JP2000337660A - Dehumidifying device and dehumidifying method - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a compact dehumidifying device, high in a COP, and a dehumidifying method. SOLUTION: A dehumidifying device is provided with a moisture adsorbing device 103 having a desiccant for adsorbing moisture in treating air, a treating air cooler 300d provided at the downstream side of the flow of the treating air of the moisture adsorbing device 103 and constituted so as to cool the treating air, whose moisture is adsorbed by the desiccant, by the evaporation of refrigerant to conduct the evaporated refrigerant to flow into one direction as a whole in a treating cooler 300d and condense the same by cooling fluid at the downstream side of the cooler and a refrigerant solution returning device 380 for returning the condensed refrigerant solution to the upstream side of the flow of one direction with respect to the treating air cooler 300d to evaporate the same in the treating air cooler 300d. Evaporation and condensation in the treating air cooler are effected at the substantially same pressure. The refrigerant solution returning device is a refrigerant solution pump or an ejector, for example. The refrigerant solution returning device for returning the condensed refrigerant solution is equipped whereby a heat transfer rate at the refrigerant side in the treating air cooler is increased remarkably.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

The present invention relates to a dehumidifying apparatus and a dehumidifying method, and more particularly to a dehumidifying apparatus and a dehumidifying method using a desiccant.

[0002]

2. Description of the Related Art As shown in FIG. 8, there has conventionally been an air conditioning system in which a heat pump as a heat source is combined with a so-called desiccant air conditioner. In the air conditioning system of FIG. 8, a compression heat pump HP using a compressor 260 is used as a heat pump.
Is used. This air conditioning system desorbs and regenerates moisture in the desiccant by passing through the path of the processing air A to which moisture is adsorbed by the desiccant rotor 103 and passing through the desiccant rotor 103 after being heated by the heating source and adsorbing the moisture. A sensible heat exchanger having a path for the regeneration air B, between the treated air to which moisture has been adsorbed and the regeneration air before regenerating the desiccant (desiccant) of the desiccant rotor 103 and before being heated by the heating source. An air conditioner having an air conditioner 104 and a compression heat pump HP, and using regeneration air of the air conditioner as a high heat source of the compression heat pump HP;
That is, the regenerated air is heated by the heater 220 to regenerate the desiccant with the heated regenerated air, and the processing air of the air conditioner is used as a low heat source of the compression heat pump HP. It cools down.

In this air conditioning system, the compression heat pump HP is configured to simultaneously cool the processing air of the desiccant air conditioner and heat the regenerated air. Also,
Heat exchanger 1 between regenerated air between sensible heat exchanger 104 and heater 220 and regenerated air exiting desiccant rotor 103
21 are provided to save energy.

Here, referring to the Mollier diagram of FIG. 9, FIG.
The operation of the compression heat pump HP shown in FIG. FIG. 9 is a Mollier diagram of the refrigerant HFC134a.
Point a indicates the state of the refrigerant evaporated in the cooler 210, and is in the state of a saturated gas. The pressure is 4.2 kg / cm ² , the temperature is 10 ° C., and the enthalpy is 148.83 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 the state is a superheated gas. This refrigerant gas is cooled in the heater (cooler or condenser as viewed from the refrigerant side) 220 and reaches a point c on the Mollier diagram. This point is a saturated gas state, the pressure is 19.3 kg / cm ² , and the temperature is 65 ° C. Under this pressure, it is further cooled and condensed,
The point d is reached. This point is a state of the saturated liquid, and the pressure and the temperature are the same as those of the point c. And the enthalpy is 122.97
kcal / kg. This refrigerant liquid is decompressed by the expansion valve 270 and has a saturation pressure of 4.2 kg / c at a temperature of 10 ° C.
The pressure is reduced to m ^2, and reaches a cooler (evaporator from the viewpoint of refrigerant) 210 as a mixture of a refrigerant liquid and a gas at 10 ° C., where heat is removed from the processing air and evaporated to a point a on the Mollier diagram.
, And is sucked into the compressor 260 again, and the above cycle is repeated.

[0005]

According to the conventional air conditioning system described above, the sensible heat exchanger 104, which preliminarily cools the processing air before cooling it with the cooler 210, plays an important role. However, since the sensible heat exchanger generally occupies a large volume in the system, it has made the system configuration difficult and, as a result, the system has to be enlarged.
Further, even when the sensible heat exchanger 104 was used, the refrigerating effect of the refrigerant was not always high, and as a result, the COP of the dehumidifier was not necessarily high.

Accordingly, an object of the present invention is to provide a compact dehumidifier having a high COP.

[0007]

Means for Solving the Problems In order to achieve the above object, a dehumidifying apparatus according to the first aspect of the present invention, as shown in FIG. 1, for example, has a moisture adsorption having a desiccant that adsorbs moisture in processing air. A heat pump HP1 that operates using the processing air as a low heat source and the regeneration air for regenerating the desiccant as a high heat source; the heat pump HP1 includes an evaporator 210 that evaporates a refrigerant with the processing air; A condenser 220 for condensing the refrigerant with air, and a throttle 3 for reducing the pressure of the refrigerant condensed by the condenser 220 in a refrigerant path from the condenser 220 to the evaporator 210.
60, a processing air cooler 300d is provided through the first processing air cooler 60. The processing air cooler 300d is configured to place the processing air A and the cooling medium C in a heat exchange relationship, and the processing air cooler 300d is At a pressure intermediate the refrigerant evaporating pressure in the evaporator 210 and the refrigerant condensing pressure in the condenser 220, heat is taken from the processing air after passing through the desiccant and before reaching the evaporator 210 to evaporate the refrigerant and heat the cooling medium C. Thus, the refrigerant is condensed, and the heat pump HP1 further includes an increasing means for relatively increasing the amount of the refrigerant passing through the processing air cooler 300d.

