CN100464133C - Adsorption heat pump and use of the adsorption material as adsorption material for the adsorption heat pump - Google Patents

Abstract

By increasing the moisture adsorption capacity difference between the adsorption and desorption of the adsorbent, and regenerating (desorbing) the adsorbent at low temperature, it is possible to provide an adsorption heat pump that efficiently adsorbs/desorbs water vapor using a heat source at a lower temperature than conventional ones. The present invention resides in an adsorption heat pump, in which an adsorption/desorption section having an adsorbate, an adsorption material with the adsorbed/desorbed substance, an evaporating section connected to the adsorption/desorption section for evaporation of the adsorbed substance, and the adsorption/desorption section connected to the adsorption/desorption section On the adsorption heat pump of the condensation part of the condensation part of the adsorbate, the adsorption material has a relative vapor pressure change of 0.15 in the range of relative vapor pressure above 0.05 and below 0.30 on the water vapor adsorption isotherm measured at 25 °C Adsorbent materials in the relative vapor pressure region where the water adsorption capacity changes over 0.18g/g.

Description

Adsorption heat pump and use of the adsorption material as adsorption material for the adsorption heat pump

This application is a divisional application of a Chinese patent application with an application date of February 20, 2002, an application number of 02805332.X, and an invention title of "Adsorption Heat Pump and Adsorption Material as Adsorption Material for Adsorption Heat Pump".

technical field

The present invention relates to an adsorption heat pump using a specific adsorption material and to the use of the specific adsorption material as an adsorption material for the adsorption heat pump.

Background technique

In an adsorption heat pump, in order to regenerate the adsorbent that has adsorbed the adsorbate, such as water, the adsorbent is heated to desorb the adsorbate, the dried adsorbent is cooled to the temperature used for the adsorption of the adsorbate, and used again Adsorption of adsorbate.

Absorption heat pumps that use relatively high-temperature (above 120°C) waste heat and thermal energy as regeneration heat sources for adsorption materials have been put into practical use. However, because the heat obtained by cogeneration devices, fuel cells, cooling water of automobile engines, or solar heat is generally below 100°C, which is a relatively low temperature, it cannot be used to drive absorption heat pumps that are currently in practical use. As for the heat source, it is necessary to seek effective utilization of low-temperature heat of 100°C or even lower 60°C to 80°C. Among them, the practical use in automobiles that generate a large amount of waste heat is also being sought as much as possible.

Even though the principle of operation of the adsorption heat pump is the same, the adsorption characteristics required for the adsorbent are greatly different depending on the temperature of the available heat source. For example, the waste heat temperature of a gas engine cogeneration process or solid polymer fuel cell used as a heat source on the high temperature side is 60°C to 80°C, and the cooling water temperature of an automobile engine is 85°C to 90°C. Furthermore, the temperature of the heat source on the cooling side also varies depending on the installation location of the device. For example, in the case of automobiles, it is the temperature obtained by heat exchangers, and in buildings and houses, it is the temperature of water cooling towers and river water. That is, the operating temperature range of the adsorption heat pump is 25°C to 35°C on the low temperature side and 60°C to 80°C on the high temperature side when it is installed in a building, etc., and 30°C to 45°C on the low temperature side and It is about 85°C to 90°C. Thus, in order to effectively utilize waste heat, a device that can be driven even if the temperature difference between the low-temperature side heat source and the high-temperature side heat source is small, and an adsorbent suitable for the device are desired.

In addition, zeolite 13X and silica gel A type are known as representative adsorbents for adsorption heat pumps.

Also, recently, the micelle structure of the surfactant has been studied as a cast-synthesized mesoporous (medium) pore molecular sieve (FSM-10, etc.) (JP-9-178292) or as a desiccant material collectively referred to as AlPO ₄ Porous Zeolites such as aluminum phosphate-based molecular sieves (JP-P-11-197439).

In addition, it has been introduced that the temperature dependence of the adsorption properties of the adsorption material for adsorption heat pumps is important [Chemical Engineering Papers, Vol. SG3 (Fuji Silysia Co., Ltd.) that has a temperature dependence and SG1 (the same company) that does not show a large temperature dependence.

Furthermore, the dependence of the adsorption performance of AlPO ₄ -5 as a porous aluminum phosphate-based molecular sieve on temperature was introduced, and the adsorption performance at 25°C and 30°C was specifically shown [Colloid PolymSci 277(1999) p83-88]. Also introduced the temperature dependence of AlPO ₄ -5, and recorded the adsorption isotherms under the adsorption process of 20°C, 25°C, 30°C, 35°C, and 40°C (the 16th Zeolite Research Conference Lecture Preliminary Collection p91; November 21, 22, 2012).

As an adsorption material for adsorption heat pumps, the use of various adsorption materials has been studied. According to our research, in order to be suitable for a device that can be driven even if the temperature difference between the low-temperature side heat source and the high-temperature side heat source is small, in terms of adsorption performance There is still room for improvement.

Contents of the invention

In order for the device to operate adequately even at relatively high temperatures around the adsorbent, it is necessary to adsorb the adsorbate at a low relative vapor pressure, and to miniaturize the device by designing the adsorbent to be used in a small amount. The adsorption/desorption capacity is large. Furthermore, in order to utilize a low-temperature heat source for the desorption of the adsorbate (regeneration of the adsorbent), the desorption temperature must be low. That is, as an adsorption material for adsorption heat pumps, it is important to (1) adsorb the adsorbate at a low relative vapor pressure (adsorbable at high temperature), (2) have a large amount of adsorption/desorption, and (3) work at a high relative vapor pressure Adsorbent material that desorbs the adsorbate (desorbable at low temperature).

An object of the present invention is to provide a high-efficiency adsorption heat pump using an adsorbent capable of adsorbing/desorbing an adsorbate in a low relative vapor pressure region.

Also, the present invention provides the use of an adsorbent capable of adsorbing/desorbing an adsorbate in a region of low relative vapor pressure as an adsorbent for an adsorption heat pump.

Also, the present invention provides an adsorption heat pump having practically efficient adsorption performance.

The present invention provides an adsorption heat pump comprising (a) an adsorbate, (b) an adsorption/desorption section having an adsorption material for adsorbing/desorbing the adsorbate, (c) a an evaporation section for performing evaporation of the adsorbate, and (d) a condensation section connected to the adsorption/desorption section for performing condensation of the adsorbate;

in,

(1) The adsorption material contains a zeolite comprising aluminum and phosphorus in its framework structure;

(2) The adsorbent is a water vapor adsorbent having a relative vapor pressure φ2b of not less than 0.115 and not more than 0.18 during the adsorption operation of the adsorption/desorption unit, and a relative vapor pressure φ1b of at least 0.18 during the desorption operation of the adsorption/desorption unit. The region of 0.1 to 0.14 has a range in which the difference in the adsorption amount of the adsorbent obtained by the following formula is 0.15 g/g or more:

Adsorption amount difference = Q2-Q1,

In the formula,

Q1 = The adsorption amount at φ1b obtained from the water vapor desorption isotherm measured from the desorption operation temperature (T3) of the adsorption/desorption part,

Q2 = The adsorption amount at φ2b obtained from the water vapor adsorption isotherm measured from the adsorption operation temperature (T4) of the adsorption/desorption part,

and

φ1b (relative vapor pressure during desorption operation of the adsorption/desorption part) = [equilibrium water vapor pressure at the refrigerant temperature (T2) cooling the condenser] / [heating medium temperature (T1) heating the adsorption/desorption part Under the equilibrium water vapor pressure],

φ2b (relative vapor pressure during adsorption operation of the adsorption/desorption part) = [equilibrium vapor pressure at the refrigeration temperature (T0) generated by the evaporator part] / [equilibrium vapor at the refrigerant temperature (T2) cooling the adsorption/desorption part pressure],

(However, let T0=5-10°C, T1=T3=90°C, T2=T4=40-45°C).

