 251 and the condensing section 252 in a direction opposite to the one direction will be described.
Here, the evaporating section 251A and the condensing section 25
2A is extracted and shown. In the figure, the evaporating section 251A and the condensing section 252A are formed as an integral tube. A wick W is lined on the inner surface of the tube wall. The wick W is typically a nonwoven or woven fabric formed of fine fibers. The fiber is
Organic fibers such as vegetable fibers such as cotton and animal fibers such as wool and silk may be used, and metal fibers and inorganic fibers such as rock wool (rock wool) may be used. It may be a wire mesh using metal fibers. In short, it is only necessary to use a fiber having a hydrophilic property (wetting property with respect to the coolant liquid) or a thin wire to cause the capillary phenomenon.

The wick W is applied particularly across the partition wall 301. For the evaporation section 251A, the partition 30
It is not necessary to apply it to the region near the entrance of the evaporating section 251A on the upstream side from 1. This is because a sufficient amount of the refrigerant liquid flows from the upstream side to the region without causing the refrigerant liquid to flow backward from the condensation section 252A.

The refrigerant flows in one direction as a whole, that is, in the direction DR from the evaporating section 251A to the condensing section 252A.
The refrigerant gas that flows to 1 and evaporates in the evaporating section 251A is condensed in the condensing section 252A. When the cooling load of the fluid to be cooled (for example, the processing air A) flowing through the first section 310 is large, the end of the evaporating section 251A, that is, in the vicinity of the partition wall 301, may become completely dry gas.

Here, when the wick W is lined as described above, the refrigerant liquid condensed in the wick W in the condensing section 252A soaks the wick W as indicated by an arrow CN, and the refrigerant liquid is introduced into the evaporating section 251A by capillary action. In the figure, since the liquid flows backward (in the direction DR2 opposite to the direction DR1), the refrigerant liquid can be secured also at the end of the evaporating section 251A, and evaporates from the wick W as indicated by the arrow EV.

In addition, instead of lining the wick W,
Fine linear grooves may be formed on the inner surfaces of the heat exchange tubes constituting the evaporating section 251 and the condensing section 252 in the longitudinal direction of the tubes. In this case, the inner surface of the tube may be further subjected to a hydrophilic treatment.

FIG. 3 is a flow chart of an air conditioning system having a dehumidifying air conditioner, that is, a desiccant air conditioner according to an embodiment of the present invention. FIG. 4 is an example of a psychrometric chart in the case of performing air conditioning with the dehumidifying air conditioner of FIG. FIG. 5 is a refrigerant Mollier diagram of the heat pump HP1 included in the air conditioner of FIG.

Referring to FIG. 3, the configuration of a dehumidifying air conditioner according to an embodiment of the present invention will be described. In this air conditioning system, the humidity of the processing air is reduced by a desiccant (drying agent), and the air-conditioned space 101 to which the processing air is supplied is maintained in a comfortable environment. In the figure, a blower 102 for circulating processing air along a path of processing air A from an air-conditioned space 101, and a desiccant rotor 10 filled with desiccant.
3. The first section 310 of the processing air cooler 300, the refrigerant evaporator (cooler as viewed from the processing air) 210, are arranged in this order, and are configured to return to the air-conditioned space 101.

A heat exchanger 121 for exchanging heat between the regeneration air before entering the desiccant rotor 103 and the subsequent regeneration air along the path of the regeneration air B from the outdoor OA, a refrigerant condenser (as viewed from the regeneration air) A heater 220, a desiccant rotor 103, a blower 140 for circulating regenerated air, and a heat exchanger 121 are arranged in this order, and are configured to exhaust EX to the outside.

The second section 320 of the processing air cooler 300 and the blower 160 for circulating the cooling fluid are arranged in this order along the path from the outdoor OA to the outside air as the cooling fluid C. The exhaust EX is configured.

A compressor 260 for increasing the pressure of the refrigerant evaporated and gasified by the refrigerant evaporator 210 along a refrigerant path from the refrigerant evaporator 210, a refrigerant condenser 220, a header 230 having a built-in throttle, and a process air cooling system. Evaporator section 251, condensing section 252, process air cooler 30
The heat pump HP <b> 1 is configured such that the headers 240 with built-in throttling, which collect pipes from the heat exchange tubes of the condensation section 252, are arranged in this order and returned to the refrigerant evaporator 210 again.

The desiccant rotor 103 is formed as a thick disk-shaped rotor that rotates around a rotation axis, and the rotor is filled with a desiccant with a gap through which gas can pass.

Since a large amount of regeneration air must be passed through the heat exchanger 121, a cross-flow type heat exchanger in which low-temperature regeneration air and high-temperature regeneration air flow orthogonally,
A rotary heat exchanger having a structure similar to the desiccant rotor 103 and filled with a heat storage material having a large heat capacity is used instead of the drying element.

Referring to FIG. 4, the flow of the refrigerant of the heat pump HP1 in the configuration of FIG. 3 and the operation of the heat exchanger 300 according to the embodiment of the present invention will be described. This figure shows the refrigerant HF
It is a Mollier diagram in case C134a is used. In this diagram, the horizontal axis is enthalpy and the vertical axis is pressure.

In the figure, the point a is the state of the refrigerant outlet of the cooler 210 in FIG. 5 and is in the state of saturated gas. Pressure is 4.2
kg / cm ² , temperature 10 ° C., enthalpy 148.
It is 83 kcal / kg. The state where the gas is sucked and compressed by the compressor 260 and the state at the discharge port of the compressor 260 are indicated by a point b. In this state, the pressure is 19.3 kg /
cm ² , the temperature is 78 ° C., and it is in a superheated gas state.