Here, the cooling medium may be regeneration air B. The amount required to form a heat pump cycle is typically the amount condensed in condenser 220 or the amount evaporated in evaporator 210. However, when the gas-liquid separator 350 is provided on the upstream side of the refrigerant of the processing air cooler 300d, the amount of the liquid separated there corresponds to the amount necessary for forming a heat pump cycle.

The increasing means for relatively increasing the refrigerant amount is, for example, an increasing means which is larger than the amount necessary for forming a cycle of the heat pump HP1. The increasing means is, for example, a refrigerant liquid return device, and more specifically, is, for example, a refrigerant liquid pump or an ejector that uses the condensation pressure of a condenser.

The provision of the increasing means increases the cooling capacity of the processing air cooler in the processing air cooler, which is determined by the product of the latent heat and the amount of the refrigerant. Further, the heat transfer coefficient on the refrigerant side in the processing air cooler also increases.

According to a second aspect of the present invention, in the dehumidifier of the first aspect, the processing air cooler 300d includes an evaporating section 251 for removing heat from the processing air to evaporate a refrigerant; and the cooling medium. Condensing section 252 for condensing the refrigerant by heating the cooling means;
80 may be configured to circulate the refrigerant between the evaporating section 251 and the condensing section 252.

In order to achieve the above object, a dehumidifier according to a third aspect of the present invention comprises, as shown in FIG. 1, for example, a moisture adsorber 103 having a desiccant for adsorbing moisture in treated air; A processing air cooler 3 provided downstream of the processing air flow with respect to the device 103;
00d, the processing air to which water has been adsorbed by the desiccant is cooled by evaporating a refrigerant, and the evaporated refrigerant flows in the processing air cooler as a whole in one direction and is cooled by a cooling fluid on the downstream side. A process air cooler 300d configured to condense and condense; an upstream side of the one-way flow with respect to the process air cooler 300d so as to provide the condensed refrigerant liquid for evaporation in the process air cooler 300d. And a refrigerant liquid return device 380 for returning to Typically, the evaporation and condensation of the refrigerant in the processing air cooler 300d are performed under substantially the same pressure.

[0013] With this configuration, a refrigerant liquid return device is provided for returning the condensed refrigerant liquid to the upstream side of the one-way flow with respect to the processing air cooler so as to be used for evaporation in the processing air cooler. Since the circulation amount of the refrigerant passing through the processing air cooler increases, the cooling capacity of the processing air determined by the product of the latent heat and the refrigerant circulation amount increases. Further, the heat transfer coefficient on the refrigerant side in the processing air cooler also increases. The refrigerant liquid return device is, for example, a refrigerant liquid pump or an ejector that uses the condensation pressure of a condenser. Here, the evaporated refrigerant flows in one direction as a whole in the processing air cooler, and is cooled and condensed by the cooling fluid on the downstream side. The part to be evaporated and the part to be condensed are typically one body. However, the present invention is not limited to this, and a configuration may be adopted in which each of the tubes is formed of a separate tube and both are connected by piping.

According to a fourth aspect of the present invention, in the dehumidifier according to the third aspect, the refrigerant condensed in the processing air cooler is evaporated to further cool the processing air cooled by the processing air cooler. Refrigerant evaporator 210; a booster 260 for increasing the pressure of the refrigerant evaporated and gasified by the refrigerant evaporator 210; and a condenser 220 for cooling and condensing the refrigerant pressurized by the booster 260 with regeneration air. Equipped; condenser 2
The refrigerant condensed at 20 may be supplied to the processing air cooler 300d. Typically, a throttle 270 for reducing the refrigerant pressure is provided between the processing air cooler 300d and the refrigerant evaporator 210.

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.

In the present invention, typically, the refrigerant condensed in the processing air cooler 300d is decompressed and the refrigerant is evaporated.
And evaporated under the reduced first pressure.
The pressure of the refrigerant is increased to a second pressure by the booster 260, and the refrigerant condensed under the second pressure by the condenser 220 is reduced in pressure and sent to the processing air cooler 300d, where the same pressure (first and second pressures) is applied. Evaporation and condensation are performed at a pressure intermediate between these pressures).
Also, typically, the cooling medium is cooled by a condenser, and the regenerated air heated by itself is configured to flow to the moisture adsorption device, and is used to regenerate the desiccant of the moisture adsorption device.

According to a fifth aspect of the present invention, in the dehumidifier according to the fourth aspect, the condenser 220 and the processing air cooler 3 are provided.
00d, a gas-liquid separator 350 for separating the refrigerant into a refrigerant liquid and a refrigerant gas may be provided. Typically, a throttle 360 for reducing the pressure of the refrigerant is provided between the condenser 220 and the gas-liquid separator 350.

With this configuration, since the gas-liquid separator is provided, the refrigerant flowing into the processing air cooler for cooling the processing air by evaporation can be mainly composed of the liquid phase, and is condensed by the cooling fluid. It is possible to make the gaseous phase component of the refrigerant to be uniform.

