JPH11137947A - Dehumidifying air conditioner - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide an energy-saving and compact dehumidifying air conditioner. SOLUTION: This dehumidifying air conditioner has a treated air line and a regenerated air line and further a heat exchanger between the treated air with moisture adsorbed and the air to be regenerated before being dehumidified by a desiccant and heated by a heating source. The desiccant is not deliquescent, and the maximum value of the differentiated heat of adsorption when the moisture of >=20% of the maximum adsorption amount is adsorbed, is <=1.1 times as high as the heat of condensation of water. Further, when the relative adsorption amount obtd. by defining the maximum adsorption amount at 90% relative humidity as the denominator and the adsorption amount as the numerator is denoted by X, the relative humidity by P and the isotherm separation factor by R, and the function shown by X=R/(R+P-R.P) is used, the adsorption isotherm exhibiting the absorption characteristics of the desiccant lies in the area enclosed between the X-P curve at R=0.2 and the X-P curve at R=2.5 in the relative humidity range of 30% to 70%.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a dehumidifying air conditioner, and more particularly to a dehumidifying air conditioner capable of continuously performing a desiccant adsorption process with a desiccant and a desiccant regeneration process with regenerated air heated by a heating source. .

[0002]

2. Description of the Related Art FIG. 16 shows a prior art in which a processing air path A, a regeneration air path B, a desiccant rotor 103, two sensible heat exchangers 104 and 121, a heater 220, Using the humidifier 105 as a main component, the processing air is dehumidified by the desiccant rotor 103, and the processing air heated by the heat of moisture adsorption of the desiccant exchanges heat with the regenerated air in the first sensible heat exchanger 104 to be cooled. After that, while being humidified by a humidifier and supplied to the air-conditioned space, the regenerated air is taken in from the external space (OA) and exchanged with the processing air in the first sensible heat exchanger 104 to raise the temperature. The relative humidity was reduced by heating with a heating source 200 in a vessel 220, and the desiccant rotor 103 was passed through the desiccant rotor 103 to desorb and regenerate moisture in the desiccant rotor 103. In this conventional example, the sensible heat component of the regenerated air after regeneration is further recovered by exchanging heat with the regenerated air before heating in the second sensible heat exchanger 121, and then discharged to the outside (EX). Was.

[0003] Such a technique is called so-called desiccant air conditioning, and has a high practical value as a technique capable of controlling the humidity of an air-conditioned space. It is known that silica gel or zeolite is used as the desiccant used for such desiccant air conditioning. However, it is a modified zeolite, which is classified into Brunauer type 1, and has an isothermal separation factor of 0.07 to 0.07. It is known that a value in the range of 0.5 is most suitable for a desiccant air conditioner that heats regeneration air with combustion gas. In the past, lithium chloride was used as a hygroscopic substance in the past. However, in a high-humidity environment, lithium chloride is deliquescent and has a drawback of falling off from the rotor, so that it is gradually not used.

[0004]

In the prior art as described above, in a desiccant air conditioner which heats regeneration air with combustion gas, the regeneration temperature of the desiccant is 101 ° C. (215 ° C.).
(F) to 143 ° C. (290 ° F.), and zeolite is suitable as a desiccant suitable for such a regeneration temperature. In particular, as shown in FIG. 17, the isothermal separation factor (separation factor) is 0.07. ~ 0.5
It is known that it is optimal to have an adsorption characteristic indicated by an adsorption isotherm in the range of However, when various waste heat or solar heat is to be used as a desiccant regeneration heat source, it is easier to put the regeneration temperature to 65 to 75 ° C. because there are many available heat sources, and in such a case, the zeolite is used. Is not always optimal.

The reason will be described below with reference to FIG. FIG. 17 is an adsorption isotherm of zeolite. When outdoor air is used as regenerating air for desiccant air conditioning, the absolute humidity in summer is typically 21 g for those skilled in air conditioning design.
/ Kg or so. 101 ℃
Heating to about 3.0% relative humidity. On the other hand, the relative humidity of the adsorbed processing air is determined by the JI of the air conditioner.
Dry-bulb temperature 2 based on indoor conditions specified in S-C9612 etc.
7 ° C. and a wet bulb temperature of 19 ° C. are common, at which time the relative humidity is about 50%. The desiccant thus alternates between 50% process air and 3.0% process air.

[0006] The water content of the zeolite when equilibrated in contact with the regenerating air, as shown in FIG.
Using a function represented by (R + P−RP), the isotherm separation factor R = 0.1, and when the relative humidity is 3.0%, when P = 0.030, X = 0.30. 236
Becomes On the other hand, the water content of the zeolite when equilibrated by contacting with the processing air from the room is similarly calculated by setting the isotherm separation factor R = 0.1 and P = 0.5.
X = 0.910. Therefore, when the regenerated air is heated to 101 ° C. using zeolite, the desiccant has a difference in the relative adsorption amount of 0.910−0.236 = 0.67.
4 can be adsorbed and desorbed by a value obtained by multiplying the maximum amount of adsorption.

If a material such as silica gel having a linear adsorption isotherm (isothermal separation factor R = 1) is used, the difference in the amount of adsorption and desorption is the same as the difference in relative humidity.
500−0.030 = 0.470, which is 0.470 times the maximum adsorption amount. Further, a differential coefficient dP / d indicating a ratio of a change amount ΔP of the relative humidity to a change amount ΔX of the adsorption / desorption amount.
As X is smaller, the water vapor pressure is less likely to increase even when moisture is adsorbed, and the driving force for adsorption is maintained, so that the adsorption speed can be increased. Therefore, the relative humidity is plotted on the horizontal axis and the relative moisture content is plotted on the vertical axis. When viewed from above, it is advantageous that the adsorption isotherm has an upwardly convex shape. Therefore, in this case, zeolite is more advantageous. As described above, the regeneration temperature is 101, which is shown in the conventional example.
At higher temperatures, such as ° C, it was advantageous to use zeolites. However, if the same difference in adsorption and desorption is calculated at a regeneration temperature of 65 to 75 ° C. as intended by the present invention, the result will be different.

That is, when regenerated air having an absolute humidity of 21 g / kg is heated to 70 ° C., the relative humidity becomes 10.6%
become. Therefore, when the relative humidity is 10.6%, the water content of the zeolite when equilibrated in contact with the regeneration air is calculated as P = 0.106, and X = 0.532.
Becomes On the other hand, the water content of the zeolite when equilibrated by contact with the processing air from the room is the same as above, and P =
If calculated as 0.5, X = 0.910. Therefore, when regenerating air is heated to 70 ° C. using zeolite, the desiccant takes the difference between the two and 0.910-
0.532 = 0.378, that is, 0.378 of the maximum adsorption amount
It can absorb and desorb twice as much water. Further, the curve connecting the suction start point and the end point has a small curvature in this section, is not much different from a linear straight line, and the effect of increasing the suction speed is almost the same as that of the linear case.

If a material such as silica gel having a linear adsorption isotherm (isothermal separation factor R = 1) is used, the difference in the amount of adsorption and desorption is the same as the difference in relative humidity.
5−0.106 = 0.394, which is the maximum adsorption amount of 0.
The adsorption and desorption of 394 times was possible, and 0.37 of the zeolite
More than 8. In addition, as described in a known document (for example, practical design of dehumidification for an air conditioning engineer, Kyoritsu Shuppan, 1980, Chapter 4, FIG. 4.1), the maximum adsorption amount of silica gel is higher than that of zeolite. Therefore, 65-
For desiccant air conditioning at a regeneration temperature of 75 ° C., desiccants such as silica gel having adsorption isotherms that are nearly linear are more advantageous than zeolite. However, zeolites and silica gels have drawbacks due to common heat of adsorption. The reason will be described below.

FIG. 18 shows a desiccant air-conditioning cycle having the equipment configuration shown in FIG. 16 on a psychrometric chart, and the solid line in the figure shows the process when the heat of adsorption is large.
The dotted line shows the process when the heat of adsorption is small (close to the latent heat of condensation of water), the alphabetic symbols K to V indicate the states of air in FIG. 16 when the heat of adsorption is large, and L 'to V' are the adsorption. 17 shows each state of air in FIG. 16 when heat is small.

FIG. 1 shows changes in the states of the processing air and the regeneration air.
8, the process air (state K) is adsorbed by the desiccant rotor 103 (state L), and is cooled by heat exchange with the regenerated air (state Q) in the first sensible heat exchanger 104 (state M). ), Humidified by the humidifier 105 (state P)
Return to the air-conditioned space 101. On the other hand, the regenerated air takes in outside air (state Q), is heated and exchanges heat with the processing air (state L) in the first sensible heat exchanger 104 (state R), and is further regenerated air after desiccant regeneration (state R). U) and the second sensible heat exchanger 121 are heated and exchanged (state S), and the heater 220
After being heated by the heating source in (state T), the desiccant rotor 103 is regenerated. The regenerated air (state U) in which the desiccant has been regenerated is supplied to the second sensible heat exchanger 121.
Then, the heat is recovered by exchanging heat with the regenerated air exiting the first sensible heat exchanger 104 (state V) and then discarded as exhaust gas to the outside.

In the desiccant air conditioner forming such a cycle, the performance tends to decrease as the heat of adsorption increases. This will be described below using mathematical expressions. The moisture adsorption process (states K to L, L ') on the psychrometric chart of FIG.
When the heat of adsorption is equal to the heat of condensation of water (states K to L '), the following equation is established from the heat balance. .DELTA.X.R = .DELTA.T.Cp Therefore, this process has a gradient of .SIGMA.X / .DELTA.T = Cp / R.SIGMA.Ci
(Where R is the latent heat of condensation of water and Cp is the specific heat at constant pressure of air). On the other hand, when there is heat of adsorption (states K to L), the gradient is similarly set to ∂X / ∂T = C
It is indicated by a line segment of p / H ≒ Cs (= constant) (where H is the heat of adsorption). Normally, the heat of adsorption H> the heat of condensation R, so that the gradient of the line segment in the adsorption process with the heat of adsorption is closer to horizontal than in the process without the heat of adsorption.