The present invention also provides the use of a water vapor adsorbent (1) containing zeolite containing aluminum and phosphorus in its skeleton structure, (2) relatively In the region where the vapor pressure φ2 is 0.115 to 0.18 and the relative vapor pressure φ1 is 0.1 to 0.14 during the desorption operation of the adsorption/desorption part, the difference in the adsorption amount of the adsorbent obtained by the following formula is in the range of 0.15 g/g or more :

Adsorption amount difference = Q2-Q1,

In the formula,

Q1 = The adsorption amount at φ1 obtained from the water vapor desorption isotherm measured at the desorption operation temperature (T3) of the adsorption/desorption part,

Q2 = The adsorption amount at φ2 obtained from the water vapor adsorption isotherm measured at the adsorption operation temperature (T4) of the adsorption/desorption section,

and

φ1 (relative vapor pressure during desorption operation of the adsorption/desorption part) = [equilibrium water vapor pressure at the refrigerant temperature (T2) cooling the condenser] / [heating medium temperature (T1) heating the adsorption/desorption part Under the equilibrium water vapor pressure],

φ2 (relative vapor pressure during adsorption operation of the adsorption/desorption part) = [equilibrium vapor pressure at the refrigeration temperature (T0) generated by the evaporator part] / [equilibrium vapor at the refrigerant temperature (T2) cooling the adsorption/desorption part pressure],

(However, let T0=5-10°C, T1=T3=90°C, T2=T4=40-45°C).

The present invention also provides a vehicle air conditioner using the above-mentioned adsorption heat pump.

The present invention also provides a method for using an adsorbent, which includes heating the adsorbent with the adsorbate to desorb the adsorbate, cooling the dried adsorbent to a temperature for the adsorption of the adsorbate, and reusing the adsorbate The adsorption of substances is characterized in that: (1) the adsorption material contains zeolite containing aluminum and phosphorus in the framework structure, (2) the adsorption material is a water vapor adsorption material, and the relative vapor pressure is In the region where φ2b is 0.115 to 0.18 and the relative vapor pressure φ1b is 0.1 to 0.14 during the desorption operation of the adsorption/desorption part, there is a range in which the difference in the adsorption amount of the adsorbent obtained by the following formula is 0.15 g/g or more:

Adsorption amount difference = Q2-Q1,

in,

Q1 = The adsorption amount at φ1b obtained from the water vapor desorption isotherm measured at the desorption operating temperature (T3) of the adsorption/desorption part,

Q2 = The adsorption amount at φ2b obtained from the water vapor adsorption isotherm measured at the adsorption operation temperature (T4) of the adsorption/desorption section,

and

φ1b (relative vapor pressure during desorption operation of the adsorption/desorption part) = [equilibrium water vapor pressure at the refrigerant temperature (T2) cooling the condenser] / [heating medium temperature (T1) heating the adsorption/desorption part Under the equilibrium water vapor pressure],

φ2b (relative vapor pressure during adsorption operation of the adsorption/desorption part) = [equilibrium vapor pressure at the refrigeration temperature (T0) generated by the evaporator / cooling the adsorption] / [equilibrium vapor at the refrigerant temperature (T2) of the desorption part pressure],

(However, let T0=5-10°C, T1=T3=90°C, T2=T4=40-45°C).

Description of drawings

Fig. 1 is a conceptual diagram of an adsorption heat pump.

Fig. 2 is a water vapor adsorption isotherm (25° C.) of SAPO-34 (manufactured by UOP LLC) of Example 1.

3 is a measurement record of ²⁹ Si-MAS-NMR spectrum of SAPO-34 (manufactured by UOP LLC) in Example 1. FIG.

FIG. 4 is the water vapor adsorption isotherm (25° C.) of the zeolite of Example 2. FIG.

Fig. 5 is the Si-MAS-NMR spectrum measurement record of zeolite ²⁹ in Example 2.

FIG. 6 is the water vapor adsorption isotherm (25° C.) of the zeolite of Example 3. FIG.

7 is a water vapor adsorption isotherm of SAPO-34 (manufactured by UOP LLC) in Example 4 in the adsorption process at 40°C and the desorption process at 90°C.

8 is a water vapor adsorption isotherm of SAPO-34 (manufactured by UOP LLC) in Example 4 in the adsorption process at 45°C and the desorption process at 90°C.

Fig. 9 is a water vapor adsorption isotherm (25°C) of the zeolite of the reference example.

Fig. 10 is a record of ²⁹ Si-MAS-NMR spectrum measurement of the zeolite of the reference example.

11 is the water vapor adsorption isotherm (25° C.) of the silica gel type A of Comparative Example 2. FIG.

12 is the ALPO-5 water vapor adsorption isotherm (30°C) of Comparative Example 3.

In addition, in the figure, 1 is an adsorption tower, 2 is an adsorption tower, 3 is an adsorbate piping, 4 is an evaporator, 5 is a condenser, 11 is a heating medium piping, 111 is a cooling water inlet, and 112 is a cooling water inlet. Water outlet, 113 is hot water inlet, 114 is hot water outlet, 115 is switching valve, 116 is switching valve, 21 is heating medium piping, 211 is cooling water inlet, 212 is cooling water outlet, 213 is hot water inlet, 214 is a hot water outlet, 215 is a switching valve, 216 is a switching valve, 30 is an adsorbed substance piping, 31 is a control valve, 32 is a control valve, 33 is a control valve, 34 is a control valve, 300 is an indoor unit, 301 is a In the pump, 41 is a cold water pipe (inlet), 42 is a cold water pipe (outlet), 51 is a cooling water pipe (inlet), and 52 is a cooling water pipe (outlet).

Detailed ways

The present invention will be described in more detail below.

<Structure of Adsorption Pump>

First, the structure of the adsorption heat pump will be described by taking the adsorption heat pump shown in FIG. 1 as an example.

The adsorption heat pump is mainly composed of the following parts: the adsorbed substance, the adsorption material filled with the adsorbed substance and the adsorption/desorption part (adsorption tower 1 And 2. Hereinafter, the adsorption/desorption part is sometimes called an adsorption tower), the refrigeration (cooling capacity) obtained by the evaporation of the adsorbate is taken out from the external evaporation part (evaporator 4), and the refrigeration (cooling capacity) obtained by the condensation of the adsorbate is taken out. The heat energy is released from the external condensation section (condenser 5).

The evaporator 4 seals a refrigerant (water in this embodiment) while maintaining a substantially vacuum inside, and a heat exchanger 43 is provided in the evaporator 4 for connecting the indoor unit 300 and the The air blown out of the room is heat-exchanged with the heat medium (in this embodiment, a fluid mixed with glycol-based antifreeze fluid in water) and the refrigerant.

The adsorption towers 1 and 2 have heat exchangers bonded and filled with adsorbent on the interior surface, and the condenser 5 has a built-in heat exchanger 53, which is used to make the vapor refrigerant ( Water vapor) is cooled and condensed by a heat carrier cooled by external air, etc.

The adsorption towers 1 and 2 filled with the adsorbent are connected to each other by the adsorbate piping 30 , and the adsorbate piping 30 is provided with control valves 31 to 34 . In addition, the adsorbate exists in the adsorbate piping as vapor of the adsorbate, liquid of the adsorbate, and a mixture with vapor.

The evaporator 4 and the condenser 5 are connected to the adsorbate piping 30 . The adsorption towers 1 and 2 are connected in parallel between the evaporator 4 and the condenser 5, and the adsorbate (condensed water suitable for regeneration) that is condensed in the condenser is set between the condenser 5 and the evaporator 4 to return to the evaporator 4 return pipe 3. In addition, reference numeral 41 is an inlet of cold water used for outputting cooling from the evaporator 4 , and reference numeral 51 is an inlet of cooling water to the condenser 5 . Symbols 42 and 52 are cold water and cooling water outlets, respectively. Furthermore, the indoor unit 300 for exchanging heat with the indoor space (air-conditioned space) and the pump 301 for circulating cooling water are connected to the cold water pipes 41 and 42 .