This refrigerant gas is cooled in the heater (condenser as viewed from the refrigerant side) 220 and reaches a point c on the Mollier diagram. This point is a saturated gas state, and the pressure is 19.3.
kg / cm ² and the temperature is 65 ° C. Under this pressure, it is further cooled and condensed to reach point d. This point is a saturated liquid state, the pressure and temperature are the same as point c, and the enthalpy is 122.97 kcal / kg.

This refrigerant liquid is decompressed by the throttle 230 and flows into the evaporating section 251 of the heat exchanger 300. On the Mollier diagram, it is indicated by a point e. The temperature will be about 30 ° C. The pressure is a predetermined pressure of the present invention, an intermediate value, i.e. saturation pressure corresponding to 30 ° C. and 4.2 kg / cm ² and 19.3 kg / cm ² in the present embodiment. Here, a part of the liquid is evaporated and the liquid and the gas are mixed. In the evaporating section 251, the refrigerant liquid evaporates under the predetermined pressure and reaches a point f between the saturated liquid line and the saturated gas line at the same pressure. Here, the liquid has almost completely evaporated. At the point e, the ratio between the refrigerant liquid and the gas is:
Since the saturation pressure line at 30 ° C. is the inverse ratio of the difference between the enthalpy at the point where the saturated liquid line and the saturated gas line cross, and the enthalpy at the point d,
As is clear from FIG. 4, the weight ratio of the liquid is larger. However, gas is overwhelmingly larger in volume ratio,
In the evaporating section, the liquid is mixed with a large amount of gas, and the liquid evaporates while flowing along the inner surface of the tube of the evaporating section or while immersing the wick W.

The refrigerant in the state indicated by the point f flows into the condensation section 252. In the condensing section 252, the refrigerant is deprived of heat by the outside air flowing through the second compartment 320 and / or sprayed water and reaches the point g. This point is on the saturated liquid line in the Mollier diagram. The temperature is 30 ° C. and the enthalpy is 109.99 kcal / kg.

Here, the wick W as described with reference to FIG. 2 is lined on the inner surfaces of the tubes constituting the evaporating section 251 and the condensing section 252, so that the refrigerant condensed in the condensing section 252 is subjected to capillary action. It flows back to the evaporation section 251. On the Mollier diagram,
The refrigerant liquid at point g is returned to point e. Therefore, it is possible to prevent a region where the refrigerant liquid does not exist near the boundary between the evaporating section 251 and the condensing section 252. That is, it is possible to prevent the point f from entering the superheated gas region beyond the saturated gas line on the Mollier diagram.

Further, the refrigerant liquid at point g is reduced to a saturation pressure of 4.2 kg / cm ² at a temperature of 10 ° C. by a restrictor 240 and is cooled as a mixture of the refrigerant liquid and gas at 10 ° C. (The evaporator) 210, where heat is removed from the processing air, and evaporated to become a saturated gas in the state of the point a on the Mollier diagram, sucked into the compressor 260 again, and the above cycle is repeated.

As described above, in the heat exchanger 300, the refrigerant evaporates from the point e to the point f in the evaporating section 251, and changes state from the point f to the point g in the condensing section 252. The heat transfer coefficient is very high because of the evaporation heat transfer and the condensation heat transfer. Further, since the refrigerant liquid in the state at the point g is returned to the point e via the wick W, even if the point f approaches the superheated gas region beyond the saturated gas line due to a large cooling load, this is not changed. The prevention point f can be kept in the wet gas area.

Further, as the compression heat pump HP1 including the compressor 260, the heater (refrigerant condenser) 220, the throttles 230 and 240, and the cooler (refrigerant evaporator) 210, if the heat exchanger 300 is not provided, Vessel (condenser) 22
In order to return the refrigerant in the state of the point d at 0 to the cooler (evaporator) 210 via the throttle, the cooler (evaporator) 210
Enthalpy difference available in is 148.83-122.9
7 = 25.86 kcal / kg, whereas in the embodiment of the present invention in which the heat exchanger 300 is provided, 14
8.83-109.99 = 38.84 kcal / kg, and the amount of gas circulating through the compressor for the same cooling load, and consequently the required power, can be reduced by 33%. That is, the cycle of the heat pump HP1 can be an economizer cycle.

The operation of the dehumidifying apparatus according to the embodiment of the present invention will be described with reference to FIG. 5 and the configuration as appropriate with reference to FIG. In FIG. 5, alphabet symbols D, E,
K to N and Q to X indicate the state of air in each part. This symbol corresponds to the circled alphabet in the flowchart of FIG.

First, the flow of the processing air A will be described. In FIG. 5, the processing air (state K) from the air-conditioned space 101 is:
The air is sucked by the blower 102 through the processing air path 107 and is sent to the desiccant rotor 103 through the processing air path 108. Here the desiccant rotor 103
Moisture is adsorbed by the desiccant therein to lower the absolute humidity, and the dry bulb temperature is raised by the heat of adsorption of the desiccant to reach the state L. This air is sent through processing air path 109 to a first section 310 of processing air cooler 300,
Here, the refrigerant is cooled by the refrigerant evaporated in the evaporating section 251 (FIGS. 1 and 2) while the absolute humidity is kept constant, becomes the air in the state M, and enters the cooler 210 through the path 110. Here, the air is further cooled at a constant absolute humidity to be in the state N. This air is dried and cooled, and is returned to the air-conditioned space 101 via the duct 111 as the processing air SA having an appropriate humidity and an appropriate temperature.