The cooling effect of the desiccant cycle shown in FIG. 18 is compared between the case where the heat of adsorption is present (when the heat of condensation is larger) and the case where the heat of adsorption is not present (when the heat of condensation is equal). The indoor state (state K) of the processing air is the dry bulb temperature Tr and the absolute humidity Xr, and the dehumidification amount of the processing air is ΔX. The outside air having the same flow rate as the processing air is used as the regeneration air (therefore, the humidification amount of the regeneration air also becomes ΔX), the inlet conditions are dry bulb temperature To, the absolute humidity Xo, and the regeneration temperature is Tg. These conditions are compared with each other with and without heat of adsorption. In the process of adsorption and dehumidification of treated air, if there is no heat of adsorption, the temperature Tl 'after adsorption is: Tl' = Tr + ΔX / Ci (1) where ΔX is the absolute value of the humidity difference before and after dehumidification. This processing air exchanges heat with the outside air, and becomes the state M '. The temperature of the state M ′ is as follows: Tm ′ = Tl′−ε (Tl′−To) = (1−ε) Tl ′ + To = (1−ε) (Tr + ΔX / Ci) + To (2) where ε is the first Is the temperature efficiency of the sensible heat exchanger, which is a function of NTU (number of heat passing) (ε = f (NTU)). In this calculation example, the flow rate, the heat transfer If the coefficient and the heat transfer area are equal, the NTU is the same, so there is no difference and it can be treated as a constant.

Similarly, when the heat of adsorption is present, Tm = T1-ε (T1-To) = (1-ε) T1 + εTo = (1-ε) (Tr + ΔX / Cs) + εTo (3) The lower the dry bulb temperature of M or M ', the greater the cooling effect. Therefore, taking the difference between Tm and Tm', Tm'-Tm = (1-.epsilon.) (1 / Ci-1 / Cs) ΔX = (1−ε) (Cs−Ci) ΔX / CiCs (4) Since Cs <Ci, Tm′−Tm <0, and therefore, Tm ′ <Tm and a smaller heat of adsorption, The temperature decreases and the cooling effect increases. That is, in FIG.
ΔQ ′> ΔQ, and the greater the heat of adsorption, the smaller the cooling effect.

Next, the required heating amount of the regeneration air will be compared between a case where the heat of adsorption is present (when the heat of condensation is larger) and a case where it is not present (when the heat of condensation is equal to the heat of condensation). Figure 1 as above
8, when there is no heat of adsorption, the state U 'is Tu' = Tg-.DELTA.X / Ci (5) The state R 'is Tr' = To + .epsilon. (T1'-To) = (1-.epsilon.) To + .epsilon.Tl ' (6) Since the state U ′ and the state R ′ exchange heat, the state S ′ is Ts ′ = (1−ε) To + εTl ′ + ε ′ [(Tg−ΔX / Ci) − (1−ε) To−εTl '] = (1−ε ′) (1−ε) To + ε ′ (Tg−ΔX / Ci) + ε (1−ε ′) Tl ′ (7) where ε ′ is the temperature of the second sensible heat exchanger. It shows efficiency and can be treated as a constant as above. Similarly, the state U when the heat of adsorption is large is as follows: Ts = (1−ε ′) (1−ε) To + ε ′ (Tg−ΔX / Cs) + ε (1−ε ′) Tl (8) In this case, the higher the dry bulb temperature of the state S ′ or S, the smaller the regeneration heating amount.
Ts′−Ts = −ε ′ (ΔX / Ci−ΔX / Cs) + ε (1−ε ′) (T1′−T1) = − ε ′ (ΔX / Ci−ΔX / Cs) + Ε (1−ε ′) [(Tr + ΔX / Ci) − (Tr + ΔX / Cs)] = ΔX (Ci−Cs) (ε′−ε + ε′ε) / CsCi (9) Usually, the temperatures of the two sensible heat exchangers The efficiency is 70% or more. In this range, (ε′−ε + ε′ε) is positive, and since Ci> Cs, the equation (9) is positive. Therefore, S
The smaller the heat of adsorption becomes, the higher the temperature of the point becomes, so that the amount of heating of the regeneration air may be small. That is, in FIG.
G ′ <ΔG. Therefore, as the heat of adsorption increases, the amount of heat required to heat the regeneration air increases.

As described above, the smaller the heat of adsorption of the desiccant, the greater the cooling effect and the less the amount of heating of the regenerated air. Therefore, it is desirable to use a desiccant with as little heat of adsorption as possible. It is reported that zeolite and silica gel are larger than the heat of condensation of water as shown in the following known examples 1 to 5. (Known Example 1) FIG. 17 of JP-A-6-277440 shows that the heat of differential adsorption of the modified zeolite is 1.28 times the heat of condensation of water, and the practical range of desiccant air conditioning (adsorption amount 0.06 to 0.2 g /
In g), it is described that it is almost constant. (Known Example 2) In the literature (Practical Design of Dehumidification for Air Conditioning Engineers, Kyoritsu Shuppan, 1980), Ch.4, p.172, it is described that zeolite has twice the heat of condensation of water. (Known Example 3) Literature (Air Conditioning Sanitation Engineering Vol. 57 No. 7 61)
Page) describes that silica gel has a heat of adsorption of 800 kcal / kg. (Known Example 4) Literature (Practical Design of Dehumidification for Air Conditioning Engineers, Kyoritsu Shuppan, 1980), Ch 4, 172, describes that silica gel has 1.3 times the heat of condensation of water. . (Known Example 5) Literature (Heat Recovery Systems, Vo, UK)
l. 6, No. 2, pp 151-167, 1986, Fi
g. It is described in 5) that the maximum value of the heat of differential adsorption of silica gel is 1.33 times the heat of condensation of water, and the minimum value is 1.12 times the heat of condensation of water. For this reason, zeolite and silica gel have disadvantages in that the cooling effect is reduced and the amount of heating of the regenerated air is increased as compared with desiccant having little heat of adsorption.

On the other hand, as a desiccant having a relatively small heat of adsorption, there is a method of using lithium chloride impregnated in a fibrous material, and the heat of adsorption is reported to be low in the following known example 6: . (Known Example 6) Literature (Air Conditioning Sanitation Engineering Handbook (Showa 42)
However, as described above, since lithium chloride is deliquescent under high humidity, its use conditions are limited, and desiccant air conditioning is used as described above. Can not be used.

As another desiccant having a relatively small heat of adsorption, there is a method using activated carbon. Activated carbon, particularly wood-based activated carbon, has an adsorption isotherm described in the following known example 7 shown in FIG. As described above, there is a characteristic that the water content rapidly rises from a relative humidity region of 40 to 50%,
Therefore, under the use condition of the desiccant air conditioning, the amount of adsorption and desorption of moisture is small, and the differential coefficient dP / dX indicating the ratio of the change ΔP of the relative humidity to the change ΔX of the adsorption and desorption is large and convex downward. There was a drawback that the adsorption speed was slow. (Known Example 7) Literature (Chemical Engineering Transactions, Vol. 15, No. 1)
No. 1989, pp 38-43, Fig. 4)

As described above, in the prior art, desiccants having excellent adsorption characteristics have a drawback in that heat energy is increased due to large heat of adsorption, and desiccants having low heat of adsorption have adsorption characteristics matching the use conditions of desiccant air conditioning. In particular, the maximum value of the heat of differential adsorption is 1.1% of the heat of condensation of water.
And the adsorption characteristic indicated by the adsorption isotherm is 65 to 75 times
The use of desiccants having properties suitable for regeneration temperatures of ° C. has not been made.

[0020]

SUMMARY OF THE INVENTION The present invention has been made in view of the above points, and has as its object to provide an energy-saving and compact dehumidifying air conditioner.

[0021]

Means for Solving the Problems The present invention has been made to achieve the above-mentioned object, and the invention according to claim 1 has a processing air path in which moisture is adsorbed by a desiccant and a heating air path after being heated by a heating source. It has a path for regeneration air that passes through the desiccant after adsorbing the moisture and desorbs and regenerates the moisture in the desiccant, and the treated air to which the moisture is adsorbed and the regeneration air before desiccant regeneration and before being heated by the heating source. In a dehumidifying air-conditioning apparatus having a heat exchanger between it and the desiccant, there is no deliquescent and the maximum value of the differential heat of adsorption when adsorbing water of 20% or more of the maximum adsorbed amount is one of the heat of condensation of water. When the adsorption isotherm that is less than or equal to 1 and that indicates the desiccant adsorption characteristics is within the range of 30% to 70% relative humidity, the maximum adsorption amount at a relative humidity of 90% is defined as a denominator, and the adsorption amount is defined as a numerator. phase The amount of adsorption is X, the relative humidity is P, the isotherm separation factor is R, and an isotherm separation factor R = 0.2 is obtained using a function represented by the formula X = P / (R + P-RP). XP curve and isotherm separation factor R = 2.5
And a desiccant existing in a range surrounded by an XP curve obtained as follows.

As described above, an air conditioner is constructed by using a desiccant having no deliquescent, having a smaller heat of adsorption than conventional desiccants, and having characteristics suitable for a regeneration temperature of 65 to 75 ° C. An energy-saving and compact dehumidifying air conditioner can be provided.

According to a second aspect of the present invention, there is provided the dehumidifying air conditioner according to the first aspect, wherein a porous alumina-crosslinked clay is used as a desiccant. As described above, by using an alumina crosslinked clay porous material as a desiccant, a desiccant having no deliquescent, having a lower heat of adsorption than conventional desiccants, and having characteristics suitable for a regeneration temperature of 65 to 75 ° C. can be obtained. In addition, an energy-saving and compact dehumidifying air conditioner can be provided.