The heating medium piping 11 is connected to the adsorption tower 1, and the heating medium piping 21 is connected to the adsorption tower 2, respectively. The switching valves 115 and 116 and 215 and 216 are provided on the heating medium piping 11 and 21, respectively. In addition, the heating medium pipes 11 and 21 respectively flow a heating medium serving as a heating source or a cooling source for heating or cooling the adsorption materials in the adsorption towers 1 and 2 . The heating medium is not particularly limited, as long as it can effectively heat and cool the adsorption material in the adsorption tower.

Hot water is introduced from the inlet 113 and/or 213 by opening and closing switching valves (3-way valves) 115, 116, 215 and 216, passes through each adsorption tower 1 and/or 2, and is exported from the outlet 114 and/or 214. Cooling water is also introduced from the inlet 111 and/or 211 by opening and closing the switching valves 115 , 116 , 215 and 216 , passes through each adsorber 1 and/or 2 , and is led out from the outlet 112 and/or 212 .

Also, on the refrigerant pipes connecting the evaporator 4 and the adsorption towers 1 and 2 and the refrigerant pipes connecting the condenser 5 and the adsorption towers 1 and 2, control valves 31 to 34 for opening and closing the respective refrigerant pipes are respectively provided. The control valves 31-34, the pump 301 for circulating the heating medium, and the 3-way valves 115, 116, 215, and 216 for controlling the flow of the heating medium are controlled by an electronic control device (not shown).

Furthermore, an outdoor unit arranged to exchange heat with outside air, a heat source for generating hot water, and a pump for circulating the heating medium are connected to the heating medium pipes 11 and/or 21 (none of which are shown in the figure). The heat source is not particularly limited, and examples include cogeneration processes such as automobile engines, gas engines, and gas turbines, and fuel cells. In addition, when used in automobiles, automobile engines and automobile fuel cells are ideally used. An example of a heat source.

<Overview of Adsorption Heat Pump Operation Principle>

Next, an outline of the operation of the air conditioner (adsorption heat pump) of this embodiment will be described. By operating the pump 301, the heating medium circulates between the indoor unit 300 and the evaporator 4, evaporates the liquid refrigerant (suitable for water) in the evaporator 4 to cool the heating medium, and cools the air blown into the room. At the same time, switch the control valves 31-34 and the 3-way valves 115, 116, 215, 216 to make any one of the two adsorption towers 1 and 2 perform the adsorption process, and the other adsorption tower perform the detachment process (recycling process).

Specifically, when the first adsorption tower 1 is set as the adsorption process and the second adsorption tower 2 is set as the detachment process, the control valve 31 is opened, and the control valve 33 is closed, and in this state, the 3-way valve 115 is communicated. The cooling water inlet 111 side, connect the 3-way valve 116 to the cooling water outlet 112 side, at the same time, close the control valve 32, and open the control valve 34, in this state, connect the 3-way valve 215 to the hot water inlet 213 side, connect the 3 The through valve 216 communicates with the hot water outlet 214 side.

In this way, the refrigerant (water vapor) evaporated in the evaporator 4 flows into the adsorption material adsorbed therein in the first adsorption tower 1, and the temperature of the adsorption material is kept equivalent to the temperature of the outside air by cooling water from the inlet 111.

On the other hand, on the 2nd adsorption tower 2, since the hot water heated by the heat source (the engine is used when being used for vehicles) is provided by the hot water inlet 213, the adsorbent material in the 2nd adsorption tower 2 is released during the adsorption process. adsorbed refrigerant. And the released refrigerant (water vapor) is cooled and condensed again in the condenser 5 .

After a predetermined period of time, by switching the control valves 31 to 34 and the 3-way valves 115, 116, 215, and 216, the first adsorption tower 1 can be switched to the detachment process, and the second adsorption tower 2 can be switched to the adsorption process. By repeating such switching every predetermined time, continuous cooling operation can be performed.

<adsorbent material>

One of the features of the present invention resides in the adsorbent material used in the adsorbent heat pump.

<Absorptive material—1>

The adsorption material of the present invention has a relative vapor pressure of 0.05 to 0.30 on the water vapor adsorption isotherm measured at 25°C, and has a water adsorption amount change of 0.18 g/g or more when the relative vapor pressure changes by 0.15, Adsorbent materials in the relative vapor pressure region above 0.2g/g are preferred. It is preferably an adsorbent having a water adsorption capacity change of 0.18 g/g or more, most preferably 0.2 g/g or more, in the range of 0.05 to 0.20.

The adsorbate is adsorbed on the adsorbent as vapor, but the adsorbent is ideally a material whose adsorption amount of the adsorbate varies greatly within a narrow relative vapor pressure range. The reason is that if the adsorption amount of the adsorbate changes greatly in a narrow relative vapor pressure range, the amount of adsorbent material necessary to obtain the same adsorption amount under the same conditions will decrease, even if the temperature difference between the cooling heat source and the heating heat source Small can also drive adsorption heat pumps.

Next, the reason why the adsorbent material preferably has the above-mentioned properties can be understood from the following studies.

First of all, the operating vapor pressure range of the adsorption heat pump is determined by the relative vapor pressure of the desorption side (φ1a) and the relative vapor pressure of the adsorption side (φ2a), and φ1 and φ2 can be calculated using the following formula, and the operable relationship between φ1a and φ2a relative vapor pressure range.

Desorption side relative vapor pressure (φ1a) = equilibrium vapor pressure (Tlow1) / equilibrium vapor pressure (Thigh)

Adsorption side relative vapor pressure (φ2a) = equilibrium vapor pressure (Tcool)/equilibrium vapor pressure (Tlow2)

Here, the meanings of the symbols are as follows:

Thigh (high temperature heat source temperature): the temperature of the heat carrier heated when the adsorbate is desorbed from the adsorbent and the adsorbent is regenerated

Tlow1 (low temperature heat source temperature): The temperature of the adsorbed substance in the condensation part

Tlow2 (low temperature heat source temperature): The temperature of the heat carrier that is cooled while using the regenerated adsorbent material for adsorption

Tcool (refrigeration generation temperature): The temperature of the adsorbate in the evaporator is the temperature of the generated refrigeration

In addition, the equilibrium vapor pressure can be obtained from the temperature using the equilibrium vapor pressure curve of the adsorbate.

Hereinafter, the operating vapor pressure range when the adsorbate is water is exemplified. When the temperature of the high temperature heat source is 80°C and the temperature of the low temperature heat source is 30°C, the operating vapor pressure range (φ1a～φ2a) is 0.09～0.29. Similarly, when the temperature of the high temperature heat source is 60°C and the temperature of the low temperature heat source is 30°C, the operating relative vapor pressure range (φ1a～φ2a) is 0.21～0.29. Also, if it is estimated from the description in JP-A-2000-140625 that the exhaust heat of the automobile engine is used to drive the adsorption heat pump, the temperature of the high-temperature heat source is about 90°C and the temperature of the low-temperature heat source is 30°C. At this time, the relative vapor pressure range (φ1a～ φ2a) is 0.06 to 0.29.

According to the above analysis, when using the gas engine cogeneration process, solid polymer fuel cell or automobile engine waste heat to drive the adsorption heat pump, it can be considered that the operating relative vapor pressure range (φ1a～φ2a) is 0.05～0.30, preferably 0.06～0.29 . That is, a material with a large change in the adsorption amount in this operating humidity range is preferable. Therefore, a material with a large change in the adsorption capacity is usually in the range of relative vapor pressure of 0.05 to 0.30, preferably in the range of 0.06 to 0.29.

For example, assume a case where a refrigeration capacity of 3.0 kw (=10,800 kJ/hr) is obtained by an adsorption heat pump. Here, 3.0kw is the cooling capacity of an air conditioner used in a general car air conditioner. The capacity of the adsorption heat pump can be considered to be at least 15 liters or less according to the investigation of engine rooms of various vehicles.

"Adsorption difference"

Next, the weight of the adsorbent that can be filled in a capacity of 15 liters or less is obtained.