Next, the flow of the regeneration air B will be described. In FIG. 5, the regeneration air (state Q) from the outdoor OA is sucked through the regeneration air path 124 and sent to the heat exchanger 121. Here, heat exchange is performed with the high-temperature regenerated air to be exhausted (air in state U described later) to raise the dry-bulb temperature to become air in state R. This air is sent to a refrigerant condenser (heater as viewed from the regeneration air) 220 through a path 126, where it is heated to increase the dry-bulb temperature and become air in state T. This air is sent to the desiccant rotor 103 through the path 127, where it takes water from the desiccant in the drying element and regenerates it, thereby increasing the absolute humidity and lowering the dry bulb temperature by the desiccant moisture desorption heat. To reach the state U. This air passes through path 128
Through the blower 140 for circulating the regenerated air, and the regenerated air (the air in the state Q) before being sent to the heat exchanger 121 through the path 129 and being sent to the desiccant rotor 103 as described above. After heat exchange, the temperature of the air itself is reduced to state V, and
Exhaust EX through 0.

Next, the flow of the outside air C as the cooling fluid will be described. The outside air C (state Q) is sent from the outdoor OA to the second section 320 of the process air cooler 300 through the path 171. Here, first, moisture is absorbed by the humidifier 165,
By changing the isenthalpy and increasing the absolute humidity and lowering the dry-bulb temperature, the air becomes state D. State D is almost on the saturation line of the wet vapor diagram. This air is supplied to the second compartment 3
The cooling medium in the condensing section 252 is cooled while absorbing the water supplied by the watering pipe 325 in the inside 20. This air rises in absolute humidity and dry-bulb temperature substantially along the saturation line, becomes air in state E, and is exhausted EX through the passage 172 by the blower 160 provided in the middle of the passage 172.

Referring now to FIG. 5, the humidifier 16
5. The operation of the watering pipe 325 will be described. In the air conditioner as described above, when the amount of heat added to the regeneration air for regeneration of the desiccant of the device is ΔH, the amount of heat pumped from the processing air is Δq, and the driving energy of the compressor is Δh,
ΔH = Δq + Δh. The cooling effect ΔQ obtained as a result of the regeneration based on the heat quantity ΔH increases as the temperature of the outside air (state Q) to be heat-exchanged with the treated air (state L) after the adsorption of moisture is lower. That is, it becomes larger as ΔQ−Δq becomes larger in the figure. Therefore, spraying water on the outside air as the cooling fluid is useful for enhancing the cooling effect. In FIG. 4, points indicated as state M ′ and state N ′ are the evaporator humidifier 165.
7 schematically shows positions of a state M and a state N when the watering pipe 325 is not used.

Next, an example of a desiccant air conditioner incorporating a heat pump HP2 according to another embodiment of the present invention will be described with reference to FIG. Except that water is used as the second fluid flowing to the second section 320 of the heat exchanger 300b,
The configuration and operation of the embodiment described with reference to FIG. 3 are the same.
In the figure, the cooling tower 470 installed outdoors has a
The cooling water cooled to 0 ° C. is led to the suction port of the cooling water pump 460 through the cooling water pipe 471 connected to the bottom of the cooling tower 470, and the cooling water pipe 4 connected to the discharge port thereof.
Through 72, it is fed into the second compartment 320 of the heat exchanger 300b.

In the second section 320 of the heat exchanger 300b, the cooling water flows outside the heat exchange tubes perpendicular to the tubes, excluding a baffle provided perpendicular to the heat exchange tubes. A cooling water pipe 473 is connected to a cooling water outlet of the second section 320, and is configured to return the cooling water whose temperature has increased in the heat exchanger 300b to the cooling tower. Thus, in the embodiment of FIG.
While the refrigerant is condensed in the condensing section by the outside air, in this embodiment, the refrigerant is condensed in the condensing section by the cooling water. The refrigerant cycle of the heat pump HP2 is the same as that in FIG.

FIG. 7 is a schematic sectional view of a heat exchanger (process air cooler) according to another embodiment of the present invention. This processing air cooler 300c is different from the structure shown in FIG. 1 in that the processing air cooler 300c does not include the vaporization humidifier 165 and the spray pipe 325. The wick W is lined with the evaporating section 251 and the condensing section 252 as shown in FIG.

FIG. 8 is a flowchart of a dehumidifying air conditioner using the heat exchanger 300c of FIG. In the figure, heater 2
A throttle such as an orifice is inserted between the header 235 and the evaporating section 251 on the downstream side of the refrigerant flow 20. The restrictor is provided with a plurality of evaporation sections 251A, 251
250A, 250B, 250C for B and 251C respectively
Has been assigned. The condensing sections 252A, 252B, and 252C have respective coolers 210.
The throttles 240A, 240B, and 240C are distributed between the refrigerant and the header 245 on the upstream side of the refrigerant.

In such a structure, the processing air A is
In the first section 310, the evaporating sections are 251A, 2
51B and 251C, which flow in a direction orthogonal to the heat exchange tube so as to come into contact with each other, perform heat exchange between the refrigerant and the outside air B having an inlet temperature lower than that of the processing air.
Flow through the condensing section orthogonally to the heat exchange tubes so as to contact 252C, 252B, and 252A in this order. In such a case, the evaporating pressure (temperature) or the condensing pressure (temperature) of the refrigerant is determined for each section grouped by the throttle.
B, 251C, high to low, and in the condensing section, 252C, 252B, 252A, low to high. Paying attention to the flows of the processing air A and the outside air B, since the flow is a so-called counter flow, an extremely high heat exchange efficiency φ, for example, a heat exchange efficiency φ of 80% or more can be realized.