According to a third aspect of the present invention, the alumina-crosslinked clay porous body is obtained by exchanging exchangeable cations between layered silicate layers with aluminum-containing polynuclear metal hydroxide ions and subjecting the resultant to heat dehydration. The dehumidifying air conditioner according to claim 2, wherein: In this way, the exchangeable cation between the layered silicate layers is exchanged with a polynuclear metal hydroxide ion containing aluminum, and this is heated and dehydrated to produce an alumina-crosslinked clay porous body, which is used as a desiccant. Thus, a desiccant having less heat of adsorption than conventional desiccants and having characteristics suitable for a regeneration temperature of 65 to 75 ° C. can be obtained, and an energy-saving and compact dehumidifying air conditioner can be provided.

According to a fourth aspect of the present invention, there is provided the dehumidifying air conditioner according to the third aspect, wherein the layered silicate is a natural or synthetic smectite. Thus, using a natural or synthetic smectite such as montmorillonite having an exchangeable cation as the layered silicate, the exchangeable cation between the layered silicate layers is exchanged with a polynuclear metal hydroxide ion containing aluminum, and this is exchanged. By heating and dehydrating to produce an alumina crosslinked clay porous material and using it as a desiccant, it has no deliquescence, has a lower heat of adsorption than conventional desiccants, and has properties suitable for a regeneration temperature of 65 to 75 ° C. Thus, an energy-saving and compact dehumidifying air conditioner can be provided.

According to a fifth aspect of the present invention, there is provided the dehumidifying air conditioner according to the first aspect, wherein a structured activated carbon is used as a desiccant. As described above, by using the structured activated carbon as the desiccant, there is no deliquescence, the heat of adsorption is smaller than that of the conventional desiccant, and 65 to 75 ° C.
A desiccant having characteristics suitable for the regeneration temperature of
An energy-saving and compact dehumidifying air conditioner can be provided.

The invention according to claim 6 is characterized in that the structural activated carbon is obtained by carbonizing polyvinyl formal and activating the activated carbon at a temperature of 850 ° C. or less. Device. As described above, the polyvinyl formal is carbonized, activated at a temperature of 850 ° C. or less to produce a structured activated carbon, and is used as a desiccant. Thus, there is no deliquescence, and the heat of adsorption is smaller than that of the conventional desiccant. A desiccant having characteristics suitable for a regeneration temperature of 65 to 75 ° C. can be obtained, and an energy-saving and compact dehumidifying air conditioner can be provided.

According to a seventh aspect of the present invention, there is provided the dehumidifying air conditioner according to the first aspect, wherein a porous aluminum phosphate (molecular sieve) is used as a desiccant. As described above, an air conditioner is configured by using aluminum phosphate (molecular sieve) having no deliquescent, having less heat of adsorption than conventional desiccants, and having characteristics suitable for a regeneration temperature of 65 to 75 ° C. as a desiccant. By doing so, an energy-saving and compact dehumidifying air conditioner can be provided.

According to the invention of claim 8, the porous aluminum phosphate (molecular sieve) is a heat dissociable template (for example, aluminum hydroxide, boehmite, pseudo boehmite, etc.) and phosphoric acid. The dehumidifying air conditioner according to claim 7, wherein the air conditioner is a substance obtained by a reaction using an organic base such as tripropylamine. By using the porous aluminum phosphate (molecular sieve) thus produced as a desiccant, there is no deliquescence, the heat of adsorption is smaller than that of a conventional desiccant, and a characteristic suitable for a regeneration temperature of 65 to 75 ° C. Thus, it is possible to provide an energy-saving and compact dehumidifying air conditioner.

According to the ninth aspect of the present invention, the regenerated air is supplied to 75
The dehumidifying air conditioner according to any one of claims 1 to 8, wherein the desiccant is regenerated by heating to a temperature of not more than ° C. As described above, by regenerating the desiccant at the regeneration temperature that matches the adsorption characteristics of the desiccant and by using a relatively low driving heat source, an energy-saving dehumidifying air conditioner can be provided.

According to a tenth aspect of the present invention, the process air that has undergone heat exchange with the regeneration air after moisture adsorption is cooled by a low heat source of a heat pump, and the regeneration air before desiccant regeneration is heated by a high heat source of the heat pump. The dehumidifying air conditioner according to claim 9, wherein As described above, by taking heat from the regenerated air after moisture adsorption and using the heat for regenerating the regenerated air, multiple effects of the driving energy of the heat pump can be achieved, and an energy-saving dehumidifying air conditioner can be provided. it can.

[0032]

DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of a dehumidifying air conditioner according to the present invention will be described below. A first embodiment of the present invention is to use a natural or synthetic smectite such as montmorillonite having a sodium group as an exchangeable cation as a layered silicate, and to convert the exchangeable cation between the layered silicate layers into an aluminum-containing polynuclear metal. This is a dehumidifying air conditioner in which a material exchanged with hydroxide ions and heated and dehydrated to form a porous alumina cross-linked clay is used as a desiccant. The moisture absorption characteristics and the production method of this kind of porous alumina cross-linked clay are described in the following Reference 8 and the production method is described in another Reference 9 described below. (Known Example 8) Literature (US, Journal of Colloid and Int
erface Science, Vol. 134, No. 1. January (19
90), pp51-58) (known example 9) Literature (Surface, Vol. 29, No. 5, 199)
1 year, pp387-398, 5.2)

FIG. 1 shows that FIG. Alumina crosslinked clay porous body (Alumina Pi
FIG. 4 is a diagram showing heat of adsorption of the llared clay, wherein the horizontal axis represents the amount of adsorption and the vertical axis represents the heat of adsorption. FIG. 2 shows the ratio of the heat of adsorption to the heat of condensation of water using the relationship of FIG. 1. The horizontal axis indicates the amount of adsorption, and the vertical axis indicates the ratio of the heat of adsorption to the heat of condensation of water. From FIG. 2, it can be seen that the heat of adsorption of this material is at most 1.08 times the heat of condensation of water with respect to the heat of differential adsorption and, on average, has a characteristic substantially equal to the heat of condensation of water.

The effect when the desiccant having such a small heat of adsorption is used in the desiccant air conditioner shown in FIG. 16 will be described below. In the moisture adsorption process (states K to L, L ') on the wet psychrometric diagram of FIG. 18, when the heat of adsorption is equal to the heat of condensation of water (states K to L'), the following equation is established from the heat balance. . .DELTA.X.R = .DELTA.T.Cp Therefore, this process has a gradient of .SIGMA.X / .DELTA.T = Cp / R.SIGMA.Ci
(= 0.24 / 580 = 0.414 × 10 ⁻³ = constant). (Where R is the latent heat of condensation of water and Cp is the specific heat of air at constant pressure). On the other hand, when there is heat of adsorption (states K to
L) similarly has a gradient of ∂X / ∂T = Cp / H ≒ C
s (= constant) line segment (where H is heat of adsorption).
Incidentally, when the modified zeolite (the heat of adsorption is 1.28 times the heat of condensation of water) is used in FIG. 17 of JP-A-6-277440 of Known Example 1, X / ΔT = Cp / HΔCs = 0.24 /580/1.28=0.323×10 ⁻³ .

Here, the cooling effect will be compared. The indoor state of the treated air (state K) is dry bulb temperature Tr, absolute humidity X
r, and the dehumidification amount of the processing air is ΔX. Outside air having the same flow rate as the processing air is used as the regeneration air, the inlet conditions are dry bulb temperature To, the absolute humidity Xo, and the regeneration temperature is Tg.
These conditions are compared with each other with and without heat of adsorption. In the process of adsorption and dehumidification of the treated air, if there is no heat of adsorption, the temperature Tl 'after adsorption is: Tl' = Tr + ΔX / Ci (1) where ΔX is the absolute value of the humidity difference before and after dehumidification. 70 ° C
As described above, desiccant is used for relative humidity of 1
Since it can adsorb up to 0%, the indoor air condition is JIS-C9
Dry-bulb temperature 27 ° C, wet-bulb temperature 19 ° C specified in 612 etc.
If the relative humidity is 48% and the absolute humidity is 10.7 g / kg, the absolute humidity reached when the point where the enthalpy line passing through the state intersects with the relative humidity of 10% is obtained is about 5 g / kg. Therefore, the amount of water ΔX to be dehumidified is 5.7 g / kg.
Becomes Therefore, Tl ′ = 27 + 0.0057 / 0.00
0414 = 40.77 ° C. This process air exchanges heat with the outside air, and becomes the state M ^′ . State M 'temperature ^{of, Tm' = Tl '-ε (} Tl'-To) = (1-ε) Tl' + εTo = (1-ε) (Tr + ΔX / Ci) + εTo (2) where epsilon is the first 3 shows the temperature efficiency of the sensible heat exchanger. Therefore, assuming that the temperature efficiency of the first sensible heat exchanger is 80% and the outside air temperature is 30 ° C., Tm ′ = (1−0.80) 40.77
+ 0.8 × 30 = 32.15 ° C. Point L 'before cooling
Is a point on the same enthalpy line as the room, that is, ΔQ ′ = (Tl′−Tm ′) / Cp is obtained as the cooling effect. That is, ΔQ ′ = (40.77
-32.15) x 0.24 = 2.069 kcal / kg
Cooling effect is obtained.

On the other hand, when there is heat of adsorption, Tm = T1−ε (T1−To) = (1−ε) T1 + εTo = (1−ε) (Tr + ΔX / Cs) + εTo (3) Tm′−Tm = (1−ε) (1 / Ci−1 / Cs) ΔX = (1−ε) (Cs−Ci) ΔX / CiCs (4) Therefore, Tm′−Tm = (1−0.80) (0.323 × 10 ⁻³ −0.414 × 10 ⁻³ ) 5.7 × 10 ⁻³ /0.414×10 ⁻³ / 0.323 × 10 ⁻³ = −0.776 ° C. Therefore, the cooling effect is 0.776 × 0.24 = 0.186 kcal when there is heat of adsorption such as zeolite.
/ Kg. That is, the heat of adsorption is reduced by about 9% as compared with the case where the heat of condensation is equal to the heat of condensation of water. In other words, according to the present invention, the cooling effect is increased by 10% compared to the case where zeolite is used.