In order to achieve the above object, a method for dehumidifying treated air according to the invention according to claim 6 comprises a first step of adsorbing moisture in the treated air by desiccant; evaporating the refrigerant liquid at a predetermined pressure. A second step of cooling the processing air to which moisture has been adsorbed in the first step; and a third step of condensing the refrigerant evaporated at the predetermined pressure at substantially the same pressure as the predetermined pressure. And a fourth step of providing the refrigerant condensed in the third step to evaporate in the second step. In a typical fourth step, the refrigerant liquid condensed in the third step is subjected to evaporation in the second step without passing through other steps such as evaporation and condensation before being evaporated in the second step. For this purpose, it is sent directly to the second step by a refrigerant liquid pump or the like.

In this method, in the first step, moisture is adsorbed using a desiccant to adsorb (remove) water in the processing air; and the processing air is further reduced to a first pressure lower than the predetermined pressure. A fifth step of cooling with a refrigerant evaporating at a pressure; a sixth step of increasing the pressure of the refrigerant evaporated at the fifth step to a second pressure higher than the predetermined pressure; and condensing at a second pressure. A seventh step of heating the regenerated air for regenerating the desiccant adsorbing the moisture with the refrigerant to be cooled;
And an eighth step of regenerating the desiccant by desorbing moisture from the desiccant adsorbing the moisture with the regeneration air heated in the step. Typically, the refrigerant condensed in the third step is also provided for evaporating in the fifth step. The refrigerant condensed at the second pressure in the seventh step is provided as a refrigerant to be evaporated in the second step.

With this configuration, for example, the first pressure is set to the refrigerant evaporation pressure corresponding to the temperature of the processing air suitable for supplying to the air-conditioned space 101, and the second pressure is set to the regeneration temperature of the regeneration air. The so-called economizer cycle can be used by setting the intermediate pressure to a pressure corresponding to the atmospheric temperature as the refrigerant condensing pressure, so that the refrigerating effect of the refrigerant can be remarkably increased, and thus the processing air with a high COP can be obtained. Can be dehumidified. Further, the refrigerant is evaporated at a predetermined pressure, that is, an intermediate pressure between the first and second pressures, to cool the processing air, to condense the refrigerant at substantially the same pressure as the intermediate pressure, and to evaporate the condensed refrigerant again. Process, the process air can be cooled with a high heat transfer coefficient, and a high CO
With P, it is possible to provide a method for dehumidifying process air.

Further, in the above dehumidifying air conditioner,
Using air as the cooling fluid, the processing air cooler 300
When the refrigerant is condensed in d, liquid moisture may be supplied together with the air, and in this case, the temperature of air as a cooling fluid decreases due to heat of vaporization due to evaporation of the liquid moisture. , The cooling effect increases.

[0023]

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 flowchart 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. 2 is a flowchart showing a process air cooler of the present invention used in the air conditioning system of FIG. FIG. 3 is a schematic sectional view showing an example of a heat exchanger, and FIG. 3 is a schematic sectional view showing another example of a heat exchanger that can be used in the dehumidifying air conditioner of FIG. 1 in place of the heat exchanger of FIG. 4 is an example of a psychrometric chart when air conditioning is performed by the dehumidifying air conditioner of FIG. 1, and FIG. 5 is a refrigerant Mollier chart of the heat pump HP1 included in the air conditioner of FIG.

Referring to FIG. 1, the structure of the dehumidifying air conditioner according to the first embodiment will be described. This air conditioning system
The desiccant (desiccant) reduces the humidity of the treated air,
This is to maintain the air-conditioned space 101 to which the processing air is supplied in a comfortable environment. In the drawing, a blower 1 for circulating the processing air along the path of the processing air A from the air-conditioned space 101
02, desiccant rotor 103 filled with desiccant
The processing air cooler 300d and 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 a path from the outdoor OA to the regeneration air B, 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.

A processing air cooler 300d and a blower 160 for circulating the cooling fluid are arranged in this order along a path from the outdoor OA to the outside air as the cooling fluid C,
And it is comprised so that exhaust EX may be carried out outdoors.

A compressor 260, a refrigerant condenser 220, a throttle 360, which compresses the refrigerant evaporated and gasified in the refrigerant evaporator 210 along a refrigerant path from the refrigerant evaporator 210.
The gas-liquid separator 350, the processing air cooler 300d, the header 370 that collects the pipes from the heat exchange tubes of the processing air cooler 300d, and the throttle 270 are arranged in this order, and returned to the refrigerant evaporator 210 again. , A heat pump HP1.

In this embodiment, the gas-liquid separator 350
Also serves as a header for collecting pipes to the heat exchange tubes of the processing air cooler 300d. A refrigerant pipe 385 connecting the header 370 and the gas-liquid separator 350
Is laid, and in the middle of the refrigerant pipe 385, the refrigerant liquid pump 380 sends the refrigerant liquid from the header 370 to the gas-liquid separator 350.
It is set up to be sent back to.

The desiccant rotor 103 is formed as a thick disk-shaped rotor that rotates around the rotation axis AX, 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.

Next, referring to FIG. 2, heat pump HP1
The configuration of a heat exchanger suitable for use in the present invention will be described. In the figure, a heat exchanger 300d is provided in a first section 310 through which the processing air A flows.
And a second section 320 for flowing outside air as a cooling fluid,
They are provided adjacent to each other with one partition 301 interposed therebetween.

A plurality of heat exchange tubes as a fluid flow path through which the refrigerant flows are provided substantially horizontally through the first section 310, the second section 320, and the partition wall 301. Among the heat exchange tubes, 251A, B, C, 252A, B, and C in the figure including an evaporating section and a condensing section will be described first (refrigerant gas pipe 340, tube 341, condensing section indicated by arrow YY). 252D will be described separately later).