Here, a plurality of evaporating sections 251A,
Each evaporation pressure, which is a predetermined pressure in each of the evaporation sections 251B and 251C, is provided with an independent throttle 230 at the entrance of each evaporation section.
As a result of providing A, 230B, and 230C, different values can be taken, and the processing air flows through the first section 310 so as to contact the evaporation sections 251A, 251B, and 251C in this order, As a result of the deprivation of sensible heat, the temperature decreases from the entrance to the exit. As a result, the evaporation pressure in the evaporation sections 251A, 251B, and 251C will decrease in this order, and the evaporation temperatures will be in order.

Exactly as well, the condensing temperature is determined in section 252.
C, 252B, 252A in order from low to high, but, like the evaporator section, each condensing section has independent throttles 240A, 240B, 240C,
It can have an independent condensation pressure or temperature, where the outside air flows from the inlet to the outlet of the second compartment 320 to contact the condensing sections 252C, 252B, 252A in that order, resulting in a condensing pressure of They will be arranged in this order. Therefore, focusing on the processing air A and the outside air B, a so-called counter-flow heat exchanger is formed as described above, and high heat exchange efficiency can be achieved.

In the embodiment of FIG. 8, the outside air as the second fluid is used as the desiccant regeneration air B. In the figure, a duct 124 for introducing outside air from the outdoor OA is connected to the entrance of the second section 320. Duct 12
The outside air introduced by 4 is introduced into the second compartment 320 and as it passes through it draws heat from the refrigerant in the condensation section 252 and condenses it. Here, the condensing section 252 is configured to include sections 252C, 252B, and 252A, and the condensing temperatures are arranged from a low temperature to a high temperature in this order. Thus, outside air will exit the second compartment 320 after contacting the hottest condensing section 252A. The outlet of the second section 320 is connected to the heater 220 by a duct 126, and the outside air heated to some extent in the second section 320 is introduced into the heater 220, where it is further heated and regenerated as regenerated air. Duct 1 connecting heater 220 and desiccant rotor 103
27, and reaches the desiccant rotor 103.

In this manner, the desiccant rotor 103
The regeneration air introduced into the duct 1 heats and regenerates the desiccant, and then the duct 1 communicates with the outside air from the desiccant rotor 103.
28 and 129. A blower 140 is provided between the duct 128 and the duct 129,
Used to take in outside air and flow through the regeneration air path.

Next, the route of the refrigerant will be described. In the figure, a refrigerant gas compressed by a refrigerant compressor 260 is guided to a regenerative air heater (condenser as viewed from the refrigerant) 220 via a refrigerant gas pipe 201 connected to a discharge port of the compressor.
The temperature of the refrigerant gas compressed by the compressor 260 is increased by the heat of compression, and this heat heats the regeneration air. The refrigerant gas itself is deprived of heat and condenses.

At the refrigerant outlet of the heater 220, the refrigerant pipe 2
No. 02 is connected, and further reaches the header 235, where it is divided into a plurality (three in FIG. 8) of refrigerant systems, each of which is provided with another restrictor 230A, 230B, 230C. Each of the throttles 230A, 230B, and 230C is provided with an evaporation section 251A, 251B,
251C. Therefore, each of the evaporating sections 251A, 251B, 251C is configured to be able to evaporate at a different evaporating pressure and thus a different evaporating temperature. Each aperture 230A, 230B, 2
30C, each evaporating section 251A, 251B, 25
It is provided near the entrance of 1C. As the throttle, an orifice, an expansion valve, a capillary tube, or the like is used.

The liquid refrigerant exiting the heater (refrigerant condenser) 220 is decompressed by the throttles 230A, 230B and 230C.
It expands and some liquid refrigerant evaporates (flashes). The refrigerant in which the liquid and gas are mixed is supplied to each evaporating section 251.
At A, 251B, 251C, the liquid refrigerant flows to wet the inner wall of the evaporator section tube and evaporates, thereby cooling the process air flowing through the first section 310.

Each of the evaporation sections 251A, 251B, 2
51C and each condensing section 252A, 252B, 252
Since C is a series of tubes, the evaporated refrigerant gas (and the non-evaporated refrigerant liquid) flows through the condensing section 25.
2A, 252B, 252C, and the second section 32
Heat is deprived by the outside air flowing through zero and condenses.

Each condensing section 252A, 252B, 2
At the outlet side of 52C, there are apertures 240A, 240A, respectively.
B, 240C. Beyond that, header 24
5 is provided, and the header 245 has a refrigerant pipe 20.
3 is connected, and is configured to guide the liquid refrigerant to the cooler 210.

In such a configuration, the refrigerant liquid condensed in each condensing section 252A, 252B, 252C is:
After being decompressed and expanded at each of the throttles 240A, 240B, 240C to lower the temperature, and joined at the header 245, the cooler 21
0 and evaporates, and the process air is cooled by the heat of evaporation.

The refrigerant evaporated and gasified by the cooler (refrigerant evaporator) 210 is guided to the suction side of the refrigerant compressor 260,
The above cycle is repeated.

Referring to FIG. 9, the flow and operation of the refrigerant of heat pump HP3 in the air conditioner of FIG. 8 will be described. FIG.
FIG. 5 is a Mollier diagram when the same refrigerant HFC134a as in FIG. 4 is used.

In the figure, the point a is the state of the refrigerant outlet of the cooler 210 in FIG. 8 and is the state of the saturated gas. Pressure is 4.2
kg / cm ² , temperature 10 ° C., enthalpy 148.8
It is 3 kcal / kg. The state where this gas is sucked and compressed by the compressor 260 and the state at the discharge port of the compressor 260 are point b.
Indicated by In this state, the pressure is 19.3 kg / c
m ² , temperature is 78 ° C.