Next, as to the required heating amount of the regenerated air, the case where the heat of adsorption such as zeolite is present (when it is larger than the heat of condensation) and the case where it is not present (when it is equal to the heat of condensation) are compared.
As in the above, in FIG. 18, when there is no heat of adsorption,
In the state U ′, Tu ′ = Tg−ΔX / Ci = 70−0.0057 / 0.000414 = 56.23 ° C. (5) In the state R ′, Tr ′ = To + ε (Tl′−To) = (1− ε) To + εTl ′ = 0.2 × 30 + 0.8 × 40.77 = 38.62 (6) Since the state U ′ and the state R ′ exchange heat, the state S ′ is: Ts ′ = (1−ε) To + εTl '+ Ε' × [(Tg-ΔX / Ci)-(1-ε) To-εTl '] = (1-ε') (1-ε) To + ε '(Tg-ΔX / Ci) + ε (1-ε') ) Tl ′ (7) = 0.2 × 0.2 × 30 + 0.8 (70−0.0057 / 0.000414) + 0.8 × 0.2 × 40.77 = 52.70 ° C. where ε ′ Is the temperature efficiency of the second sensible heat exchanger. Accordingly, the heating amount ΔG ′ of the regeneration air is as follows: ΔG ′ = (Tg−Ts ′) × Cp = (70−52.70) × 0.24 = 4.152 kca
l / kg

Similarly, the state U when the heat of adsorption is large
Ts = (1−ε ′) (1−ε) To + ε ′ (Tg−ΔX / Cs) + ε (1−ε ′) Tl (8) In this case, the state S ′ or the higher the dry bulb temperature of S is higher However, since the regeneration heating amount is small, taking the difference between Ts ′ and Ts, Ts′−Ts = −ε ′ (ΔX / Ci−ΔX / Cs) + ε (1−ε ′) (Tl′− Tl) = − ε ′ (ΔX / Ci−ΔX / Cs) + ε (1−ε ′) [(Tr + ΔX / Ci) − (Tr + ΔX / Cs)] = ΔX (Ci−Cs) (ε′−ε + ε′ε) / CsCi (9) = 0.0057 × (0.000414-0.000323) (0.8−0.8 + 0.8 × 0.8) /0.000323/0.000414=2.48° C. The amount of heating when the heat is large is 2.48 ×
0.24 = 0.595 kcal / kg. That is, about 14% of the case where the heat of adsorption is equal to the heat of condensation of water.
To increase. In other words, according to the present invention, the required heating amount is reduced by 13% as compared with the case where zeolite is used. When the two are compared in terms of energy efficiency, the difference is further increased.
According to the present invention, the operating coefficient is: COP ′ = ΔQ ′ / ΔG ′ = 2.069 / 4.152 =
0.4983 On the other hand, in the conventional case using a zeolite having a large heat of adsorption, COP = ΔQ / ΔG = (2.069−0.186) / (4.152 + 0.595) = 0.3967 According to this, the operation coefficient is improved by 25.6% as compared with the conventional example using zeolite.

On the other hand, the moisture absorption properties of the porous alumina cross-linked clay used in this example are introduced in Known Example 8 and are optimal for desiccant air conditioning. This will be described below with reference to the drawings. FIG. 3 shows the adsorption of a material obtained by exchanging exchangeable cations between layered silicate (montmorillonite) layers with a polynuclear metal hydroxide ion containing aluminum and heating and dehydrating the same at 200 ° C. The horizontal axis indicates the relative humidity, and the vertical axis indicates the relative amount of adsorption (relative moisture content) which defines the amount of adsorption as a denominator and the amount of adsorption as a numerator when the desiccant has a humidity of 90%. From this figure, 70 ° C
It can be seen that the relative moisture content equilibrated with the heated air having a relative humidity of 10% and the relative moisture content equilibrated with the treated air having a relative humidity of 50% is 0.66. The difference between the adsorption and desorption is 0.43, which is larger than the above-mentioned 0.378 when the conventional zeolite is used. Also,
The curve connecting both points is upwardly convex, and as described above, the differential coefficient dP / dX indicating the ratio of the relative humidity change ΔP to the adsorption / desorption change ΔX is small. Since the water vapor pressure does not easily increase, the driving force for adsorption is maintained, and the adsorption speed can be increased, which is advantageous.

FIG. 4 shows that the exchangeable cation between the layered silicate (montmorillonite) layers described in Known Example 8 was exchanged with a polynuclear metal hydroxide ion containing aluminum, and this was heated and dehydrated at 300 ° C. Material isotherm,
The horizontal axis indicates the relative humidity, and the vertical axis indicates the relative adsorption amount (relative moisture content) which defines the adsorption amount as a numerator with the adsorption amount at a humidity of 90% of each desiccant as a denominator. From this figure, 7
The relative moisture content equilibrated with the regeneration air heated to 0 ° C. and the relative humidity of 10% is 0.27, and the relative moisture content equilibrated with the treated air having the relative humidity of 50% is 0.73. The difference in adsorption and desorption is 0.46, which exceeds the above-mentioned 0.378 when the conventional zeolite is used. Further, the curve connecting both points is upwardly convex, and as described above, the relative humidity variation ΔX with respect to the adsorption / desorption variation ΔX.
Since the differential coefficient dP / dX indicating the ratio of P is small and the water vapor pressure does not easily rise even when moisture is adsorbed, the driving force for adsorption is maintained and the adsorption speed can be increased, which is advantageous.

FIG. 5 shows that the exchangeable cation between the layered silicate (montmorillonite) layers described in Known Example 8 was exchanged with a polynuclear metal hydroxide ion containing aluminum, which was heated and dehydrated at 400 ° C. Material isotherm,
The horizontal axis indicates the relative humidity, and the vertical axis indicates the relative adsorption amount (relative moisture content) which defines the adsorption amount as a numerator with the adsorption amount at a humidity of 90% of each desiccant as a denominator. From this figure, 7
The relative moisture content equilibrated with the regeneration air heated to 0 ° C. and the relative humidity of 10% is 0.18, and the relative moisture content equilibrated with the treated air having the relative humidity of 50% is 0.78. It can be seen that the difference in adsorption and desorption is 0.60, which exceeds 0.378 when the conventional zeolite is used. Further, the curve connecting both points is upwardly convex, and as described above, the relative humidity variation ΔX with respect to the adsorption / desorption variation ΔX.
Since the differential coefficient dP / dX indicating the ratio of P is small and the water vapor pressure does not easily rise even when moisture is adsorbed, the driving force for adsorption is maintained and the adsorption speed can be increased, which is advantageous.

FIG. 6 shows that the exchangeable cations between the layered silicate (montmorillonite) layers described in Known Example 8 were exchanged with aluminum-containing polynuclear metal hydroxide ions, which were heated and dehydrated at 600 ° C. Material isotherm,
The horizontal axis indicates the relative humidity, and the vertical axis indicates the relative adsorption amount (relative moisture content) which defines the adsorption amount as a numerator with the adsorption amount at a humidity of 90% of each desiccant as a denominator. From this figure, 7
Relative moisture content equilibrated with 10% relative regeneration air heated to 0 ° C. is 0.19, and relative moisture content equilibrated with 50% relative humidity treated air is 0.73. The difference between the adsorption and desorption is 0.54, which exceeds the above-mentioned 0.378 when the conventional zeolite is used. Further, the curve connecting both points is substantially convex upward, and as described above, the differential coefficient dP / dX indicating the ratio of the change ΔP in the relative humidity to the change ΔX in the amount of adsorption and desorption is small, and the water adsorbs. However, since the water vapor pressure does not easily increase, the driving force for adsorption is maintained, and the adsorption speed can be increased, which is advantageous.

FIG. 7 shows that the exchangeable cation between the layered silicate (montmorillonite) layers described in Known Example 8 was exchanged with a polynuclear metal hydroxide ion containing aluminum, and this was heated and dehydrated at 300 ° C. The horizontal axis is relative humidity, and the vertical axis is relative adsorption amount (relative moisture) which defines the adsorption amount as a numerator and the adsorption amount as a numerator when the adsorption isotherm of the material is measured at the time of desorption. Content). From this figure, it can be seen that the relative humidity 1 heated to 70 ° C.
The relative moisture content, which is in equilibrium with 0% regeneration air, is 0.25
It can be seen that the relative moisture content equilibrated with the treated air having a relative humidity of 50% is 0.82, and the difference in adsorption and desorption is 0.57, which is the above-mentioned value when the conventional zeolite is used. Exceeds 0.378. The curve connecting both points is upwardly convex, and as described above, the derivative dP / d represents the ratio of the change ΔP in the relative humidity to the change ΔX in the amount of adsorption and desorption.
Since dX is small and the water vapor pressure does not easily rise even when moisture is adsorbed, the driving force for adsorption is maintained and the adsorption speed can be increased, which is advantageous.

As shown in FIGS. 3 to 7, the desiccant of this embodiment has a characteristic that a large difference in adsorption and desorption can be obtained and the adsorption speed can be maintained high irrespective of the heating and dehydrating treatment temperature. Therefore, in desiccant air conditioning, since a large amount of water can be treated with a small amount of desiccant, only a compact desiccant rotor is required, and the air conditioner can be made compact. As described above, the exchangeable cation between the layered silicate layers is converted to a polynuclear metal hydroxide ion containing aluminum by using montmorillonite having a sodium group as an exchangeable cation as the layered silicate of the first embodiment. By exchanging and heating and dehydrating the porous alumina-crosslinked clay body to be used as a desiccant, it is possible to provide a compact air conditioner having a large cooling effect, excellent energy saving, and a small size, as compared with the conventional example. it can.