The components that should be installed in the engine room include the adsorption tower body, evaporator, condenser, and control valves. It is necessary to design these generally integrated components to a capacity of less than 15 liters. According to our research, it is considered that the volume of the evaporator, condenser and control valves can be formed at about 4.5 liters. Therefore, the capacity of the adsorption tower body is approximately 10.5 liters or less. Because the filling rate of the adsorbent in the adsorption tower and the bulk density of the adsorbent are usually about 30% and 0.6kg/liter respectively, so the adsorbent weight (W) that can be filled is 10.5×30%×0.6=1.89kg about.

The properties required of the adsorbent will be described below.

The refrigeration capacity R of the adsorption heat pump is represented by the following formula A.

R=(W·ΔQ·ηc·ΔH/τ)·η _h ... (Formula A)

Here, W is the weight of the adsorbent filled in one adsorption tower (one side); ΔQ is the amplitude of the equilibrium adsorption amount in the conditions of adsorption and detachment——the above-mentioned adsorption amount difference (Q2-Q1); η _c is the adsorption The amplitude efficiency represents the ratio of the actual adsorption amplitude within the switching time of the relative equilibrium adsorption amount amplitude ΔQ; ΔH is the latent heat of evaporation of water; _τ is the switching time between the adsorption process and the detachment process; The heat loss of the heater due to the temperature change between the hot water temperature and the cooling water temperature.

R is 3kw as mentioned above, and W is 1.89kg/2=0.95kg. In addition, according to our past research, τ is approximately 60 sec, and the values of ΔH, _ηc , and _ηh can be approximately 2500kJ/kg, 0.6, and 0.85 respectively. Therefore, if ΔQ is calculated according to (Formula A), then ΔQ=R /W/η _c /ΔH·τ/η _h = 3.0/0.95/0.6/2500·60/0.85 = 0.149kg/kg

That is, as an adsorbent used in an adsorption heat pump for automobiles, ΔQ is at least 0.15 g/g, preferably at least 0.18 g/g, more preferably at least 0.20 g/g.

Although the above description is based on the premise that it is used in automobiles, it goes without saying that it can be suitably applied to other applications such as stationary use as long as the above-mentioned characteristics are satisfied.

Based on the above studies, the adsorption material used in the adsorption heat pump of the present invention can be determined.

)的最大吸附量约为0.30g/g。因此，如果本发明规定的相对蒸气压的下限0.05处的吸附量大于0.15g/g，则不可能得到0.18g/g的吸附量差。因此，在水蒸气吸附等温线上，相对蒸气压0.05处的吸附量要在0.15g/g以下，最好在0.12g/g以下，0.10g/g以下，理想的是0.07g/g以下，更理想的是0.05g/g以下。In addition, there are no particular limitations on adsorbents that have a difference in the amount of water adsorbed at a relative vapor pressure of 0.05 to 0.30 with a relative vapor pressure change of 0.15 or more of 0.18 g/g or more as long as this characteristic is satisfied, but promising materials are zeolites. Since zeolite is crystalline, the pore volume for adsorption depends on the framework density. 13X (framework density 12.7T/1000

) has a maximum adsorption capacity of about 0.30 g/g. Therefore, if the adsorption amount at the lower limit of 0.05 of the relative vapor pressure specified by the present invention is greater than 0.15 g/g, it is impossible to obtain a difference in adsorption amount of 0.18 g/g. Therefore, on the water vapor adsorption isotherm, the adsorption capacity at the relative vapor pressure of 0.05 should be below 0.15g/g, preferably below 0.12g/g, below 0.10g/g, ideally below 0.07g/g, More preferably, it is 0.05 g/g or less.

<Absorptive material—2>

Another feature of the adsorbent of the present invention is that the relative vapor pressure (φ2b) during the adsorption operation of the adsorption/desorption part is 0.115 to 0.18, and the relative vapor pressure (φ1b) during the desorption operation of the adsorption/desorption part is 0.1 or higher. In the region of 0.14 or less, there is a water vapor adsorbent in which the difference in the adsorption amount of the adsorbent obtained by the following formula is in the range of 0.15 g/g or more.

Adsorption amount difference = Q2-Q1

here,

Q1 = The adsorption amount at φ1b obtained from the water vapor desorption isotherm measured at the desorption operation temperature (T3) of the adsorption/desorption part

Q2 = The adsorption amount at φ2b obtained from the water vapor adsorption isotherm measured at the adsorption operation temperature (T4) of the adsorption/desorption section

and

φ1b (relative vapor pressure during desorption operation of the adsorption/desorption part) = equilibrium water vapor pressure at the refrigerant temperature (T2) cooling the condenser/equilibrium at the temperature (T1) of the heating medium heating the adsorption/desorption part water vapor pressure

φ2b (relative vapor pressure during adsorption operation of the adsorption/desorption part) = equilibrium vapor pressure at the refrigeration temperature (T0) generated by the evaporator/equilibrium vapor pressure at the refrigerant temperature (T2) that cools the adsorption/desorption part

(Here, T0=5 to 10°C, T1=T3=90°C, T2=T4=40 to 45).

The adsorption amount difference of the adsorbent of the present invention is particularly limited by the above formula, but a more desirable adsorbent is one specifically defined by any one of the following conditions (A) to (C).

(A) T0 is 10°C, T2 is 40°C

(B) T0 is 5°C, T2 is 40°C

(C) T0 is 10°C, T2 is 45°C

The performance of the adsorbent will be described below with reference to FIG. 1 as described above.

First, the case where the control valves 31 and 34 are closed and the control valves 32 and 34 are opened in FIG. 1 will be described.

In this case, the water vapor supplied from the evaporator 4 is adsorbed, and the adsorbent filled in the adsorption tower 2 generates heat. At this time, the adsorption tower 2 is cooled by the heat medium (for example, cooling water) flowing through the heat medium pipes 211 and 21 to remove heat. In addition, let the temperature of the heating medium (cooling water) supplied from the pipe 211 which cools the adsorption tower 2 (adsorption/desorption part) at this time be T2.

On the other hand, the temperature of the evaporator 4 is controlled according to the purpose of generating refrigeration. At this time, the relative vapor pressure φ2b on the suction side is defined by the following equation.

Adsorption side relative vapor pressure φ2b = equilibrium water vapor pressure (T0)/equilibrium water vapor pressure (T2)

Equilibrium water vapor pressure (T0): The equilibrium water vapor pressure at the temperature T0 of the evaporator 4

Equilibrium water vapor pressure (T2): The equilibrium water vapor pressure at the heat carrier temperature T2 of adsorption tower 2

On the other hand, while the adsorption tower 1 is in the desorption (regeneration) process, the adsorbent filled in the adsorption tower 1 is regenerated using a regeneration heat source (heating the temperature of the heat carrier in the adsorption/desorption part. This temperature is set as T1). The condenser 5 is cooled by cooling water supplied through the heating medium pipe 51 to condense water vapor. At this time, the relative vapor pressure φ1 on the desorption side is defined by the following equation.

Desorption side relative vapor pressure φ1b = equilibrium vapor pressure (T2)/equilibrium vapor pressure (T1)

Equilibrium vapor pressure (T2): the equilibrium vapor pressure at the temperature of the condenser 5 (=the equilibrium vapor pressure at the heat carrier temperature T2 of the adsorption tower 2)

Equilibrium vapor pressure (T1): The equilibrium vapor pressure at the regeneration heat source temperature (T1) of adsorption tower 1

What is important here is that the temperature at the time of adsorption of the adsorption tower is different from the temperature at the time of desorption (regeneration). Therefore, in the present invention, according to the desorption isotherm at the temperature of desorption and the adsorption isotherm at the temperature of adsorption, the difference in the amount of adsorption can be obtained, specifically using the following formula to calculate:

Adsorption amount difference = Q2-Q1

here,

Q1 = The adsorption amount at φ1b obtained from the water vapor desorption isotherm measured at the desorption operation temperature (T3) of the desorption section

Q2 = The adsorption amount at φ2b obtained from the water vapor adsorption isotherm measured at the adsorption operation temperature (T4) of the adsorption/desorption section

and

φ1b (relative vapor pressure during desorption operation of the adsorption/desorption part) = equilibrium water vapor pressure at the refrigerant temperature (T2) cooling the condenser/equilibrium at the temperature (T1) of the heating medium heating the adsorption/desorption part Vapor Pressure

φ2b (relative vapor pressure during adsorption operation of the adsorption/desorption part) = equilibrium vapor pressure at the refrigeration temperature (T0) generated by the evaporator/equilibrium vapor pressure at the refrigerant temperature (T2) that cools the adsorption/desorption part

(Here, T0=5 to 10°C, T1=T3=90°C, T2=T4=40 to 45°C).