This refrigerant gas is supplied to a heater (refrigerant condenser) 2
It is cooled in 20 and reaches point c on the Mollier diagram. This point is a state of a saturated gas, and the pressure is 19.3 kg / cm.
^{2. The} temperature is 65 ° C. Under this pressure, it is further cooled and condensed to reach point d. This point is the state of the saturated liquid,
The pressure and temperature are the same as point c, the enthalpy is 122.
97 kcal / kg.

The state of the refrigerant liquid which has been decompressed by the throttle 230A and has flowed into the evaporation section 251A is indicated by a point e1 on the Mollier diagram. The temperature is about 43
° C. The pressure is one of the different second pressures of the present invention, and is a saturation pressure corresponding to a temperature of 43 ° C. Similarly,
The state of the refrigerant decompressed by the throttle 230B and flowing into the evaporating section 251B is indicated by a point e2 on the Mollier diagram, where the temperature is 40 ° C. and the pressure is another one of the different second pressures of the present invention. And a saturation pressure corresponding to a temperature of 40 ° C. Similarly, the state of the refrigerant decompressed by the throttle 230C and flowing into the evaporating section 251C is indicated by a point e3 on the Mollier diagram, the temperature is 37 ° C., and the pressure is the second pressure different from the present invention. Another one, temperature 37 ℃
Is the saturation pressure.

At any of the points e1, e2, and e3,
The refrigerant is in a state where a part of the liquid is evaporated and the liquid and the gas are mixed. In each evaporating section, the refrigerant liquid evaporates under each of the second pressures to reach points f1, f2, f3 between the saturated liquid line and the saturated gas line at each pressure.

The refrigerant in this state is supplied to each condensing section 25.
2A, 252B, and 252C. In each condensing section, the refrigerant is deprived of heat by the outside air flowing through the second section 320, and reaches points g1, g2, and g3, respectively. These points are on the saturated liquid line in the Mollier diagram. The temperatures are 43 ° C, 40 ° C and 37 ° C, respectively. Some of these refrigerant liquids flow back toward the evaporation section while immersing the wick W. That is, the process returns to points e1, e2, and e3, respectively. In addition, the remaining refrigerant liquid passes through the respective throttles, and then goes to points j1 and j, respectively.
2, j3. The pressure at these points is 4.2 kg / cm ² at a saturation pressure of 10 ° C.

Here, the refrigerant is in a state where a liquid and a gas are mixed. These refrigerants merge into one header 245, and the enthalpy here is a value obtained by averaging the points g1, g2, and g3 by weighing them with the flow rates of the respective refrigerants. In this example, about 113.51. It is. Despite having three stages, the enthalpy is higher than in the case of FIG.
This is because water is not sprayed in the second section 320.

This refrigerant is supplied to a cooler (refrigerant evaporator) 210
Takes heat from the processing air, evaporates and points a on the Mollier diagram
, And is sucked into the compressor 260 again, and the above cycle is repeated.

As described above, in the heat exchanger 300c, the refrigerant evaporates in each evaporating section and condenses in each condensing section. Since the refrigerant is an evaporative heat transfer and a condensed heat transfer, the heat transfer coefficient is lower. Very high. Moreover, the first section 310
In the figure, the processing air cooled from a high temperature to a low temperature as it flows from top to bottom in the drawing is 43 ° C. and 40 ° C., respectively.
Since the cooling is performed at the temperature sequentially arranged in the order of ° C. and 37 ° C., the heat exchange efficiency can be increased as compared with the case where the cooling is performed at one temperature, for example, 40 ° C. The same applies to the condensing section.
That is, in the second section 320, outside air (regenerated air) heated from a low temperature to a high temperature as it flows from the bottom to the top in the drawing is heated at a temperature of 37 ° C, 40 ° C, and 43 ° C, respectively. Therefore, the heat exchange efficiency can be increased as compared with the case of heating at one temperature, for example, 40 ° C.

Further, since the wick W is continuously lined from the evaporating section 251 to the condensing section 252, even when the cooling load is large, the evaporating section 25 is formed.
No. 1 does not dry, and good cooling can be performed.

Further, as a compression heat pump HP3 including a compressor 260, a heater (refrigerant condenser) 220, a throttle and a cooler (refrigerant evaporator) 210, a heat exchanger 300c
Is not provided, the refrigerant at the state of the point d in the heater (condenser) 220 is passed through the throttle to the cooler (evaporator) 21.
To return to 0, the enthalpy difference available in the cooler (evaporator) is only 25.86 kcal / kg,
In the case of the embodiment of the present invention provided with the heat exchanger 300b, 1
48.83-113.51 = 35.32 kcal / kg
Thus, the amount of gas circulating through the compressor for the same cooling load, and thus the required power, can be reduced by as much as 27%. That is, the same operation as in the case of having a normal economizer can be provided in FIG. 3 or FIG.
This is the same as the embodiment.

Referring to FIG. 10, an example of a desiccant air conditioner incorporating a heat pump HP4 according to another embodiment of the present invention will be described. FIG. 11 is a heat exchanger 300d suitable for use in the heat pump HP4, and FIG. 12 is a Mollier diagram illustrating a refrigerant cycle of the heat pump HP4.

In FIG. 10, the throttle 360 and the processing air cooler 3
00d, a gas-liquid separator 350 is provided.
The processing air path and the regeneration air path are the same as those of the air conditioner of the embodiment in FIG.

Here, the refrigerant path of the heat pump HP4 will be described. In the figure, a refrigerant gas compressed by a refrigerant compressor 260 is guided to a regenerative air heater 220 via a refrigerant gas pipe 201 connected to a discharge port of the compressor. The temperature of the refrigerant gas compressed by the compressor 260 is increased by the heat of compression, and the heat heats the regeneration air (described later).
The refrigerant gas itself is deprived of heat and condenses.