In this example, montmorillonite was used as the layered silicate, and exchangeable cations between layers were exchanged with polynuclear metal hydroxide ions containing aluminum.
This was shown as an example in which a porous alumina-crosslinked clay that had been heated and dehydrated was used as a desiccant, but the layered silicate is not limited to montmorillonite, but has a similar swelling property of 2: 1.
Using a natural or synthetic smectite such as hectorite, beidellite, or saponite as a clay mineral having a layered structure, exchangeable cations between layered silicate layers are exchanged with polynuclear metal hydroxide ions containing aluminum and heated. What was dehydrated and made into an alumina crosslinked clay porous body may be used as a desiccant.

The second embodiment of the present invention is a dehumidifying air-conditioning apparatus in which structural activated carbon (SAC) obtained by carbonizing polyvinyl formal and activating at a temperature of 850 ° C. or less is used as a desiccant. The hygroscopic property and the production method of this type of structured activated carbon are introduced in the following Reference 10 and the production method is disclosed in another Reference 11 described below. (Known Example 10) Literature (Chemical Engineering Transactions, Vol. 15, No. 1)
No. 1989, pp. 38-43) (Known Example 11) Literature (Chemical Engineering Transactions, Vol. 10, No. 5)
No. 1984, pp. 574-579) It is described on page 40 of the document of known example 10 that, on average, the heat of adsorption of this material is approximately 1.02 times the heat of condensation of water. Therefore, in the same manner as in the first embodiment, the gradient of the moisture adsorption process is as follows: ∂X / ∂T ≒ Ci = 0.24 / 580 / 1.02 = 0.
It becomes 406 × 10 ^-3 . On the other hand, FIG. 17 of JP-A-6-277440 of Known Example 1 shows that the modified zeolite (the heat of adsorption is 1.28 of the heat of condensation of water).
In the case of using (times), X / ΔT = Cp / HΔCs = 0.24 / 580 / 1.28 = 0.323 × 10 ⁻³ as in the first embodiment.

Here, the cooling effect will be compared. Calculation is performed under the same conditions as in the first embodiment, and the amount of water ΔX to be dehumidified is 5.7 g / kg. Therefore, Tl ′ = 27 + 0.0057 / 0.000406 = 4
1.04 ° C. This processing air exchanges heat with the outside air, and becomes the state M '. From the equation (2), the temperature of the state M ′ is given by: Tm ′ = (1−0.80) 41.04 + 0.8 × 30 =
32.21 ° C. In the calculation of the cooling effect, since the state L 'is not on the same enthalpy line as the room air because there is a little heat of adsorption in this embodiment, the temperature of the state L' in the first embodiment is used. That is, ΔQ ′ = (40.77−32.22) × 0.24 = 2.
A cooling effect of 054 kcal / kg is obtained. On the other hand, when there is heat of adsorption,
Referring to the first example, ΔQ = 2.069−0.186 = 1.883 kcal /
A cooling effect of kg is obtained. Therefore, the cooling effect is reduced by about 8% as compared with the case where the heat of adsorption is 1.02 times the heat of condensation of water. In other words, according to the present invention, the cooling effect is increased by 9% as compared with the case where zeolite is used.

Next, regarding the required heating amount of the regeneration air, the case of zeolite having a large heat of adsorption (case of 1.28 times the heat of condensation) and the case of the present embodiment (case of 1.02 times heat of condensation) ). In FIG. 18 as above,
When the heat of adsorption is small, the state U ′ is calculated from the above equation (5) by Tu ′ = Tg−ΔX / Ci = 70−0.0057 / 0.000406 = 55.96
From the equation (6), the state R ′ is given by: Tr ′ = To + ε (Tl′−To) = (1−ε) To + εTl ′ = 0.2 × 30 + 0.8 × 41.04 = 38.83 ° C. State U ′ And the state R ′ exchanges heat, the state S ′ becomes (7)
From the formula, Ts ′ = (1−ε ′) (1−ε) To + ε ′ (Tg−ΔX / Ci) + ε (1−ε ′) Tl ′ = 0.2 × 0.2 × 30 + 0.8 (70− 0.0057 / 0.000406) + 0.8 × 0.2 × 41.04 = 52.54 ° C. Therefore, the heating amount ΔG ′ of the regeneration air is ΔG ′ = (Tg−Ts ′) × Cp = (70− 52.54) × 0.24 = 4.190 kca
l / kg

Similarly, the heating amount Δ when the heat of adsorption is large
G is ΔG = 4.152 + with reference to the first embodiment.
Since 0.595 = 4.747 kcal / kg, the amount of heat in the case of zeolite having an adsorption heat of 1.28 times the heat of condensation of water is calculated as follows. It is increased by about 13% as compared with the embodiment. In other words, according to the present invention, the required heating amount is reduced by 12% as compared with the case where zeolite is used. When the two are compared in terms of energy efficiency, the difference is further increased. According to the present invention, the operating coefficient is: COP ′ = ΔQ ′ / ΔG ′ = 2.054 / 4.190 =
0.4902 On the other hand, in the case of the conventional case where the zeolite having a large heat of adsorption is used, referring to the first embodiment, COP = ΔQ / ΔG = 0.3967 Therefore, according to the present invention, the conventional example using the zeolite Operating coefficient is improved by 23.6%.

On the other hand, the hygroscopic property of the structural activated carbon (SAC) used in this embodiment is introduced in the known example 10 and is optimal for desiccant air conditioning. This will be described below with reference to the drawings. FIG. 8 is described in Known Example 10.
It is an adsorption isotherm of a material obtained by low activation of structural activated carbon (SAC) at 800 ° C. for 1.5 hours,
The horizontal axis indicates the relative humidity, and the vertical axis indicates the relative adsorption amount (relative moisture content) which defines the adsorption amount as a numerator with the adsorption amount at a humidity of 90% of each desiccant as a denominator. Open circles indicate desorption characteristics, and black circles indicate adsorption characteristics. From this figure, the relative moisture content equilibrated with the regeneration air heated to 70 ° C. and the relative humidity of 10% is 0.04, and the relative moisture content equilibrated with the treated air having the relative humidity of 50% is 0.1%. 70 to 0.75, and the difference in adsorption and desorption was 0.66 to 0.71, which was 0.37 when the conventional zeolite was used.
8 is much more advantageous. Further, the maximum adsorption amount of the present material is as large as 40%, which is 1.7 times higher than the maximum adsorption amount (23%) of zeolite (4A) described in Known Example 12.
This is more advantageous because it is twice as large. In addition, although the curve connecting both points is a gentle S-shape, it can be approximated as a substantially linear characteristic, so that an adsorption driving force similar to silica gel is obtained, and the performance is significantly improved compared to conventional wood-based activated carbon. . (Publication Example 12) Literature (Practical Design of Dehumidification for Air Conditioning Engineers, Kyoritsu Shuppan, 1980), Chapter 4, page 152, Figure 4.1b
Describes that the maximum water adsorption of zeolite 4A is 23%.

FIG. 9 shows the low activation (Activity) of structural activated carbon (SAC) described in Known Example 10 at 850 ° C. for 1 hour.
vation) is the adsorption isotherm of the material, the horizontal axis is the relative humidity, and the vertical axis is the relative adsorption amount (relative amount) that defines the adsorption amount as a numerator with the adsorption amount at 90% humidity of each desiccant as the denominator. (Moisture content). Open circles indicate desorption characteristics, and black circles indicate adsorption characteristics. From this figure, the relative moisture content equilibrated with the regeneration air heated to 70 ° C. and the relative humidity of 10% is 0.03, and the relative moisture content equilibrated with the treated air having the relative humidity of 50% is 0.1%. 77 to 0.79, and the difference between adsorption and desorption was 0.74 to 0.76, which was 0.378 when the conventional zeolite was used.
Is significantly more advantageous. Further, the maximum adsorption amount of the present material is as large as 30%, which is more advantageous because it is 1.7 times larger than the maximum adsorption amount (23%) of zeolite (4A) described in Known Example 12. In addition, although the curve connecting both points is a gentle S-shape, it can be approximated as a substantially linear characteristic, so that an adsorption driving force similar to silica gel is obtained, and the performance is significantly improved compared to conventional wood-based activated carbon. .

FIG. 10 describes a known example 10.
It is the adsorption isotherm of the material before activating the activated carbon (SAC). The horizontal axis is relative humidity, and the vertical axis is the amount of adsorption at 90% humidity of each desiccant as the denominator, and the amount of adsorption is the numerator. The relative adsorption amount (relative moisture content) to be defined is shown. From this figure, it can be seen that the relative humidity 1 heated to 70 ° C.
The water content equilibrated with 0% regeneration air was 0.03, the relative moisture content equilibrated with 50% relative humidity treated air was 0.70, and the difference between adsorption and desorption was 0%. .6
7, which is significantly higher than the above-mentioned 0.378 when the conventional zeolite is used, and is advantageous. Further, although the maximum adsorption amount of this material is 20%, it is not much different from the maximum adsorption amount (23%) of zeolite (4A) described in Known Example 12, so that the material before activation is used. But the advantage remains.

As shown in FIGS. 8 to 10, the desiccant of this embodiment is activated at 850 ° C. or lower.
If it is temperature, regardless of the activation temperature, the difference between adsorption and desorption can be large, and it has the property of keeping the adsorption rate high, so in desiccant air conditioning, a large amount of water can be treated with a small amount of desiccant. Therefore, only a compact desiccant rotor is required, and the air conditioner can be made compact. As described above, the structural activated carbon (SAC) obtained by carbonizing polyvinyl formal, which is the second embodiment, and activating the same at a temperature of 850 ° C. or less is used as a desiccant. It is possible to provide a compact air conditioner that has a large cooling effect, is excellent in energy saving, and is compact.