The adsorption material of the present invention has an adsorption capacity difference obtained by the above formula of at least 0.15 g/g, preferably at least 0.18 g/g. Although the greater the difference in adsorption capacity, the better, but considering the available material sources that meet the required performance, it is usually below 0.50 g/g, in reality it is below 0.40 g/g, and even below 0.35 g/g.

In addition, the above-mentioned difference in adsorption amount is specifically, for example, under the conditions of (1) T0 being 10°C and T2 being 40°C, (2) T0 being 5°C and T2 being 40°C, or (3) T0 being 10°C. , T2 measured under the condition of 45 ° C, the difference in the amount of adsorption can also be 0.15 g/g or more.

The required adsorption amount difference of 0.15 g/g or more can be derived from the following analysis assuming that the adsorption heat pump is used in an automobile.

"Adsorption temperature, desorption temperature"

First, as described above, since the amount of adsorption depends on the temperature at the time of adsorption and the temperature at the time of desorption, the adsorption isotherm at the temperature at the time of adsorption and the desorption isotherm at the temperature at the time of desorption are obtained.

During adsorption, since the adsorption tower is cooled with cooling water in order to suppress heat generation caused by adsorption heat, the cooling water temperature (T2) is approximately the temperature during adsorption (T4). On the other hand, during desorption, the adsorption tower needs desorption heat, so the hot water temperature (T1) becomes the desorption temperature (T3).

However, the temperature of the heat medium in the adsorption heat pump is (1) hot water temperature, which is about 90°C because it is obtained by using engine cooling water; (2) cooling temperature, which is the temperature obtained by exchanging heat with outside air. It is roughly 40°C to 45°C; (3) The temperature of cold water necessary to make cold air is roughly 5 to 10°C. That is, the temperature of the cold water is approximately 5 to 10° C. on the assumption that a general vehicle in Japan is used. Also, the cooling temperature is about 40°C in Japan, and about 45°C in areas where the outside air temperature is high.

Therefore, the adsorption temperature (T4) is approximately 40°C to 45°C, and the desorption temperature (T3) is approximately 90°C.

In the present invention, the required adsorption temperature and desorption temperature are used as indicators for evaluating the performance of the adsorption material, and at least any one of the adsorption isotherms and the desorption temperature is satisfied according to the adsorption isotherms obtained at an adsorption temperature of 40° C. to 45° C. The desorption isotherm obtained at 90°C is a condition under which the difference in the amount of adsorption obtained by the above formula is 0.15 g/g or more.

"Adsorption difference"

The above-mentioned adsorption amount difference (0.15 g/g or more) was obtained in the same manner as in the adsorption material-1.

Although the above description is based on the premise that it is used in automobiles, it goes without saying that it can be suitably applied to other applications such as stationary use if the above-mentioned characteristics are satisfied.

In addition, the above-mentioned difference in the amount of adsorption of the present invention satisfies the relative vapor pressure φ2b in the range of 0.15 to 0.18 during the adsorption operation of the adsorption/desorption unit, and the relative vapor pressure φ1b in the range of 0.1 to 0.14 during the desorption operation of the adsorption/desorption unit. of. This range roughly corresponds to the operating relative vapor pressure range of an adsorption heat pump.

In addition, when φ1b and φ2b are in the range of 0.115 to 0.18, and φ1b is greater than or equal to φ2b, when the difference in the adsorption amount reaches 0.15g/g or more, even in the severe situation that it was previously considered impossible to start as an adsorption heat pump It is also conducive to operation under certain temperature conditions.

In addition, the above-mentioned adsorbent-2 is selected from zeolites containing at least aluminum and phosphorus in their skeleton structure.

<Material of adsorption material>

The adsorption material of the present invention is preferably a zeolite, especially a zeolite containing aluminum, phosphorus and heteroatoms in the framework structure. The zeolite mentioned here may be a natural zeolite or an artificial zeolite. For example, if it is an artificial zeolite, it includes aluminosilicates and aluminophosphates specified by the International Zeolite Association (International Zeolite Association IZA).

Here, even among aluminophosphates, ALPO ₄ -5 is not suitable as the adsorption material of the present invention because of its hydrophobic adsorption properties. As the adsorbent of the present invention, it is preferable to replace a part of aluminum and phosphorus with silicon, lithium, magnesium, titanium, zirconium, vanadium, chromium, manganese, iron, cobalt, nickel, and palladium for proper use and hydrophilicity. , copper, zinc, gallium, germanium, arsenic, tin, calcium or boron and other heteroatoms.

Among them, a zeolite in which a part of aluminum or phosphorus is substituted with silicon, magnesium, titanium, zirconium, iron, cobalt, zinc, gallium, or boron is preferable, and a zeolite in which silicon is substituted is most preferable, which is generally called SAPO. In addition, these substituted heteroatoms may be of two or more types.

Among the zeolites used as the adsorbent in the present invention, the aluminophosphate is a zeolite containing aluminum, phosphorus and heteroatoms in the framework structure, and preferably has the following formulas (1), (2) and (3) Indicates the proportion of atoms present.

0.001≤x≤0.3 ...(1)

(In the formula, x represents the molar ratio of heteroatoms to the sum of aluminum and phosphorus of the skeleton structure and heteroatoms)

0.3≤y≤0.6 ...(2)

(wherein, y represents the molar ratio of aluminum relative to the sum of the framework structure of aluminum, phosphorus, and heteroatoms)

0.3≤z≤0.6 ...(3)

(In the formula, z represents the molar ratio of phosphorus to the sum of aluminum and phosphorus and heteroatoms in the skeleton structure)

Furthermore, among the above-mentioned abundance ratios of atoms, the existence ratio of heteroatoms is preferably represented by the following formula (4):

0.003≤x≤0.25 ...(4)

(In the formula, x has the same meaning as above)

More preferably, it is represented by the following formula (5).

0.005≤x≤0.2 ...(5)

Even in a zeolite containing aluminum, phosphorus and heteroatoms in the framework structure, the heteroatoms are preferably silicon atoms, and the integrated intensity area of the signal intensity of -108ppm to -123ppm on the ²⁹ Si-MAS-NMR spectrum of the zeolite, Preferably, it is not more than 10%, more preferably not more than 9.5%, and most preferably not more than 9% of the integrated intensity area of the signal intensity of -70ppm to -123ppm.

Also, the integrated intensity area of the signal intensity of -70ppm to -92ppm on ^{the 29} Si-MAS-NMR spectrum of the zeolite is preferably more than 25% of the integrated intensity area of the signal intensity of -70ppm to -123ppm, more preferably Above 50%.

In addition, the ²⁹ Si-MAS-NMR spectrum of the present invention is measured by using tetramethylsilane as a standard substance, storing the test material at room temperature in a water desiccator for a whole day and night, and measuring the test material saturated with water adsorbed under the following conditions .

Device: Chemagnetic CMX-400

Probe: 7.5mmMAS probe

Resonance frequency: 79.445MHz

Pulse amplitude: 5.0 microseconds

Pulse series: single pulse

Waiting time: 60 seconds

Number of revolutions: 4000rps

^{The 29} Si-MAS-NMR spectrum of zeolite gives information on the binding state of Si in the zeolite, and the Si binding state can be known from the position or distribution of peaks.