The refrigerant outlet of the heater 220 is connected to the heat exchanger 30
The refrigerant passage 202 is connected to the entrances of the 0d evaporation sections 251A, B, and C by a refrigerant path 202. A throttle 360 such as an expansion valve is provided in the middle of the refrigerant path 202. The restriction 360 and the evaporation sections 251A, B, and A gas-liquid separator 350 is provided between C and C. The configuration of the heat exchanger 300d will be described later in detail with reference to FIG.

The liquid refrigerant which has exited the heater (cooler or condenser as viewed from the refrigerant side) 220 is decompressed by an expansion valve 360 as a first throttle, expands, and a part of the liquid refrigerant evaporates (flashes). ). The refrigerant mixed with the liquid and gas is
The refrigerant liquid and the refrigerant gas are separated by the gas-liquid separator 350, and the refrigerant liquid reaches the evaporating sections 251A, B, and C, and the refrigerant evaporates in the tubes of the evaporating section to form the first section 3
The process air flowing through 10 is cooled.

Evaporation section 251 and condensation section 2
52 is a series of tubes, ie, configured as an integral flow path, so that the evaporated refrigerant gas (and the non-evaporated refrigerant liquid) flows into the condensing section 252 and into the second section 320 The heat is deprived by the outside air flowing through and the sprayed water and condensed.

The outlet side of the condensing section 252 is connected to an expansion valve 270 as a second throttle by the refrigerant liquid pipe 203.
Further, it is connected to a cooler 210 by a refrigerant pipe 204. The refrigerant liquid condensed in the condensing section 252 is decompressed and expanded by the throttle 270 to reduce the temperature, and
And evaporates, and the process air is cooled by the heat of evaporation. As the throttles 360 and 270, for example, an orifice or a capillary tube other than the expansion valve may be used.

Cooler (evaporator as viewed from refrigerant side) 210
The refrigerant evaporated and gasified by the above is guided to the suction side of the refrigerant compressor 260, and the above cycle is repeated.

The gas-liquid separator 350 includes a container into which a mixture of gas and liquid flows, and a baffle plate 355 disposed in the container so as to face the inlet of the gas-liquid mixture. I have. The gas-liquid mixture collides with the baffle plate 355 and the liquid is separated from the gas, and the gas flows out of the gas outlet provided in the vessel alongside the gas-liquid mixture inlet, and is connected to the gas outlet. Heat exchanger 300 through refrigerant pipe 340
Flow to d. The refrigerant liquid flows out from a liquid outlet provided vertically below the container of the gas-liquid separator. Refrigerant pipes 430A, 430B, and 430C are connected to the liquid outlets, and communicate with the evaporation sections 251A, 251B, and 251C, respectively.

Referring to FIG. 11, the configuration of a heat exchanger 300d according to another embodiment of the present invention suitable for use in heat pump HP4 will be described. In the figure, heat exchanger 300d
Is a first section 31 through which processing air A as a first fluid flows.
0 and the second section 320 for flowing the outside air B as the second fluid.
Are provided adjacent to each other with a single partition 301 interposed therebetween, which is similar to the heat exchanger shown in FIGS.

The arrangement of the evaporating sections 251A, B, and C, the arrangement of the condensing sections 252A, B, and C, the watering pipe 325, the evaporative humidifier 165, the processing air paths 109,
10. The arrangement of the outside air path 171 is the same as that of the heat exchanger shown in FIG.

Headers 450A, B, and C are connected to the evaporation sections 251A, B, and C, and refrigerant pipes 430A, 430B, and 43 are connected to the headers 450A, B, and C, respectively.
0C is connected. Also, each evaporating section 251
Each of A, B, and C is configured to include one or more typically two or more (six in the example of FIG. 11) heat exchange tubes, and the plurality of heat exchange tubes are connected to each header 450A, B and C.

[0092] The refrigerant gas pipe 340 is connected to the heat exchanger 300d.
Pass through the first compartment 310 via the tube 341. The tube 341 is disposed so as to penetrate the partition 301 and penetrate the second section 320. In the example of FIG. 11, two tubes 341 are arranged in parallel, and each of the tubes 341 is configured by three passes of the second section 320. Here tube 3
The part in the second compartment 320 of 41 is the condensing section 2
Similar to 52A, B and C, fins are attached to the outside of the tube to promote heat exchange. This part is called a condensation section 252D. This condensation section 2
52D is disposed upstream of the outside air flow of the condensing section 252C, between the condensing section 252C and the vaporizing humidifier 165. In the condensation section 252D, the refrigerant gas is deprived of heat by the outside air as the second fluid and condenses. The condensing section 252D may be arranged on the downstream side of the outside of the condensing section 252A.

Since the tube 341 hardly contributes to heat exchange in the first section 310, the first section 31
0 is effectively bypassed. Accordingly, the first compartment 310 may be arranged to actually be structurally bypassed, ie, pass through the exterior of the first compartment 310 and connect to the condensing section 252D in the second compartment 320.

Headers 455A, 455B, and 455C are provided on the refrigerant liquid outlet side of the condensing sections 252A, 252B, and 252C, respectively, and the condensing sections 252A, 252B, and 252C each composed of a plurality of tubes are integrated. . The piping from each header is further combined into one header 370 (FIG. 8).
03 is connected to the expansion valve 270. The refrigerant liquid from the condensing section 252D is led out by the refrigerant pipe 345 connected to the condensing section 252D, and joins the path 203 on the downstream side of the header 370. In addition, piping 3
45 may be connected to header 370.

Here, the evaporation sections 251A, 251
B, 251C, condensation sections 252A, 252B, 2
The wick W as shown in FIG. 2 is lined with 52C. The operation of Wick W is as described above. The condensing section 252D does not need to line the wick W because there is no evaporating section on the upstream side.