FIG. 11 shows the adsorption isotherms of the desiccant material shown in FIGS. 3 to 10 collectively. The horizontal axis indicates the relative humidity, and the vertical axis indicates the amount of adsorption of each desiccant at 90% humidity in the denominator. And the relative amount of adsorption (relative moisture content) defining the amount of adsorption as a molecule. As shown in this figure, the desiccants of the present invention all have a relative adsorption amount of X, a relative humidity of P, and an isotherm separation factor of R in the range of 30% to 70% relative humidity.
Assuming that an XP curve obtained as an isotherm separation factor R = 0.2 using a function represented by an equation X = P / (R + P−RP · P) and an isotherm separation factor R = 2.5 It exists in the range surrounded by the obtained XP curve. here,
When the difference between adsorption and desorption when the isotherm separation factor R = 0.2, which is a hypothetical adsorption characteristic, is determined using the above function, the moisture content that is equilibrated with the regeneration air heated to 70 ° C. and 10% relative humidity is obtained. The ratio is 0.357, and the relative moisture content that is equilibrated with the processing air at a relative humidity of 50% is 0.833. Advantageously, it greatly exceeds 0.378 when zeolite is used.

Next, as a similar desiccant having an effect common to the first embodiment and the second embodiment, as described in claim 1 of the present invention, the maximum value of the heat of differential adsorption is determined by the condensation of water. The effect of the desiccant that is 1.1 times or less the heat will be described with reference to a calculation example. In this calculation, assuming that the heat of adsorption is the highest, the average value of the heat of adsorption is assumed to be 1.1 times the heat of condensation of water, and a comparison with the zeolite of Known Example 1 is performed. In the same manner as in the first embodiment, the gradient of the moisture adsorption process is as follows: ∂X / ∂T ≒ Ci = 0.24 / 580 / 1.1 = 0.3
It becomes 76 × 10 ^-3 . On the other hand, FIG. 17 of JP-A-6-277440 of Known Example 1 shows the modified zeolite (the heat of adsorption is 1.28 of the heat of condensation of water).
In the case of using (times), X / ΔT = Cp / HΔCs = 0.24 / 580 / 1.28 = 0.323 × 10 ⁻³ as in the first embodiment.

Here, the cooling effect will be compared. Calculation is performed under the same conditions as in the first embodiment, and the amount of water ΔX to be dehumidified is 5.7 g / kg. Therefore, Tl ′ = 27 + 0.0057 / 0.000376 = 4
2.16 ° C. This processing air exchanges heat with the outside air, and becomes the state M '. From the equation (2), the temperature of the state M ′ is given by: Tm ′ = (1−0.80) 42.16 + 0.8 × 30 =
32.43 ° C. In the calculation of the cooling effect, since the state L 'is not on the same enthalpy line as the room air because there is a little heat of adsorption in this embodiment, the temperature of the state L' in the first embodiment is used. That is, ΔQ ′ = (40.77−32.43) × 0.24 = 2.
A cooling effect of 002 kcal / kg is obtained. On the other hand, when there is heat of adsorption,
Referring to the first example, ΔQ = 2.069−0.186 = 1.883 kcal /
A cooling effect of kg is obtained. Therefore, the cooling effect is reduced by about 6% compared to a case where the heat of adsorption is 1.1 times the heat of condensation of water. In other words, according to the present invention, the cooling effect is increased by 6% as compared with the case where zeolite is used.

Next, regarding the required heating amount of the regenerated air, the case of zeolite having a large heat of adsorption (1.28 times the heat of condensation) and the case of the present embodiment (1.1 times the heat of condensation) are small. ). As in the above, in FIG. 18, when the heat of adsorption is small, the state U ′ is calculated from the above equation (5) by Tu ′ = Tg−Δ × / Ci = 70−0.0057 / 0.000376 = 54.84
From the equation (6), the state R ′ is given by: Tr ′ = To + ε (Tl′−To) = (1−ε) To + εTl ′ = 0.2 × 30 + 0.8 × 42.16 = 39.73 ° C. And the state R ′ exchanges heat, the state S ′ becomes (7)
From the equation, Ts ′ = (1−ε ′) (1−ε) To + ε ′ (Tg−ΔX / Ci) + ε (1−ε ′) Tl ′ = 0.2 × 0.2 × 30 + 0.8 (70− 0.0057 / 0.000376) + 0.8 × 0.2 × 42.16 = 51.82 ° C. Therefore, the heating amount ΔG ′ of the regeneration air is ΔG ′ = (Tg−T
s') * Cp = (70-51.82) * 0.24 = 4.363 kc
al / kg

Similarly, the heating amount Δ when the heat of adsorption is large.
G is ΔG = 4.152 + with reference to the first embodiment.
Since 0.595 = 4.747 kcal / kg, the amount of heating in the case of zeolite whose heat of adsorption is 1.28 times the heat of condensation of water is equal to the amount of heat which is 1.1 times the heat of condensation of water. It is increased by about 9% as compared with the embodiment. In other words, according to the present invention, the required heating amount is reduced by 8% as compared with the case where zeolite is used. When the two are compared in terms of energy efficiency, the difference is further increased. According to the present invention, the operating coefficient is: COP ′ = ΔQ ′ / ΔG ′ = 2.002 / 4.363 =
0.4589 On the other hand, in the conventional case using a zeolite having a large heat of adsorption, referring to the first embodiment, COP = ΔQ / ΔG = 0.3967 Therefore, according to the present invention, the operating coefficient is 15. 7% improvement. Thus, as described in claim 1 of the present invention,
By using a desiccant in which the maximum value of the heat of differential adsorption is 1.1 times or less the heat of condensation of water, the cooling effect is greatly increased and a high energy saving effect is obtained. In a third embodiment of the present invention, as described in Known Example 13 below, as a desiccant, an alumina hydrate (for example, aluminum hydroxide, boehmite, pseudo-boehmite, etc.) and phosphoric acid are used as a heat-dissociable template. Aluminum phosphate (molecular sieve, for example, UnionPOWER and the so-called AlPO ₄ in Union Carbide and academic societies) obtained by reacting with an agent (eg, an organic base such as tripropylamine).
-5). The present inventors have developed a porous aluminum phosphate (molecular sieve, commonly called A).
LPO ₄ -5) was synthesized and measured adsorption properties and heat of adsorption with the following results. (Known Example 13) Literature (Journal of American Chemical S
ociety. Vol. 104, pp. 1146-1147, 19
(1982) titled “Aluminophosphate Molecular Sieve
s: A New Class of Microporous Crystalline Inorgani
As “c Solid”, the name classification of this type of porous aluminum phosphate (molecular sieve) is described.

FIG. 12 is a graph showing the measured heat of adsorption of porous aluminum phosphate (molecular sieve). The horizontal axis indicates the amount of adsorption and the vertical axis indicates the heat of adsorption. FIG.
Is the ratio of the heat of adsorption when adsorbing water of 20% or more of the maximum amount of adsorption to the heat of condensation of water using the relationship in FIG. 12, where the horizontal axis represents the amount of adsorption and the vertical axis represents the water of adsorption heat. Shows the ratio of heat of condensation to heat of condensation. From FIG. 13, it can be seen that the heat of adsorption of this material has a differential heat of adsorption of 0.97 to 1.08 times the heat of condensation of water, and on average is approximately 1.05 times the heat of condensation of water.

The effect when the desiccant having such a small heat of adsorption is used in the desiccant air conditioner shown in FIG. 5 will be described below. In the moisture adsorption process (states K to L, L ') on the wet psychrometric chart of Fig. 7, when the heat of adsorption is 1.05 times smaller than the heat of condensation of water (states K to L'), the heat balance is not obtained. The following equation holds. ΔX · (Rx1.05) = ΔT · Cp Therefore, this process has a gradient of {X / ΔT = Cp / R / 1.
05 ≒ Ci (= 0.24 / 580 / 1.05 = 0.39
4 × 10 ⁻³ = constant) (where R is the latent heat of condensation of water and Cp is the specific heat of air at constant pressure).

On the other hand, when the heat of adsorption is further large (states K to L), the gradient is similarly set to ΔX / ΔT = Cp / H
It is indicated by a line segment of ≒ Cs (= constant) (where H is the heat of adsorption). Incidentally, FIG. 17 of JP-A-6-277440 of Known Example 1 shows that the modified zeolite (the heat of adsorption is 1.2 times the heat of condensation of water).
When 8 times the zeolite) is used, X / ΔT = Cp / HΔCs = 0.24 / 580 / 1.28 = 0.323 × 10 ⁻³ .

Here, the cooling effect will be compared. The indoor state of the treated air (state K) is dry bulb temperature Tr, absolute humidity X
r, and the dehumidification amount of the processing air is ΔX. Outside air having the same flow rate as the processing air is used as the regeneration air, the inlet conditions are dry bulb temperature To, the absolute humidity Xo, and the regeneration temperature is Tg.
These conditions are compared with each other with and without heat of adsorption. In the process of adsorption and dehumidification of treated air, if the heat of adsorption is as small as 1.05 times, the temperature Tl 'after adsorption is Tl' = Tr + ΔX / Ci (1)

Here, ΔX is the absolute value of the humidity difference before and after dehumidification. In the case of regeneration at 70 ° C., as described above, desiccant can be adsorbed up to a relative humidity of 10%, so that indoor air conditions are a dry bulb temperature of 27 ° C. and a wet bulb temperature of 19 ° C. (relative humidity of 48%) specified in JIS-C9612 and the like. , Absolute humidity 10.7g /
kg), the gradient X / ΔT = 0.39 passing through the state
When the point at which the line of 4 × 10 ⁻³ intersects with the relative humidity of 10% is obtained, the absolute humidity reached is about 5 g / kg. Therefore, the amount of water ΔX to be dehumidified is 5.7 g / kg. Therefore, Tl ′ = 27 + 0.0057 / 0.000394 = 4
1.47 ° C.