In this heat exchange tube, a portion penetrating through the first section includes an evaporating section 251 (a plurality of evaporating sections 251A, 251B, and 251C along a flow of processing air) serving as a first fluid flow path. In the following, when it is not necessary to discuss a plurality of evaporation sections individually, only 25
1), and the portion penetrating the second section is a condensing section 252 (a plurality of condensing sections 252A, 25A along the flow of the cooling fluid) as a second fluid flow path.
2B and 252C. Hereinafter, when it is not necessary to discuss a plurality of condensation sections individually, it is simply referred to as 252).

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
A, B, and C are each one or more, typically a plurality of (six in the example of FIG. 2) heat exchange tubes in a direction perpendicular to the flow of the processing air, as indicated by arrows XX. , And the plurality of heat exchange tubes are grouped in each of the headers 450A, 450B, and 450C.

In the form of the heat exchanger shown in FIG. 2, each of the heat exchange tubes of the evaporating section 251A and the corresponding heat exchange tube of the condensing section 252A are formed as a single tube as an integrated flow path. . The same applies to the evaporating sections 251B, C and the condensing sections 252B, C. Therefore, in combination with the fact that the first section 310 and the second section 320 are provided adjacent to each other via one partition 301, the heat exchanger 300d can be formed as a small and compact as a whole. .

In the form of the heat exchanger of FIG. 2, the evaporating sections are arranged in the order of 251A, 251B, and 251C from the top in the figure, and the condensing sections are also 252A, 252A, and 252A from the top in the figure.
52B and 252C.

On the other hand, the processing air A is configured to enter the first section in FIG. The outside air, which is a cooling fluid, is configured to enter the second section in the drawing through the duct 171 from below and flow out from above.

Further, in the second section, the upper part thereof, above the heat exchange tube constituting the condensing section 252,
A watering pipe 325 is arranged. Watering pipe 325
Are provided with nozzles 327 at appropriate intervals to condense the water flowing in the watering pipe 325 to the condensing section 2.
It is configured to be sprayed on the heat exchange tube constituting 52 or in the air flowing around the heat exchange tube.

Further, a vaporizing humidifier 165 is installed at the inlet of the cooling fluid as the second fluid in the second section.
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 intermediate pressure in the present invention is determined by the temperature of the processing air A and the temperature of the outside air as the cooling fluid or its wet bulb temperature. Since the heat exchanger 300d shown in FIG. 2 utilizes the evaporative heat transfer and the condensed heat transfer, the heat exchanger has a very high heat transfer coefficient and a very high heat exchange efficiency. Further, since the refrigerant 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 between the processing air and the outside air as the cooling fluid is high.

The refrigerant pump 380 is connected to the evaporating section 25.
1 and the flow rate of the refrigerant liquid flowing through the condensing section 252 is increased, so that the cooling capacity is increased and the refrigerant flow rate is increased,
The heat transfer coefficient between the refrigerant and the heat exchange tubes constituting each section is increased.

Here, the heat exchange efficiency φ is defined as TP1, the inlet temperature of the heat exchanger of the fluid on the high temperature side, TP2, the inlet temperature of the heat exchanger of the fluid on the low temperature side is TC1, and the outlet temperature is TC2. When attention is paid to the cooling of the fluid on the high temperature side, that is, when the purpose of the heat exchange is cooling, φ = (TP1-
TP2) / (TP1-TC1), when attention is paid to heating of a low-temperature fluid, that is, when the purpose of heat exchange is heating, φ =
It is defined as (TC2-TC1) / (TP1-TC1).

Evaporation section 251, condensation section 2
It is preferable to form a high-performance heat transfer surface by forming a spiral groove such as a linear groove on the inner surface of the barrel of the rifle gun on the inner surface of the heat exchange tube constituting 52. The refrigerant liquid flowing inside usually flows so as to wet the inner surface,
When the spiral groove is formed, the heat transfer coefficient is increased because the boundary layer of the flow is disturbed.

Although the processing air flows through the first section, it is preferable that the fin attached to the outside of the heat exchange tube be processed into a louver shape to disturb the flow of the fluid. Preferably, the fins are similarly configured to disrupt the flow of fluid when the outside air flows into the second compartment but does not spray water. However, when water is sprayed, it is preferable to further provide a corrosion-resistant coating as flat plate fins. This is to prevent corrosive substances possibly mixed in the water from condensing and condensing by evaporation to corrode the fins or tubes. The fins are preferably made of aluminum, copper, or an alloy thereof.

Next, the system of the refrigerant gas pipe 340 will be described. The refrigerant gas separated by the gas-liquid separator 350 flows through the refrigerant gas pipe 340. The refrigerant gas pipe 340 passes through the first section 310 of the heat exchanger 300d via the tube 341. The tube 341 is disposed so as to penetrate the partition 301 and further penetrate the second section 320. In the example of FIG. 8, two tubes 341 are arranged in parallel, and each of the tubes 341 is configured by three passes of the second section 320. Here, the portion inside the second section 320 of the tube 341 has a structure in which fins are attached to the outside of the tube to promote heat exchange, similarly to the condensation sections 252A, 252B, and 252C. This part is called a condensation section 252D.
The condensing section 252D is connected to the condensing section 252.
The upstream side of the outside air flow of C is disposed between the condensation section 252C and the vaporization 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 air of the condensation section 252A.

Since the tube 341 hardly contributes to heat exchange in the first section, it effectively bypasses the first section 310. Thus, the first section 310 is actually structurally bypassed, ie, the first section 310
Of the condensing section 252D in the second compartment
May be arranged so as to be connected.