Next, referring to FIG. 12, heat pump HP
The operation of No. 4 will be described. FIG. 12 is a Mollier diagram when the refrigerant HFC134a is used. In this diagram, the horizontal axis is enthalpy and the vertical axis is pressure.

In FIG. 12, points a to d are the same as those in the above-described embodiment, and a description thereof will be omitted.

In the figure, the refrigerant liquid in the state at point d is
And flows into the gas-liquid separator 350 in the state indicated by the point s. Here, the separated refrigerant gas is a gas at a point of intersection h between the equal pressure line of the saturation pressure corresponding to 40 ° C., which is the intermediate pressure of the present invention, and the saturated gas line, and the piping 340
Through the tube 341. In the condensing section 252D, heat is deprived by outside air (outside air cooled by water from a vaporizing humidifier and a water sprinkling pipe) and condensed, and reaches a saturated liquid line and is typically supercooled, and is cooled. To the point i of the supercooled liquid phase.

The liquid separated by the gas-liquid separator 350 is
This is the liquid in the state of point e on the saturated liquid line. This liquid flows into the evaporating sections 251A, B, and C and evaporates to become a gas-liquid mixture in the state at the point f (or may evaporate completely to a state on a saturated gas line or even to a superheated state), and the condensing section 252A, The liquid flows into B and C and is condensed to become a liquid in a state of point g.

The liquid in the state at point i and the liquid in the state at point g are mixed in the header 370, in the refrigerant pipe 203, or in the evaporator 210. A part of the refrigerant liquid in the condensing section 252 flows backward while immersing the wick W and returns to the evaporating section. In the Mollier diagram, the refrigerant liquid at point g returns to point e and eventually returns to point s.

The refrigerant liquid that has not flowed back through the wick W flows into the header 370. The refrigerant liquid in the header 370 is decompressed by the expansion valve 270 and has a pressure of 4.2 kg / cm.
^2. It becomes a refrigerant (mixture of gas and liquid) at a temperature of 10 ° C. FIG. 12 shows that the refrigerant liquid (the state at the point i) from the condensing section 252D is not collected in the header 370,
In the middle of the pipe 345 (FIG. 2), a throttle 2 different from the throttle 270
70 '(not shown), wherein the refrigerant via the restriction 270 and the refrigerant via the restriction 270' are shown as merging (or mixing in the evaporator 210) after each restriction. ing.

As described above, when using the heat exchanger 300d and the gas-liquid separator 350 according to the embodiment of the present invention, the heat exchange tubes (heat transfer tubes) constituting the evaporation sections 251A, 251B and 251C are used. Almost no gaseous phase component is contained in the refrigerant introduced into the refrigerant. Therefore, the evaporating section 25
1A, B, and C, the amount of the refrigerant introduced into the evaporating sections 251A, B, and C is uniform, so that the cooling of the processing fluid, which is the first fluid, is uniform, and the condensing sections 252A, B, and C The amount of the refrigerant condensed in the heat transfer tube is occupied by the refrigerant evaporated in the evaporating section in 251A, B, and C. The presence of the gas phase results in non-uniform heat transfer, particularly in the condensing section containing a large amount of the gas phase, but such a problem does not occur if only the liquid phase is used. In addition, the refrigerant liquid flowing backward in the wick W becomes uniform.

Thus, the heat pipe action of each heat transfer tube (phase change of refrigerant, especially heat transfer action by evaporation and condensation)
Since the amount of heat transferred by the heat becomes uniform between the heat transfer tubes,
Uniform heat transfer can be performed in the entire heat exchanger 300d, and the inconvenience of air as the first fluid and the second fluid passing without being involved in heat transfer can be prevented. Therefore, in the dehumidifying air conditioner using the heat exchanger 300d, the heat exchange efficiency between the processing air as the first fluid and the cooling medium (outside air) or the regenerated air as the second fluid is improved and the operation reliability is improved. Improvement can be achieved. Further, since the wick W increases the amount of the refrigerant liquid evaporated in the evaporating section, the cooling capacity for cooling the processing air increases, and the heat transfer coefficient improves.

[0104]

As described above, according to the present invention, heat is exchanged by evaporation and condensation of the third fluid, so that evaporation heat and condensation heat having a high heat transfer coefficient can be utilized, and the first fluid can be used. Since the third fluid condensed in the second fluid flow path is configured to flow backward between the flow path and the second fluid flow path, the third fluid in the heat exchanger is The amount of heat exchange determined by the product of the latent heat and the flow rate increases, and it is possible to provide a heat exchanger that is small in comparison with the amount of heat exchange and has high heat exchange efficiency.

Further, according to the present invention, since the heat exchanger configured to use the evaporation heat transfer and the condensation heat transfer to reversely flow the third fluid from the condensation side to the evaporation side is provided, the COP of the COP is reduced. It is possible to provide a high-priced and compact heat pump and dehumidifier.

[Brief description of the drawings]

FIG. 1 is a schematic sectional view of a heat exchanger according to an embodiment of the present invention.

FIG. 2 is a sectional view showing a part of the heat exchanger shown in FIG.

FIG. 3 is a flowchart of a dehumidifying air conditioner according to an embodiment of the present invention.

FIG. 4 is a Mollier diagram of a heat pump used in a dehumidifying air conditioner using the heat exchanger of FIG.

FIG. 5 is a psychrometric chart for explaining the operation of the dehumidifying air conditioner of FIG. 1;

FIG. 6 is a flowchart of a dehumidifying air conditioner according to another embodiment of the present invention.

FIG. 7 is a schematic sectional view of a heat exchanger according to another embodiment of the present invention.

8 is a flowchart of a dehumidifying air conditioner according to an embodiment of the present invention using the heat exchanger of FIG.