This process air exchanges heat with the outside air, and the state M ′
Becomes The temperature of the state M ′ is as follows: Tm ′ = Tl′−ε (Tl′−To) = (1−ε) Tl ′ + εTo = (1−ε) (Tr + ΔX / Ci) + εTo (2) where ε is the first 3 shows the temperature efficiency of the sensible heat exchanger. Therefore, assuming that the temperature efficiency of the first sensible heat exchanger is 80% and the outside air temperature is 30 ° C., Tm ′ = (1−0.80) 41.47.
+ 0.8 × 30 = 32.29 ° C. Point L 'before cooling
Is higher than the point on the same enthalpy line as the room, and the temperature of the point on the same enthalpy line as the room is 41.4.
7-0.0057 / 0.000394 × (1.05-
1.00) = 40.77 ° C., that is, when molecular sieve is used, the cooling effect is ΔQ ′ = (40.77−32.29) × 0.24 = 2.035 kcal / kg. The effect is obtained.

On the other hand, when the heat of adsorption is large, Tm = T1−ε (T1−To) = (1−ε) T1 + εTo = (1−ε) (Tr + ΔX / Cs) + εTo (3) Tm′−Tm = (1−ε) (1 / Ci−1 / Cs) ΔX = (1−ε) (Cs−Ci) ΔX / CiCs (4) Therefore, when zeolite is used, Tm′−Tm = (1−0.80) (0.323 × 10 ⁻³ −0.394 × 10 ⁻³ ) 5.7 × 10 ⁻³ / 0 .394 × 10 ⁻³ /0.323×10 ⁻³ = −0.636 ° C. Therefore, the cooling effect is 0.636 × 0.24 = 0.153 kc when the heat of adsorption is large like zeolite.
al / kg is smaller than when molecular sieves are used. That is, it is reduced by about 7.5% as compared with the case where the molecular sieve of the present invention is used. In other words, according to the present invention, the cooling effect is increased by 8.1% as compared with the case where zeolite is used.

Next, regarding the required heating amount of the regeneration air, when the heat of adsorption is large like zeolite (1.2 of the heat of condensation).
The case where the heat of adsorption is small (equal to 1.05 times the heat of condensation) such as molecular sieve is compared. In FIG. 7 as described above, when the heat of adsorption is small, the state U ′ is Tu ′ = Tg−ΔX / Ci = 70−0.0057 / 0.000394 = 55.53 ° C. (5) The state R ′ is Tr ′ = To + ε (T1′−To) = (1−ε) To + εT1 ′ = 0.2 × 30 + 0.8 × 41.47 = 39.18 (6) Since the state U ′ and the state R ′ exchange heat. , State S ′ is: Ts ′ = (1−ε) To + εT1 ′ + ε ′ [(Tg−ΔX / Ci) − (1−ε) To−εT1 ′] = (1−ε ′) (1−ε) To + ε '(Tg−ΔX / Ci) + ε (1−ε ′) Tl ′ (7) = 0.2 × 0.2 × 30 + 0.8 (70−0.0057 / 0.000394) + 0.8 × 0.2 × 41.47 = 52.26 ° C. Here, ε ′ is the temperature efficiency of the second sensible heat exchanger.

Accordingly, the heating amount ΔG ′ of the regeneration air is as follows: ΔG ′ = (Tg−Ts ′) × Cp = (70−52.26) × 0.24 = 4.258 kcal / kg Similarly, the heat of adsorption is large. In the case (1.28 times the heat of condensation), the state U is as follows: Ts = (1−ε ′) (1−ε) To + ε ′ (Tg−ΔX / Cs) + ε (1−ε ′) Tl (8) In this case, the higher the dry bulb temperature of the state S ′ or S, the smaller the regeneration heating amount. Therefore, if the difference between Ts ′ and Ts is calculated, Ts′−Ts = −ε ′ (ΔX / Ci− ΔX / Cs) + ε (1−ε ′) (Tl′−T1) = − ε ′ (ΔX / Ci−ΔX / Cs) + ε (1−ε ′) [(Tr + ΔX / Ci) − (Tr + ΔX / Cs)] = ΔX (Ci−Cs) (ε′−ε + ε′ε) / CsCi (9) = 0.0057 × (0.000394-0.000323) × (0.8−0.8 + 0) 8 × 0.8) /0.000323 /0.000394 = 2.04 ℃ Therefore, heating amount when the adsorption heat is high, 2.04 ×
0.24 = 0.490 kcal / kg.
That is, it is increased by about 11.5% as compared with the case where the heat of adsorption is equal to 1.05 times the heat of condensation of water. In other words, according to the present invention, the required heating amount is reduced by 10.3% as compared with the case where zeolite is used.

When the two are compared in terms of energy efficiency, the difference is further increased. According to the present invention, the operating coefficient is: COP ′ = ΔQ ′ / ΔG ′ = 2.035 / 4.258 =
0.4779 On the other hand, in the conventional case using a zeolite having a large heat of adsorption, COP = ΔQ / ΔG = (2.035−0.153) /
(4.258 + 0.490) = 0.3964 Therefore, according to the present invention, the operation coefficient is improved by 20.6% as compared with the conventional example using zeolite.

On the other hand, the moisture absorption characteristics of the porous aluminum phosphate (molecular sieve) used in the present example were confirmed by the inventors to be the most suitable for desiccant air conditioning. This will be described below with reference to the drawings. FIG.
Describes the reaction of alumina hydrate (eg, aluminum hydroxide, boehmite, pseudo-boehmite, etc.) measured by the inventor with phosphoric acid using a thermally dissociable template agent (eg, an organic base such as tripropylamine). Porous aluminum phosphate (molecular sieve, for example, Union Carbide Co. and a so-called Al
PO ₄ -5) is the adsorption isotherm, the horizontal axis is the relative humidity, and the vertical axis is the relative adsorption amount (relative moisture content) that defines the adsorption amount as a numerator with the adsorption amount at a humidity of 90% of each desiccant as a denominator. ). From this figure, the relative moisture content equilibrated with the regeneration air heated to 70 ° C. and 10% relative humidity is:
It was found that the relative moisture content in equilibrium with the treated air having a relative humidity of 50% was 0.81, and the difference in adsorption and desorption was 0.76, and the conventional zeolite was used. Greatly exceeds the above-mentioned 0.378. In particular, the curve from 20% to 50% relative humidity is upwardly convex, and as described above, the differential coefficient dP / dX indicating the ratio of the change ΔP in the relative humidity to the change ΔX in the amount of adsorption and desorption is small. In addition, since the water vapor pressure does not easily rise even when water is adsorbed, the driving force for adsorption is maintained, and the adsorbing speed can be increased, which is advantageous. In general, the heat of adsorption generated when adsorbing water is extremely large when the water content is extremely small. However, in the application of the present invention, the heat of adsorption is 20% or more of the maximum adsorbed amount, that is, the relative water content. 0.20 in content
If the heat of adsorption is low in the above region, the effects of the present invention can be exhibited.

As described above, the desiccant of this embodiment has a characteristic that a large difference in adsorption and desorption can be obtained and the adsorption speed can be maintained high even when the heating and dehydrating treatment temperature is low. Since a large amount of water can be treated with a small amount of desiccant, a compact desiccant rotor is sufficient, and the air conditioner can be made compact. As described above, the reaction mixture is obtained by reacting alumina hydrate (eg, aluminum hydroxide, boehmite, pseudo-boehmite, etc.) with phosphoric acid using a thermally dissociable template (eg, an organic base such as tripropylamine). Porous aluminum phosphate (molecular sieves, such as AlPO _{4 at} Union Carbide and academic societies)
By using -5) as a desiccant, it is possible to provide a compact air conditioner that has a greater cooling effect, is more energy efficient, and is smaller than the conventional example.

FIG. 15 shows another embodiment of the present invention.
This is a so-called hybrid type desiccant air conditioner in which a desiccant air conditioner and a heat pump as shown in FIG. 16 are combined, wherein the process air which has exchanged heat with the regenerated air after adsorbing moisture is cooled by a low heat source of the heat pump, and A dehumidifying air conditioner characterized by regenerating desiccant by heating regeneration air before regeneration with a high heat source of a heat pump. According to this type of hybrid desiccant air conditioner, it is possible to provide an air conditioner with even more energy saving. This will be described below with reference to the drawings.

In the embodiment shown in FIG. 15, a processing air path A, a regeneration air path B, a desiccant rotor 103, two sensible heat exchangers 104 and 121, and a heater (condenser) 220 using a high heat source of a heat pump. Using a cooler (evaporator) 240 using a low heat source, a compressor 260 of a heat pump, and a humidifier 105 as main components, the processing air was dehumidified by a desiccant rotor 103, and the temperature was raised by the heat of moisture adsorption of the desiccant. The process air is cooled by exchanging heat with the regeneration air in the first sensible heat exchanger 104, and is further cooled by the cooler 240.
After cooling in the humidifier and supplying it to the air-conditioned space, the regeneration air is taken in from the external space (OA),
The first sensible heat exchanger 104 exchanges heat with the processing air, and the second sensible heat exchanger 121 exchanges heat with the regenerated air after desiccant regeneration to raise the temperature. Heating to lower the relative humidity,
After passing through the desiccant rotor 103, the moisture in the desiccant rotor 103 is desorbed and regenerated, and the regenerated air after regeneration is heat-exchanged with the regenerated air before heating in the second sensible heat exchanger 121, and then to the outside (EX). It is configured to emit.

The operation is different from the conventional example of FIG. 16 only in that the cooling operation by the cooler 240 is added, and therefore detailed description is omitted, and the energy saving effect will be described below. Here, the desiccant rotor 103 uses montmorillonite having a sodium group as an exchangeable cation as the same layered silicate as in the first embodiment, and exchanges the exchangeable cation between the layered silicate layers with polynuclear metal water containing aluminum. It is exchanged with an oxide ion, and this is heated and dehydrated to obtain an alumina crosslinked clay porous body. That is, the heat of adsorption of the desiccant is equal to the heat of condensation of water.