Headers 455A, 455B, and 455C are provided on the refrigerant liquid outlet side of the condensation sections 252A, 252B, and 252C, respectively, and the condenser 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. 1), and the header 370 is connected to the refrigerant piping 2 as described above.
03 is connected to the expansion valve 270. The refrigerant liquid from the condensing section 252D is
And connected to the path 203 downstream of the header 370, or, like the other condensing sections 252A, B, C, the pipe 345 is connected to the header 370. (FIG. 1 shows the case where the pipe 345 is connected to the header 370).

Next, referring to FIG. 3, heat pump HP1
The configuration of another heat exchanger suitable for use in the present invention will be described. In the figure, the heat exchanger 300 does not include the tube 341 and the condensing section 252D connected thereto unlike the heat exchanger 300d. Therefore, the gas-liquid separator 350 and the refrigerant gas pipe 340 are also unnecessary. Instead of the gas-liquid separator 350, similarly to the header 370, the evaporation section 251
A header 350 'is provided for collecting pipes to A, B, and C. The header 350 'can be considered as a container portion without the collision plate 355 in the gas-liquid separator shown in FIG.

The other parts are the same as those in FIG. 1 and will not be described again. The refrigerant pipe 385 connects the header 370 and a header 350 ′ provided instead of the gas-liquid separator 350, and a refrigerant liquid pump 380 is provided in the middle of the header 370, as shown in FIG. Same as the form.

When the heat exchanger 300 shown in FIG. 3 is used as a processing air cooler, the refrigerant decompressed by the throttle 360 flows into the evaporating section 251 in a gas-liquid mixed state in which a part thereof is vaporized (flashed). Further, the refrigerant liquid evaporates, and the evaporated refrigerant and the previously flushed refrigerant gas are condensed in the condensing section 252. The condensed refrigerant liquid collects in the header 370, is returned to the header 350 'by the refrigerant pump 380, and flows again into the evaporating section 251 together with the gas-liquid mixed refrigerant. Since the amount of the liquid refrigerant flowing through the evaporating section 251 and the condensing section 252 increases, the cooling capacity increases and the heat transfer coefficient increases, as in the case of the processing air cooler 300d. When using the processing air cooler 300, compared with the case of the processing air cooler 300d,
The device becomes simple.

The operation of the first embodiment will be described with reference to FIG. 4 and the configuration as appropriate with reference to FIG.
In FIG. 4, the state of air in each part is indicated by alphabetic symbols D, E, K to N, and Q to X. This symbol corresponds to the circled alphabet in the flow diagram of FIG.

First, the flow of the processing air A will be described. In FIG. 4, 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 to the first section 310 of the process air cooler 300 (or 300d) through the process air path 109, where the refrigerant evaporates in the evaporator section 251 (FIGS. 2 and 3) at a constant absolute humidity. The air becomes cooled 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. 4, 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. Outside air C (state Q) is passed from the outdoor OA to the second air of the process air cooler 300 (or
Is sent to the section 320. Here, first, the humidifier 16
5 absorbs moisture, changes isenthalpy, raises the absolute humidity, and lowers the dry-bulb temperature. State D is almost on the saturation line of the wet vapor diagram. This air is further distributed in the second compartment 320 by the watering pipe 325.
Cools the refrigerant in the condensing section 252 while absorbing the water supplied by 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. 4, the humidifier 16
5. The operation of the watering pipe 325 will be described. In the air conditioner as described above, as shown in the cycle on the air side shown in the psychrometric chart of FIG. 4, the amount of heat added to the regeneration air for regeneration of the desiccant of the device is pumped from the processing air by ΔH. Assuming that the heat amount 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 ′ conceptually show the positions of state M and state N, respectively, when the vaporizing humidifier 165 and the sprinkling pipe 325 are not used.

Next, the flow of the refrigerant between the devices will be described first with reference to FIG. 1, and then the operation of the heat pump HP1 will be described with reference to FIG.

In FIG. 1, a refrigerant gas compressed by a refrigerant compressor 260 is guided to a regenerative air heater (refrigerant condenser) 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.

The refrigerant outlet of the refrigerant condenser 220 is connected by a refrigerant path 202 to a throttle 360 provided upstream of the inlet of the evaporating section 251 of the processing air cooler 300d (or 300), which is a heat exchanger. .

The pressure is reduced by the throttle 360 and a part of the liquid refrigerant is flushed. The gas-liquid mixed refrigerant flows into the gas-liquid separator 350, where it is separated into refrigerant liquid and refrigerant gas. The separated refrigerant liquid reaches the evaporating section 251 and evaporates in the tubes of this section to cool the process air flowing through the first section.

The refrigerant evaporated in the evaporation section 251 is:
The refrigerant gas (or the non-evaporated refrigerant liquid) flows into the evaporating section 251 and the condensing section 252 formed as a series of tubes, and is deprived of heat by the outside air and sprayed water flowing through the second section and condensed. I do.

The outlet side of the condensing section 252 is connected to headers 455A, B, and C (FIG. 2), which are assembled by piping and further into a header 370 (FIG. 1). A part of the refrigerant liquid collected in the header 370 is returned to the gas-liquid separator 350 by the refrigerant liquid pump 380, mixed with the separated refrigerant liquid, and flows again into the evaporation section 251 and the condensation section 252.