9 is a Mollier diagram of a heat pump used in the dehumidifying air conditioner shown in FIG.

FIG. 10 is a flowchart of a dehumidifying air conditioner according to another embodiment of the present invention.

11 is a schematic sectional view of a heat exchanger suitable for use in the dehumidifying air conditioner of FIG.

FIG. 12 is a Mollier diagram of a heat pump used in the dehumidifying air conditioner shown in FIG.

FIG. 13 is a schematic perspective view of a conventional heat exchanger.

[Explanation of symbols]

101 Air conditioning space 102, 140, 160 Blower 103 Desiccant rotor 121 Heat exchanger 165 Vaporization humidifier 210 Refrigerant evaporator 220 Refrigerant condenser 230 Restricted internal header 230A, 230B, 230C Restrictor 240 Restricted internal header 240A, 240B, 240C Restrictor 251A, 251B, 251C Evaporation section 252A, 252B, 252C, 252D Condensing section 260 Compressor 270, 360 Restrictor 300, 300b, 300c, 300d Process air cooler 310 First section 320 Second section 325 Sprinkling pipe 350 Gas-liquid separator 370 Header DR1, DR2 Flow direction HP1, HP2, HP3, HP4 Heat pump W Wick

Claims (9)

[Claims] A first section for flowing a first fluid; a second section for flowing a second fluid; penetrating through the first section;
A first fluid flow path through which a third fluid that exchanges heat with the first fluid flows; a second fluid flow through which the third fluid that exchanges heat with the second fluid passes through the second compartment A fluid flow path; wherein the third fluid flows from the first fluid flow path through the second fluid flow path, and the third fluid flows on a flow-side heat transfer surface of the first fluid flow path. The third fluid evaporates at a predetermined pressure,
The third fluid is configured to condense substantially at the predetermined pressure on the channel-side heat transfer surface of the second fluid channel; the first fluid channel and the second fluid channel And the third fluid condensed in the second fluid flow path can be made to flow back between
Heat exchanger. 2. A third fluid flow path penetrating through the second compartment and arranged in parallel with the second fluid flow path and flowing a third fluid that exchanges heat with the second fluid. And a third fluid flow path substantially bypassing the first compartment in the third fluid flow path.
The heat exchanger according to claim 1, wherein the heat exchanger is configured to be supplied with the fluid. 3. The first fluid flow path is supplied with a liquid-phase third fluid, and the third fluid flow path is supplied with a gas-phase third fluid. The heat exchanger according to claim 2, wherein the heat exchanger is configured. A first compartment for flowing a first fluid; a second compartment for flowing a second fluid; penetrating through the first compartment;
A first fluid flow path through which a third fluid that exchanges heat with the first fluid flows; a second fluid flow through which the third fluid that exchanges heat with the second fluid passes through the second compartment A fluid flow path; wherein the third fluid flows from the first fluid flow path through the second fluid flow path, and the third fluid flows on a flow-side heat transfer surface of the first fluid flow path. The third fluid evaporates at a predetermined pressure,
The third fluid is configured to condense substantially at the predetermined pressure on the channel-side heat transfer surface of the second fluid channel; the first fluid channel and the second fluid channel And the third fluid condensed in the second fluid flow path is configured to flow back; a plurality of the first fluid flow paths are provided; The heat exchanger, wherein the predetermined pressures are different from each other. 5. The heat exchanger according to claim 1, a booster for increasing the pressure of the third fluid in a gaseous phase, and a vaporizer for pressurizing the third fluid in the gaseous phase. A condenser for removing heat from the third fluid by the high-temperature fluid to condense the third fluid under a first pressure; and a first pressure reducing the third fluid condensed in the condenser to the predetermined pressure. A second throttle for reducing the third fluid to a second pressure after being condensed in the heat exchanger; and applying heat from the low-temperature fluid under the second pressure to produce the second fluid. An evaporator configured to evaporate the third fluid depressurized by the throttle; heat pump. 6. A heat exchanger according to claim 4, a pressure booster for pressurizing the gaseous third fluid, and heat generated by the high temperature fluid from the gaseous third fluid pressurized by the pressure booster. And a condenser for condensing the third fluid under a first pressure; and converting the third fluid condensed in the condenser to the predetermined pressure corresponding to the plurality of first fluid flow paths. A plurality of first throttles for reducing the pressure; a second throttle for reducing the third fluid to a second pressure after being condensed in the heat exchanger; and A heat pump comprising: an evaporator configured to evaporate a third fluid provided and depressurized by the second throttle; 7. A process air cooler provided downstream of the flow of process air with respect to the process device, wherein the desiccant has a desiccant for adsorbing water in the process air. The processing air to which the moisture is adsorbed is cooled by evaporation of a refrigerant, and the evaporated refrigerant is flowed in one direction as a whole in the processing air cooler, and cooled and condensed by a cooling fluid on the downstream side. A process air cooler, wherein the condensed refrigerant liquid is configured to flow backward in the process air cooler with respect to the one-way flow so as to be subjected to evaporation in the process air cooler. Features; dehumidifier. 8. An evaporator for evaporating the refrigerant condensed by the processing air cooler and further cooling the processing air cooled by the processing air cooler; a refrigerant evaporated to a gas by the refrigerant evaporator A condenser for cooling the refrigerant pressurized by the booster with regeneration air to condense the refrigerant; and supplying the refrigerant condensed in the condenser to the processing air cooler. The dehumidifying device according to claim 7, wherein: 9. The dehumidifier according to claim 8, further comprising a gas-liquid separator for separating the refrigerant into a refrigerant liquid and a refrigerant gas between the condenser and the processing air cooler. .