Although the ideal zeolite of the present invention contains aluminum, phosphorus, and silicon, the silicon atoms in the zeolite exist as units of SiO ₂ . Here, in the spectrum of ²⁹ Si-MAS-NMR, the peak around −90 ppm is the case where silicon atoms are bonded to atoms other than 4 silicon atoms through oxygen atoms. On the other hand, the peak around −110 ppm is the case where silicon atoms are bonded to four silicon atoms via oxygen atoms. That is, a zeolite with a large peak intensity around −110 ppm means that silicon atoms are aggregated, and the dispersion of silicon atoms on the zeolite is low.

Zeolites showing the above spectrum tend to satisfy the adsorption characteristics of the present invention. This is considered to be that the dispersibility of Si affects the adsorption properties of zeolite, and as will be described later, zeolite with high Si dispersibility exhibits particularly suitable performance as an adsorbent for adsorption heat pumps.

³以上16.0T/1,000

³以下，更好的是10.0T/1,000 ³以上15.0T/1,000

³以下范围的沸石。在此所谓骨架密度，是指每1,000

³的沸石的氧以外的构成骨架的元素的数量，该值决定于沸石的构造。On the other hand, the zeolite used as the adsorption material in the present invention preferably has a framework density of 10.0T/1,000

³ or more 16.0T/1,000

Below ³ , better is 10.0T/1,000 ³ or more 15.0T/1,000

Zeolite in the range below ³ . The so-called skeleton density here refers to every 1,000

The number of framework-constituting elements other than oxygen in zeolite ³ depends on the structure of the zeolite.

Skeleton density is related to pore volume. Generally, when the skeleton density is high, the pore volume tends to be small, and the adsorption capacity tends to be insufficient, and the performance as an adsorbent for an adsorption heat pump tends to deteriorate. On the other hand, if the skeletal density is small, the adsorbable pore volume increases and the adsorption capacity increases, but the density of the adsorbent tends to decrease and the strength tends to deteriorate.

The structure of the zeolite that satisfies the above-mentioned framework density is expressed by the code determined by IZA, including AFG, MER, LIO, LOS, PHI, BOG, ERI, OFF, PAU, EAB, AFT, LEV, LTN, AEI, AFR, AFX, GIS, KFI, CHA, GME, THO, MEI, VFI, AFS, LTA, FAU, RHO, DFO, EMT, AFY, *BEA, etc. Good examples include AEI, GIS, KFI, CHA, GME, VFI , AFS, LTA, FAU, RHO, EMT, AFY, *BEA, zeolites with CHA, AEI or ERI structure are good, among which CHA structure is also good.

In addition, the structure of zeolite is determined by measuring the XRD characteristic curve by powder XRD (powder X-ray diffraction), and comparing it with the XRD characteristic curve recorded in Collection Of Simulated XRD Powder Patterns For Zeolites (1996, ELSEVIER).

Also, the relationship between the structure and the skeleton density is described in Atlas Of Zeolites Structure Types (1996, ELSEVIER) of IZA, and the skeleton density can be known from the structure.

For example, as an aluminophosphate having a CHA structure, a desired adsorption performance can be obtained by using a silicoaluminophosphate known as SAPO-34 in which atoms such as silicon are incorporated into the framework structure of zeolite.

In addition, as the adsorbent of the present invention, although the zeolite containing aluminum, phosphorus and heteroatoms in the skeleton structure is preferable, as long as it has the above-mentioned characteristics of the adsorbent, the zeolite can also be aluminosilicate. At this time, the silicon in the skeleton 1. A part of aluminum (or all of it in the case of aluminum) is replaced with other atoms, such as magnesium, titanium, zirconium, vanadium, chromium, manganese, iron, cobalt, zinc, gallium, tin, boron and the like. In the case of aluminosilicates, if the molar ratio of silicon to aluminum is too small, as in the case of zeolite 13X, it will rapidly adsorb in the low humidity region; if it is too large, it will not absorb water much because it is too hydrophobic . Therefore, the silicon/aluminum molar ratio of the zeolite used in the present invention is usually not less than 4 and not more than 20, preferably not less than 4.5 and not more than 18, more preferably not less than 5 and not more than 16.

The above-mentioned zeolite includes forms having cation species that can be exchanged with other cations, and examples of the cation species at this time include protons, alkali elements such as Li and Na, alkaline earth elements such as Mg and Ca, rare earth elements such as La and Ce, Fe , Co, Ni and other transition metals, protons, alkali elements, alkaline earth elements, and rare earth elements are ideal. And proton, Li, Na, K, Mg, Ca are more preferable. These zeolites may be used alone or in combination with other silica or alumina, activated carbon, clay and the like.

以上，特别是最好在3.1

以上。又，最好在10

以下，其中，也最好在8

以下，更好的是在7.5以下。如果细孔直径过大，则在作为目的的相对湿度下可能不吸附，而如果细孔直径过小，则有作为被吸附物的水分子难以在吸附材料上扩散的倾向。The pore diameter of the adsorbent material of the present invention is preferably at 3

above, especially preferably in 3.1

above. Also, preferably at 10

Below, among them, preferably at 8

Below, better at 7.5 the following. If the pore diameter is too large, adsorption may not occur at the target relative humidity, and if the pore diameter is too small, it tends to be difficult for water molecules as adsorbate to diffuse on the adsorbent.

In addition, the adsorption material of the present invention preferably has an adsorption heat of not less than 40 kJ/mol and not more than 65 kJ/mol. That is, easy desorption is also an important characteristic for an adsorption material of an adsorption heat pump that requires desorption by a heat source of 100°C or lower. Ease of desorption is inversely proportional to adsorption force. Therefore, the heat of adsorption, which is an index showing the degree of adsorption, is desirably close to the latent heat of condensation of water, and not less than it, at 40 KJ/mol or more. Also, if the heat of adsorption is too large, it tends to be difficult to desorb with a heat source of 100°C or lower. Therefore, it is preferable to use a zeolite that exhibits a heat of adsorption of 65 kJ/mol or more than the latent heat of condensation of water. In addition, in this specification, according to the method described in the document [Colloid PolymSci 277 (1999) p83-88], the differential heat of adsorption was obtained by simultaneous measurement of the adsorption amount and the heat of adsorption (measurement temperature 25° C.), and the adsorption amount was calculated from The differential heat of adsorption in the range of 0.005 mol/g to 0.01 mol/g was used as the heat of adsorption.

³)的SAPO(硅铝磷酸盐)的SAPO34。As an example of a particularly good adsorbent used in the present invention, a CHA type (skeleton density=14.6T/1,000

³ ) SAPO (silicoaluminophosphate) SAPO34.

The method for producing the zeolite of the present invention is not particularly limited as long as it has the above-mentioned characteristics. etc., were produced by the following method. In addition, the synthesis method of SAPO-34 is described in US Patent No. 4440871.

In particular, as a method for producing the aforementioned ideal zeolite containing aluminum, phosphorus, and silicon in its framework structure, the following methods can be cited, for example.

First, the aluminum raw material, the silica raw material, the phosphoric acid raw material and the template are mixed to prepare the aqueous gel.

As the aluminum raw material, pseudoboehmite, aluminum isopropoxide, aluminum hydroxide, alumina sol, sodium aluminate, and the like can be used.

As the silica raw material, fumed silica, silica sol, colloidal silica, water glass, orthosilicate diester, methyl silicate, etc. can be used.

Phosphoric acid can be used as a phosphoric acid raw material. In addition, aluminum phosphate can also be used.

As a template, quaternary ammonium salts such as tetramethylammonium, tetraethylammonium, tetrapropylammonium, and tetrabutylammonium, morpholine, di-n-propylamine, tripropylamine, triethylamine, triethanolamine, and piperidine can be used. , cycloethylamine, 2-picoline, N,N-dimethylbenzylamine, N,N-diethylethanolamine, dicyclohexylamine, N,N-dimethylethanolamine, choline, N,N '-Dimethylpiperazine, 1,4-diazabicyclo(2,2,2)octane, N-methyldiethanolamine, N-methylethanolamine, N-methylpiperidine, 3-methyl Piperidine, N-methylcycloethylamine, 3-picoline, 4-picoline, quinuclidinyl, N,N'-dimethyl-1,4-diazabicyclo(2,2 , 2) octane ion, di-n-butylamine, neopentylamine, di-n-pentylamine, isopropylamine, t-butylamine, ethylenediamine, pyrrolidine, 2-imidazolidinone, di-iso Primary amines such as propyl-ethylamine and dimethylcyclohexylamine, secondary amines, tertiary amines, and polyamines.