Another part of the refrigerant liquid collected in the header 370 is supplied to the expansion valve 270 as a second throttle by the refrigerant liquid pipe 203 and further to the evaporator 210 by the refrigerant pipe 204.
It is connected to the. The refrigerant liquid condensed in the condensing section 252 is decompressed by the throttle 270 and expanded to lower the temperature,
The evaporator 210 enters the evaporator 210 and evaporates. As the throttles 360 and 270, for example, an orifice or a capillary tube other than the expansion valve may be used.

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 evaporating sections 251A, 251B, and 251C via headers 450A, 450B, and 450C, respectively.

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

When the processing air cooler 300 is used, the gas-liquid separator 350 is unnecessary, and since there is no condensing section 252D for inflowing and condensing the refrigerant gas, a part of the refrigerant liquid is condensed by the throttle 360. The flashed gas-liquid mixture flows into the evaporating section 251 and also into the condensing section 252. Others are processing air cooler 300
It has basically the same operation as the case where d is used.

Next, referring to FIG. 5, heat pump HP1
The operation of will be described. FIG. 5 is a Mollier diagram when the refrigerant HFC134a is used. In this diagram, the horizontal axis is enthalpy and the vertical axis is pressure. (A) shows the case where the processing air cooler 300d is used, and (B) shows the case where the processing air cooler 300 is used.

In FIG. 5A, the point a is the refrigerant evaporator 2 in FIG.
10 is a state of a refrigerant outlet, and is in a state of a saturated gas.
The pressure is the first pressure of the present invention, and is 4.2 kg / c.
m ² , temperature 10 ° C., enthalpy 148.83 kca
1 / 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 which is the second pressure of the present invention, the temperature is 78 ° C., and the state is a superheated gas.

This refrigerant gas is cooled in the refrigerant condenser 220 and reaches a point c on the Mollier diagram. This point is a saturated gas state, the pressure is 19.3 kg / cm ² , and the temperature is 65 ° C. Under this pressure, it is further cooled and condensed,
The point d is reached. This point is in the state of a saturated liquid, the pressure and temperature are the same as in point c, the pressure is 19.3 kg / cm ² , the temperature is 65 ° C., and the enthalpy is 122.97 kcal / k.
g.

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 the point i and the liquid in the state at the point g are mixed at the header 370, at the refrigerant pipe 203, or at the evaporator 210. Part of the refrigerant liquid in the header 370 is mixed with the liquid at the point e by the refrigerant pump 380, and the evaporating sections 251A, B, and C and the condensing section 252 are formed.
A, B and C are circulated.

Another part of the refrigerant liquid in the header 370 is reduced in pressure by the expansion valve 270 to become a refrigerant (mixture of gas and liquid) having a pressure of 4.2 kg / cm ² and a temperature of 10 ° C. FIG. 5
(A) shows the refrigerant liquid from the condensing section 252D (point i).
Is not gathered in the header 370, but in the middle of the pipe 345 (FIG. 2), a restriction 27 different from the restriction 270 is formed.
0 '(not shown), and is shown as the refrigerant via the throttle 270 and the refrigerant via the throttle 270' merging (or mixing in the evaporator 210) after each throttle. ing.

As described above, when the heat exchanger 300d and the gas-liquid separator 350 according to the embodiment of the present invention are used, 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 this way, the heat pipe action of each heat transfer tube (the phase change of the refrigerant, especially the 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 refrigerant pump 380 increases the flow rate of the refrigerant liquid, the cooling capacity for cooling the processing air increases, and the heat transfer coefficient improves.

Next, a case where the processing air cooler 300 is used will be described with reference to FIG. Up to the point d, the process is the same as in the case of the processing air cooler 300d, and a duplicate description will be omitted. The refrigerant liquid in the state at the point d is depressurized by the throttle 360 and flows into the evaporating section 251 of the processing air cooler 300 as a heat exchanger in a gas-liquid mixed state. On the Mollier diagram, it is indicated by a point s. The temperature will be about 40 ° C. The pressure is an intermediate pressure of the present invention, and is 4.2 k in the present embodiment.
A saturation pressure corresponding to an intermediate value between g / cm ² and 19.3 kg / cm ² , ie, 40 ° C. Here, a part of the liquid is evaporated and the liquid and the gas are mixed.

In the evaporating section 251, under the second pressure, the refrigerant liquid evaporates to reach a point f between the saturated liquid line and the saturated gas line at the same pressure. Here, the liquid is almost or partially evaporated. At the point s, the ratio between the refrigerant liquid and the gas is the inverse ratio of the difference between the enthalpy at the point where the saturated pressure line at 40 ° C. crosses the saturated liquid line and the saturated gas line and the enthalpy at the point d. As is clear from the diagram, the liquid is more in weight ratio. However, since the volume ratio of gas is overwhelmingly large, the liquid is mixed with a large amount of gas in the evaporating section, and the liquid evaporates while the liquid wets the inner surface of the tube of the evaporating section.

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 and / or sprayed water flowing through the second compartment and reaches point g. This point is on the saturated liquid line in the Mollier diagram. Temperature 40 ° C, enthalpy 1
13.51 kcal / kg.

The refrigerant liquid in the state of the point g is supplied to the refrigerant pump 380
Circulates through the evaporating section 251 and the condensing section 252. In the figure, a bold solid line and an arrow indicate a circulating state.

The refrigerant liquid at point g is condensed at a temperature of 10
The pressure was reduced to a saturation pressure of 4.2 kg / cm ² ,
The point that reaches the refrigerant evaporator 210 is that the processing air cooler
The same as in the case of d. As described above, in the processing air cooler 300, the refrigerant evaporates from the point s 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. Very high heat transfer rate due to heat transfer and condensation heat transfer. Further, since the refrigerant liquid repeatedly circulates between the point g and the point f, even in the case of an air-conditioning load in which the point f goes over the saturated gas line and enters the gas side (becomes a superheated gas) without repeated circulation,
The point f can be kept in the wet area, and the effect of improving the heat transfer coefficient is doubled.