The heat pump used in this type of hybrid desiccant air conditioner is constructed by heating the regenerating air temperature to 70 ° C. by using the method disclosed by the applicant as Japanese Patent Application No. 9-90242. C. is required, and the temperature lift is 50 C. Therefore, the normally obtained coefficient of operation (COP) is about 3.0. Therefore, if the input energy of the compressor is 1, the heater 22
At 0, 4.0 heat is released. In the first embodiment, the heating amount ΔG ′ of S ′ to T in FIG. 18 is as follows: ΔG ′ = (40.77−32.15) × 0.24 = 2.
Since it is 069 kcal / kg, in the cooler 240 in FIG. 15, q = ΔG ′ × COP / (COP + 1) = 4.152 × 3.0 / 4.0 = 3.114 kcal /
A cooling effect of kg is obtained. The temperature of the treated air after cooling is: Tm'-q / Cp = 32.15-3.114 / 0.24
= 19.18 ° C (above the evaporation temperature). Therefore, the total cooling effect is: ΔQ ′ + q = 2.069 + 3.114 = 5.183 kc
al / kg. On the other hand, the drive energy of the heat pump is: W = ΔG ′ / (COP + 1) = 4.152 / 4 = 1.0
Since it is 38 kcal / kg, the total COP of this air conditioner is: COP = (ΔQ ′ + q) /W=5.183/1.038
= 4.993. Normally, the COP of an air conditioner using a vapor compression refrigeration cycle for general air conditioning is about 3, and according to this embodiment, an energy saving effect of 40% can be obtained.

Next, the third rotor 103 is used as the desiccant rotor 103.
Reaction of the same alumina hydrate (for example, aluminum hydroxide, boehmite, pseudo-boehmite, etc.) with phosphoric acid using a heat-dissociable template agent (for example, an organic base such as tripropylamine) as in the above Examples. The resulting porous aluminum phosphate (molecular sieve, for example, AlPO ₄ −
5) shall be used. That is, the heat of adsorption of the desiccant is equal to 1.05 times the heat of condensation of water as described above.

As in the previous example, the heat pump uses the method disclosed by the present applicant as Japanese Patent Application No. 9-90242. When the temperature of the regenerating air is heated to 70 ° C., the evaporation temperature is required to be 15 ° C., the condensing temperature is required to be about 65 ° C., and the temperature lift is 50 ° C. Therefore, the normally obtained operating coefficient (C
OP) is about 3.0. Therefore, assuming that the input energy of the compressor is 1, the heater 220 releases 4.0 heat.

In the third embodiment, S ′ in FIG.
Since the heating amount ΔG ′ of ＴT is ΔG ′ = (Tg−Ts ′) × Cp = (70−52.26) × 0.24 = 4.258 kcal / kg, the cooler 240 in FIG. A cooling effect of q = ΔG ′ × COP / (COP + 1) = 4.258 × 3.0 / 4.0 = 3.194 kcal / kg is obtained. The temperature of the treated air after cooling is Tm'-q / Cp = 32.29-3.194 / 0.24 = 18.98.degree. C. (above the evaporation temperature). Therefore, the total cooling effect is: ΔQ ′ + q = 2.035 + 3.194 = 5.229 kc
al / kg.

On the other hand, the driving energy of the heat pump is as follows: W = ΔG ′ / (COP + 1) = 4.258 / 4 = 1.
Since it is 065 kcal / kg, the total COP of this air conditioner is as follows: COP = (ΔQ ′ + q) /W=5.229/1.065=4.910 Usually, the COP of an air conditioner using a vapor compression refrigeration cycle for general air conditioning is about 3, and according to this embodiment, an energy saving effect of 39% can be obtained.

Next, when the operating coefficient (COP) when the zeolite of the known example 1 is used as the desiccant is calculated, FIG.
In the cooler 240 shown in FIG. 15, q = ΔG × COP / (COP + 1) = 4. Since the heating amount ΔG of S to T of No. 8 is ΔG = 4.747 kcal / kg from the first embodiment, A cooling effect of 747 × 3.0 / 4.0 = 3.560 kcal / kg is obtained. The temperature of the treated air after cooling is Tm−q / Cp = 32.15 + 0.776−3.560 / 0.24 = 18.09 ° C. (above the evaporation temperature). Therefore, the total cooling effect is ΔQ + q = 2.069−0.186 + 3.560 = 5.443 kcal / kg.

On the other hand, the driving energy of the heat pump is as follows: W = ΔG / (COP + 1) = 4.747 / 4 = 1.18
Since it is 7 kcal / kg, the total COP of this air conditioner is: COP = (ΔQ ′ + q) /W=5.443/1.18
7 = 4.586. Therefore, in this case, the air conditioner using the vapor compression refrigeration cycle for conventional general air conditioning is 35%
However, a heat pump having a lower capacity than the effect of the present invention and having a large capacity is required.

[0081]

As described above, according to the present invention, there is no deliquescence, the maximum value of the differential heat of adsorption is 1.1 times or less the heat of condensation of water, and the adsorption characteristic indicated by the adsorption isotherm. By using a desiccant having an appropriate isothermal adsorption characteristic at a regeneration temperature of 65 to 75 ° C., an air conditioner is configured,
Since the loss of the cooling effect due to the heat of adsorption and the amount of heating required for regeneration of the regeneration air are reduced and the difference in the amount of moisture adsorption due to desiccant adsorption and desorption can be used significantly, the air conditioner can be used at a relatively low temperature compared to the past. It is possible to provide a compact dehumidifying air conditioner that can be driven by a heat source, has a large cooling effect, saves energy, and is compact.

[Brief description of the drawings]

FIG. 1 is a diagram showing the heat of adsorption of a porous alumina-crosslinked clay described in a known example.

FIG. 2 is a diagram showing the heat of adsorption as a ratio to the heat of condensation of water using the relationship of FIG.

FIG. 3 is a view showing a relative adsorption amount (relative water content) of a desiccant described in a known example.

FIG. 4 is a view showing a relative adsorption amount (relative water content) of a desiccant described in a known example.

FIG. 5 is a view showing a relative adsorption amount (relative moisture content) of a desiccant described in a known example.

FIG. 6 is a view showing a relative adsorption amount (relative moisture content) of a desiccant described in a known example.

FIG. 7 is a view showing a relative adsorption amount (relative water content) of a desiccant described in a known example.

FIG. 8 is a view showing a relative adsorption amount (relative water content) of a desiccant described in a known example.

FIG. 9 is a diagram showing a relative adsorption amount (relative water content) of a desiccant described in a known example.

FIG. 10 is a view showing a relative adsorption amount (relative water content) of a desiccant described in a known example.

FIG. 11 is a view collectively displaying the adsorption isotherms of the desiccant material shown in FIGS.

FIG. 12 is a diagram showing heat of adsorption of porous aluminum phosphate (molecular sieve).

FIG. 13 is a diagram showing heat of adsorption as a ratio of heat of condensation of water using the relationship of FIG.

FIG. 14 is a diagram showing an adsorption isotherm of porous aluminum phosphate (molecular sieve).

FIG. 15 is a diagram showing another embodiment of the present invention.

FIG. 16 is a diagram showing a conventional technique.

FIG. 17 is a diagram showing a conventional zeolite adsorption isotherm.

18 is a diagram showing a cycle of desiccant air conditioning having the device configuration shown in FIG. 16 on a psychrometric chart.

FIG. 19 is a diagram showing a typical adsorption isotherm of activated carbon.

[Explanation of symbols]

 103 Desiccant rotor 220 Heater 240 Cooler A Processing air path B Regeneration air path

Claims (10)

[Claims] 1. A path of treated air in which moisture is adsorbed by a desiccant and a path of regenerated air which is heated by a heating source, passes through the desiccant after adsorbing the moisture, desorbs and regenerates moisture in the desiccant. In a dehumidifying air conditioner having a heat exchanger between the treated air having moisture adsorbed and the regenerated air before desiccant regeneration and before being heated by the heating source, the desiccant has no deliquescence and maximum adsorption Quantity 2
The maximum value of the differential heat of adsorption when adsorbing water of 0% or more is 1.1 times or less the heat of condensation of water, and the adsorption isotherm indicating the desiccant adsorption characteristic is in the range of 30% to 70% relative humidity. In the equation, the maximum adsorption amount at a relative humidity of 90% is defined as a denominator, the adsorption amount is defined as a numerator, the relative adsorption amount is defined as X, the relative humidity is defined as P, and the isotherm separation factor is defined as R.
R · P), the isotherm separation factor R
Dehumidifying air conditioning characterized by using a desiccant existing in a range surrounded by an XP curve obtained as = 0.2 and an XP curve obtained as an isotherm separation factor R = 2.5. apparatus. 2. The dehumidifying air conditioner according to claim 1, wherein an alumina crosslinked clay porous body is used as the desiccant. 3. The alumina-crosslinked clay porous body is obtained by exchanging exchangeable cations between layered silicate layers with aluminum-containing polynuclear metal hydroxide ions and subjecting the exchanged cations to heat dehydration. Item 3. A dehumidifying air conditioner according to item 2. 4. The dehumidifying air conditioner according to claim 3, wherein the layered silicate is a natural or synthetic smectite. 5. The dehumidifying air conditioner according to claim 1, wherein structural activated carbon is used as the desiccant. 6. The dehumidifying air conditioner according to claim 5, wherein the structural activated carbon is obtained by carbonizing polyvinyl formal and activating the same at a temperature of 850 ° C. or less. 7. The dehumidifying air-conditioning apparatus according to claim 1, wherein porous aluminum phosphate (molecular sieve) is used as the desiccant. 8. The method according to claim 7, wherein the porous aluminum phosphate (molecular sieve) is a substance obtained by reacting alumina hydrate with phosphoric acid using a thermally dissociable template. Dehumidifying air conditioner. 9. The dehumidifying air conditioner according to claim 1, wherein the desiccant is regenerated by heating the regenerated air to 75 ° C. or less. 10. The method according to claim 9, wherein the processing air which has exchanged heat with the regeneration air after adsorbing moisture is cooled by a low heat source of the heat pump, and the regeneration air before desiccant regeneration is heated by a high heat source of the heat pump. The dehumidifying air conditioner as described.