The order of mixing the aluminum raw material, silica raw material, phosphoric acid raw material, and template varies depending on the conditions, but usually, first, the phosphoric acid raw material and the aluminum raw material are mixed, and then the silica raw material and the template are mixed therein. The composition of the aqueous gel is represented by the molar ratio of oxides, generally 0.02<SiO ₂ /P ₂ O ₅ <20, 0.02<SiO ₂ /Al ₂ O ₃ <20, preferably 0.04<SiO ₂ /P ₂ O ₅ <10, 0.04<SiO ₂ /Al ₂ O ₃ <10. The pH of the aqueous gel is from 5 to 10, preferably from 6 to 9.

In addition, in the aqueous gel, components other than the above-mentioned ones may also be appropriately present at the same time. Examples of such components include hydrophilic organic solvents such as hydroxides or salts of alkali metals or alkaline earth metals, and alcohol.

Put the reconciled water-based sol into a pressure-resistant container, use self-generated pressure, or pressurize with a gas that does not hinder crystallization, and maintain a predetermined temperature under stirring or standing still to perform hydrothermal synthesis.

The conditions for hydrothermal synthesis are usually 100°C to 300°C, preferably 120°C to 250°C. The reaction time is usually 5 hours to 30 days, preferably 10 hours to 15 days.

After hydrothermal synthesis, the product is separated, washed with water, dried, and fired to remove the contained organic matter to obtain zeolite.

When processing zeolite for use as a water vapor adsorption material, care must be taken not to lower the adsorption performance of the zeolite, but generally an inorganic binder such as alumina or silica can be used for molding.

Furthermore, in order to make the adsorbent have the desired water vapor adsorption performance, the adsorbent may contain silica sol, mesoporous silica, alumina, activated carbon, clay, etc. in addition to the zeolite of the present invention. However, in order to obtain good adsorption properties under low relative vapor pressure, the proportion of zeolite in the adsorbent material of the present invention is usually more than 60% by weight, preferably more than 70% by weight, more preferably more than 80% by weight , from the point of view of adsorption characteristics, only zeolite is the best used as water vapor adsorption material.

Also, when the adsorbent is used in an adsorption heat pump, etc., it is processed and used by referring to well-known methods in order to design a predetermined strength, particle diameter, and shape corresponding to the application. For example, as described in JP-A-2001-38188, the particle size of an adsorbent used in an adsorption heat pump is suitable to be about 0.05 mm to 2 mm. Also, as described in JP-A-2000-18767, when using an adhesive to adhere to the absorbent core, it is necessary that even if the adhesive and the adsorbent particles are mixed and dispersed, the adsorbent particles will not be The strength of the degree of damage.

<operation method>

The operation method of the adsorption heat pump will be described with reference to FIG. 1 . In the first stroke, the control valves 31 and 34 are closed, the control valves 32 and 33 are opened, the regeneration stroke is performed on the adsorption tower 1, and the adsorption stroke is performed on the adsorption tower 2. Moreover, the switching valves 115 , 116 , 215 , and 216 are operated to allow hot water to pass through the heating medium pipe 11 and cooling water to pass through the heating medium pipe 21 .

For example, when cooling the adsorption tower 2, cooling water cooled by exchanging heat with external air or river water by a heat exchanger such as a cooling tower is introduced through the heating medium pipe 21, and is usually cooled to about 30°C to 40°C. Moreover, the water in the evaporator 4 is evaporated by opening the control valve 32, and flows into the adsorption tower 2 as water vapor, where it is adsorbed on the adsorbent. Use the difference between the saturated vapor pressure at the evaporation temperature and the adsorption equilibrium pressure of the corresponding adsorption material temperature (generally 20°C to 50°C, preferably 20°C to 45°C, and more preferably 30°C to 40°C) to perform water vapor adsorption. The movement of the evaporator 4 obtains the cooling corresponding to the vaporization heat of evaporation, that is, the cooling output. Although according to the relationship between the temperature of the cooling water of the adsorption tower and the temperature of the cold water produced on the evaporator, the relative vapor pressure φ2a of the adsorption side is determined (here φ2a is the equilibrium vapor pressure of the adsorbate at the temperature of the cooling water of the adsorption tower divided by obtained by the equilibrium vapor pressure of the adsorbate at the temperature of the cold water generated on the evaporator), but it is best to operate under the condition that φ2a is larger than the relative vapor pressure of the adsorption material specified in the present invention to absorb water vapor at its maximum . This is because when φ2a is smaller than the relative vapor pressure at which the adsorbent can adsorb water vapor at the maximum specified in the present invention, the adsorption energy of the adsorbent cannot be effectively utilized, and the operation efficiency is poor. Although φ2a can be appropriately set according to the ambient temperature, etc., the adsorption capacity at φ2a is usually above 0.20, preferably above 0.29, and more preferably above 0.30 to operate the adsorption heat pump. In addition, this adsorption amount can be calculated|required from the adsorption isotherm measured at 25 degreeC.

The adsorption tower 1 in the regeneration process is heated by hot water usually at 40-100°C, preferably at 50-98°C, and more preferably at 60-95°C, to reach the equilibrium vapor pressure corresponding to the aforementioned temperature range, and condense in the condenser 5 Condensation under the saturated vapor pressure at a temperature of 30°C to 40°C (which is equal to the temperature of the cooling water cooling the condenser). The water vapor moves from the adsorption tower 1 to the condenser 5, where it condenses into water. Water returns to the evaporator 4 through the return pipe 3 . Although the relative vapor pressure φ1a of the desorption side is determined according to the relationship between the cooling water temperature of the condenser and the hot water temperature (here φ1 is the equilibrium vapor pressure of the adsorbate at the temperature of the hot water divided by the temperature of the cooling water of the condenser obtained by the equilibrium vapor pressure of the adsorbate at a lower level), but it is best to operate when φ1a is less than the relative vapor pressure of the adsorbent material that rapidly adsorbs water vapor. Although φ1a can be appropriately set according to the ambient temperature, etc., the adsorption amount at φ1a is usually below 0.06, and it is best to operate the adsorption heat pump at a temperature below 0.05. In addition, the difference between the adsorption amount of the adsorbate under φ1a and the adsorption amount of the adsorbate under φ2a is usually 0.18g/g or more, preferably 0.20g/g or more, more preferably 0.25g/g or more . The above is the first itinerary.

In the following second stroke, by switching control valves 31-34 and switching valves 115, 116, 215, and 216, the adsorption tower 1 becomes an adsorption process, and the adsorption tower 2 becomes a regeneration process, and refrigeration can also be obtained from the evaporator 4. , that is, the cooling output. Continuously operate the adsorption heat pump by sequentially switching the above first and second strokes.

In addition, although the operation method when two adsorption towers are installed is described here, if any one of the adsorption towers can maintain a state where the adsorbate can be adsorbed by properly desorbing the adsorbate adsorbed by the adsorption material, how many adsorption towers should be installed? Both are fine.

In addition, the adsorption heat pump uses the ability of the adsorbent to adsorb/desorb the adsorbate as a driving source. In the adsorption heat pump, water, ethanol, acetone, etc. can be used as the adsorbate as the adsorbate, but water is the most ideal in terms of safety, price, and latent heat of evaporation.

The adsorption heat pump of the present invention adopts an adsorbent material that obtains a large change in adsorption capacity with a narrow range of relative vapor pressure change, so it is suitable for applications that require the miniaturization of the device and limit the filling amount of the adsorbent material, such as air conditioners for automobiles, etc. .

Example

Hereafter, although an Example demonstrates this invention concretely, this invention is not limited to the following Example at all.

In addition, in the following examples, the water vapor adsorption isotherm at 25° C. was obtained by measuring the water vapor adsorption characteristics of the adsorbent under the following conditions.