The amount of refrigerant flowing through the evaporating section 251 and the condensing section 252 together with the amount of refrigerant returned and circulated by the pump 380 is sent to the evaporator 210 in either of the processing air coolers 300 and 300d. The refrigerant amount is about 1.1 to 3 times, preferably 1.3 to 2 times.

Further, as the compression heat pump including the compressor 260, the refrigerant condenser (regeneration air heater) 220, the throttles 360 and 270, and the refrigerant evaporator 210, if the processing air cooler 300 or 300d is not provided, the refrigerant Since the refrigerant in the state of the point d in the condenser 220 is returned to the refrigerant evaporator 210 through the throttle, the enthalpy difference available in the refrigerant evaporator 210 is 148.83-122.97 = 2.
Whereas there is only 5.86 kcal / kg, in the case of the heat pump HP1 used in the present embodiment having the processing air cooler 300 or 300d, it is 148.83-11.
3.51 = 35.32 kcal / kg, and 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 processing air cooler 300 or 300d allows the heat pump HP1 to have the same function as the economizer.

Referring to FIG. 6, an example of the mechanical arrangement of the dehumidifying air conditioner described above will be described. In FIG. 6, devices constituting the apparatus are housed in a cabinet 700. The blower 102, the compressor 260, and the blower 14 are arranged side by side in a substantially horizontal direction in a space below the cabinet 700.
0 is arranged. Above these, the desiccant rotor 103 is arranged with the rotation axis directed vertically.

A processing air cooler 300d is provided vertically above the desiccant rotor 103, and a processing air cooler 3d is provided above a half (semicircle) region where processing air flows in.
00d first section 310, evaporating section 251
Is arranged.

Above the first section 310 in the vertical direction, a refrigerant evaporator 210 is arranged with its cooling pipe horizontal.

[0086] The refrigerant condenser 220 has a heat exchanger tube disposed substantially horizontally, and is disposed substantially side by side with the refrigerant evaporator 210. The space below the refrigerant condenser 220 in the vertical direction and between the desiccant rotor 103 forms a path 127, through which the desiccant rotor 103
It is configured such that the regeneration air is guided to the other half area with respect to the processing air side half described above.

Further, an outside air intake port is opened on the side of the cabinet 700, above the blower 102, and almost directly above the intake port of the processing air. Near the opening, above the blower 102, a humidifier is provided. 165 are provided substantially horizontally. The space above the humidifier 165 is the second compartment 32
0, in which a condensing section 25 is provided.
Two heat exchange tubes are arranged substantially horizontally.
In the space above the condensing section 252, the watering pipe 32
5 is arranged so that water can be sprayed from above the tubes (and fins) of the condensation section 252. An air outlet is opened vertically above the second section 320. This air outlet is provided with a blower 160
Is provided.

A first throttle 360 is provided below the refrigerant condenser 220, and a gas-liquid separator 35 is provided below the first throttle 360.
0 is set. The gas-liquid mixture whose pressure has been reduced by the throttle 360 and a part of the refrigerant liquid has evaporated is led to the gas-liquid separator 350, where it is separated into refrigerant liquid and refrigerant gas. Gas-liquid separator 35
0 is located below the heater 220 and near the first section 310 of the heat exchanger 300d.

A header 370 for collecting the refrigerant condensed in the condensing section 252 is provided at the outlet of the condensing section 252. The refrigerant pipe from the header 370 rises from the header 370 and is depressurized by a throttle 270 provided near the top of the pipe.

Further, below the second section 320, a refrigerant liquid pump 380 is installed, and the condensing section 25 is provided.
The refrigerant liquid is returned from the header 370 to the gas-liquid separator 350 through a refrigerant liquid pipe laid substantially horizontally along the heat exchange tube of the evaporator section 251 and the evaporating section 251.

FIG. 7 shows an example of a typical mechanical arrangement of a dehumidifying air conditioner according to another embodiment. In the example shown in this figure, a heat exchanger 300d is used, and an ejector is used as a refrigerant liquid return device. Other basic configurations are the same as those in FIG.

The refrigerant liquid pipe exiting the condenser 220 is laid almost horizontally above the evaporator 210 and the second section 320, and is connected to a throttle 360 arranged near the falling header 370. . In this embodiment, an ejector 375 is provided in the header 370.

The ejector 375 is configured so that the gas-liquid mixture which has been decompressed by the throttle 360 and a part of the refrigerant has been vaporized and expanded is blown out in a substantially horizontal direction. However, the blowing is not limited to the horizontal direction but may be vertically upward, downward or obliquely. What is necessary is just to determine mainly considering a mechanical arrangement.

The gas-liquid mixture blown out in a substantially horizontal direction sucks the refrigerant liquid collected and accumulated in the header 370, and accompanying this, the header 350 (in this embodiment, the gas-liquid separator as a gas-liquid separator) is used. No function). In this way, the refrigerant liquid once collected in the header 370 can circulate again through the evaporating section 251 and the condensing section 252. With this configuration, the refrigerant can be circulated using the expansion force of the refrigerant, so that there is no need to provide a refrigerant liquid pump that requires a separate driving force.

In the above embodiment, as shown in FIG. 2 or FIG. 3, the processing air cooler of the present invention comprises the heat exchange tubes of the evaporation section 251A and the corresponding heat exchange tubes of the condensation section 252A (evaporation section). Section 2
51B, C and the condensing sections 252B, C) have been described as being configured as an integrated flow path by one tube, but the present invention is not limited to this, and the evaporating section 251 and the condensing section 252 May be configured separately. That is, the evaporating section 251 and the condensing section 252 are separated, the refrigerant downstream side of the tube constituting the evaporating section 251 is assembled in the header, and the refrigerant upstream side of the tube constituting the condensing section 252 is similarly assembled in another header. Then, the respective headers may be connected by piping. In that case, the first section 310 and the second section 320 are not partitioned by one partition 301 but are formed as chambers each having individual walls. In this way, the evaporating section 251 and the first section 310 and the condensing section 252 and the second section 320 can be separated and freely positioned and installed.

[0096]

According to the present invention, a processing air cooler is provided. The processing air cooler is configured to cool the processing air by evaporating the refrigerant, and cool and condense the evaporated refrigerant by the cooling fluid. A refrigerant liquid return device that can use the high coefficient of evaporation heat transfer and condensation heat transfer and returns the refrigerant to the upstream side of the refrigerant flow, so that the cooling effect of cooling the processing air can be enhanced and the heat transfer can be high. The heat transfer between the processing air and the cooling fluid can be achieved at a high rate. In addition, since the heat transfer between the processing air and the cooling fluid is performed via the refrigerant, the components of the dehumidifying air conditioner can be easily arranged.

The processing air is cooled by a refrigerant evaporating at a first pressure, and the regenerated air is heated by a refrigerant condensing at a second pressure.
Cooling the process air by evaporating the refrigerant at a pressure intermediate the first and second pressures, condensing the refrigerant at approximately the same pressure as the intermediate pressure, and providing the condensed refrigerant for re-evaporation Therefore, the refrigeration effect can be enhanced, the processing air can be cooled with a high heat transfer coefficient, and a method of dehumidifying the processing air with a high COP can be provided.

[Brief description of the drawings]

FIG. 1 is a flowchart of a dehumidifying air conditioner according to a first embodiment of the present invention.

FIG. 2 is a schematic sectional view of a heat exchanger suitable for use in a heat pump used in the dehumidifying air conditioner of FIG.

FIG. 3 is a schematic sectional view of a heat exchanger suitable for use in place of the heat exchanger of FIG. 2;

FIG. 4 is a psychrometric chart for explaining the operation of the dehumidifying air conditioner of FIG. 1;

5 is a Mollier diagram of a heat pump used in a dehumidifying air conditioner using the heat exchanger of FIG. 2 and the heat exchanger of FIG. 3;

FIG. 6 is a schematic front sectional view showing an example of the actual structure of the dehumidifying air conditioner shown in the flowchart of FIG.

7 is a schematic front sectional view showing an example of the actual structure of the dehumidifying air conditioner using the heat exchanger and the ejector shown in FIG.

FIG. 8 is a flowchart of a conventional dehumidifying air conditioner.

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

[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 251A, 251B, 251C Evaporation section 252A, 252B, 252C, 252D Condensing section 270, 360 Restriction 260 Compression Machine 300, 300d Process air cooler 310 First section 320 Second section 325 Watering pipe 350 Gas-liquid separator 370 Header 375 Ejector 380 Refrigerant liquid pump 700 Cabinet HP1 Heat pump

Claims (6)

[Claims] 1. A moisture adsorbing device having a desiccant for adsorbing moisture in processing air; and said processing air as a low heat source;
A heat pump that operates using regeneration air for regenerating the desiccant as a high heat source; the heat pump includes an evaporator that evaporates a refrigerant with the processing air; a condenser that condenses the refrigerant with the regeneration air; A processing air cooler provided through a throttle that reduces the pressure of the refrigerant condensed in the condenser in a refrigerant path from the evaporator to
The process air cooler is configured to place the process air and the cooling medium in a heat exchange relationship, and the process air cooler is intermediate between a refrigerant evaporation pressure in the evaporator and a refrigerant condensation pressure in the condenser. The heat pump is configured to condense the refrigerant by heating the cooling medium by evaporating the refrigerant by heating heat from the processing air before reaching the evaporator after passing the desiccant after the pressure, and the heat pump further comprises:
A dehumidifier is provided with an increasing means for relatively increasing the amount of refrigerant passing through the processing air cooler. 2. The processing air cooler includes: an evaporating section for removing heat from the processing air to evaporate a refrigerant; a condensing section for condensing the refrigerant by heating the cooling medium; The dehumidifier according to claim 1, wherein the device is configured to circulate a refrigerant between the evaporating section and the condensing section. 3. A process air cooler provided downstream of a flow of the process air with respect to the process device, wherein the process device further comprises a desiccant for adsorbing moisture 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 cooling liquid return device for returning the condensed refrigerant liquid to an upstream side of the one-way flow with respect to the processing air cooler so as to be subjected to evaporation in the processing air cooler. A dehumidifier. 4. 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; supplying the refrigerant condensed by the condenser to the processing air cooler. The dehumidifying device according to claim 3, wherein: 5. The dehumidifier according to claim 4, 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. . 6. A first step of adsorbing moisture in the processing air with a desiccant; and a second step of evaporating the refrigerant liquid at a predetermined pressure to cool the processing air having adsorbed the water in the first step. A third step of condensing the refrigerant evaporated at the predetermined pressure at substantially the same pressure as the predetermined pressure;
And a fourth step of providing the refrigerant condensed in the second step to evaporate in the second step; a method of dehumidifying treated air.