Adsorption isotherm measuring device: Bellso-bu18 [manufactured by Bell Japan Co., Ltd.]

Air high temperature tank temperature: 50°C

Adsorption temperature: 25℃

Initial introduction pressure: 3.0torr

Imported pressure setpoints: 0

Saturated vapor pressure: 23.76mmHg

Balance time: 500 seconds

Pre-treatment: 300°C, 5 hours vacuum suction

In addition, the measurement of the differential heat of adsorption was carried out under the following conditions.

Measuring device: calorimeter and adsorption capacity measuring device (manufactured by Tokyo Tech)

Measuring part temperature: 25℃

Thermostat temperature for steam introduction: 30℃

Example 1

The water vapor adsorption isotherm (25° C.) of SAPO-34 (manufactured by UOP LLC) is shown in FIG. 2 . From Figure 2, it is known that water vapor is rapidly adsorbed at a relative vapor pressure of 0.07 to 0.10, and the change in the amount of adsorption in the relative vapor pressure range of 0.05 to 0.20 is 0.25 g/g.

³、细孔直径是3.8

。In addition, SAPO-34 is a CHA type silicoaluminophosphate, and the skeleton density of the CHA type is 14.6T/1,000

^3. The pore diameter is 3.8

.

Also, the ²⁹ Si-MAS-NMR record of SAPO-34 (manufactured by UOP LLC) is shown in FIG. 3 . According to the spectrum measurement record, on this spectrum, relative to the integrated intensity area of the signal intensity of -70ppm～-123ppm, the integrated intensity area of the signal intensity of -108ppm～-123ppm is 0.6%, and the integral intensity area of the signal intensity of -70ppm～-92ppm The intensity area is 85.9%. Also, if the heat of adsorption is calculated, it is 58.6 kJ/mol.

Example 2

Referring to the method described in JP-A-4-37007, CHA-type silicoaluminophosphate was produced by the following method.

To 18 g of water, 15.4 g of 85% phosphoric acid and 9.2 g of pseudo-boehmite (containing 25% of water, manufactured by Condea) were gradually added and stirred. Furthermore, 10 g of water was added and stirred for 1 hour, and this was made A liquid. Separately from liquid A, prepare a liquid mixed with 4.1 g of fumed silica (oxygen phase silica 200), 11.6 g of morpholine, and 15 g of water, and slowly add liquid A into it. Further, 24 g of water was added thereto, followed by stirring for 3 hours.

The obtained mixture was placed in a 200 cc stainless steel pressure cooker with a built-in polytetrafluoroethylene inner cylinder, and was allowed to stand at 200° C. for 24 hours to make it react. Cool down after the reaction, and use pouring to remove the supernatant and recover the precipitate. The obtained precipitate was washed with water three times, filtered, and dried at 120°C. This was fired at 550° C. for 6 hours under air flow to obtain a zeolite.

³)硅铝磷酸盐。另外，骨架密度参照IZA的Atlas Of Zeolites StructureTypes(1996，ELSEVIER)根据构造确定。又，使实验材料在盐酸水溶液中加热溶解，进行了ICP分析，果然相对骨架构造的铝和磷和硅的总和各成分的构成比例(摩尔比)是硅0.13、铝0.49、磷0.38。Determination of powder XRD, it turns out that the zeolite is CHA type (skeleton density = 14.6T/1,000

³ ) Silicoaluminophosphate. In addition, the skeleton density was determined according to the structure referring to Atlas Of Zeolites Structure Types (1996, ELSEVIER) of IZA. Furthermore, the test material was heated and dissolved in an aqueous hydrochloric acid solution, and ICP analysis was performed. As expected, the constituent ratios (molar ratios) of each component relative to the sum of aluminum, phosphorus, and silicon in the skeleton structure were 0.13 for silicon, 0.49 for aluminum, and 0.38 for phosphorus.

The adsorption isotherm at 25° C. of this zeolite is shown in FIG. 4 . It is understood from Fig. 4 that this zeolite rapidly adsorbs water vapor at a relative vapor pressure of 0.07 to 0.10, and the change in the amount of adsorption in the relative vapor pressure range of 0.05 to 0.20 is 0.25 g/g.

Also, the ²⁹ Si-MAS-NMR spectrum measurement record of this zeolite is shown in FIG. 5 . In ^{the 29} Si-NMR spectrum, the integrated intensity area of the signal intensity from -70ppm to -123ppm is 9.2% from -108ppm to -123pp, and 52.6% from -70ppm to -92pp.

Example 3

After adding 72 g of aluminum isopropoxide to 128 g of water and stirring, 38.76 g of 85% phosphoric acid was added and stirred for 1 hour. After adding 1.2 g of fumed silica (oxygen phase silica 200) to this solution, 89.3 g of a 35% tetramethylammonium hydroxide (TEAOH) aqueous solution was added and stirred for 3 hours. This mixture was placed in a 500 cc stainless steel pressure cooker with a built-in polytetrafluoroethylene inner cylinder, and reacted at 185° C. with stirring at 100 rpm for 60 hours. After the reaction, it was cooled, and the product was separated by centrifugation, washed with water, and dried at 120°C. This was fired at 550° C. for 6 hours under air flow to obtain a zeolite.

³)。又，使实验材料在盐酸水溶液中加热溶解，进行了ICP分析，果然相对骨架构造的铝和磷和硅的总和各成分的构成比例(摩尔比)是硅0.03、铝0.50、磷0.47。As a result of powder XRD measurement, it is CHA type silicoaluminophosphate (skeleton density=14.6T/1,000

³ ). Furthermore, the test material was heated and dissolved in aqueous hydrochloric acid solution, and ICP analysis was carried out. As expected, the composition ratio (molar ratio) of each component relative to the sum of aluminum, phosphorus, and silicon in the framework structure was 0.03 for silicon, 0.50 for aluminum, and 0.47 for phosphorus.

The adsorption isotherm at 25° C. of this zeolite is shown in FIG. 6 . As shown in Figure 6, this zeolite also exhibits the same adsorption isotherm as the zeolite of Example 2, rapidly adsorbs water vapor at a relative vapor pressure of 0.07 to 0.10, and the change in the amount of adsorption in the relative vapor pressure range of 0.05 to 0.20 is 0.23 g/g.

The heat of adsorption is 58.2 kJ/mol.

Example 4

SAPO-34 (manufactured by UOP LLC) was measured with an adsorption isotherm measurement device [Bell So-B 18: Nippon Bell Co., Ltd.]. The water vapor adsorption isotherm of this SAPO-34 in the adsorption process at 40° C. is shown in FIG. 7 . In addition, the determination of the adsorption isotherm is carried out under the following conditions: air high temperature tank temperature 50°C, adsorption temperature 40°C, initial introduction pressure 3.0torr, introduction pressure set point 0, saturated vapor pressure 55.33mmHg, equilibrium time 500 seconds.

On the other hand, the adsorption isotherm in the desorption process was measured by the gravimetric adsorption method of the steam introduction part arranged on the air constant temperature bath by connecting the gas generation part, the pressure measurement part and the gas discharge part on the magnetic levitation balance [Nippon Bell Co., Ltd.] device assay. The determination of the adsorption isotherm in the desorption process is to measure the weight change every 50 Torr of water vapor discharged at the temperature of the air high-temperature tank of 120°C and the desorption temperature of 90°C. The results are shown in Fig. 7 .

Assuming the case of a general vehicle as an in-vehicle air conditioner, the conditions of T1 = 90°C, T2 = 40°C, and T0 = 10°C can be considered. At this time, the relative vapor pressure of the desorption side is φ1=0.11, and the relative vapor pressure of the adsorption side is φ2=0.17. It can be judged that the difference between the adsorption capacity of φ1 and φ2 is 0.21g/g. If it exceeds the target adsorption amount difference of 0.15 g/g, it can be considered that the capacity is sufficient for a vehicle air conditioner used in general vehicles.

Also, when T1=90°C, T2=40°C, and T0=5°C, the adsorption amount between φ1=0.11 and φ2=0.17 reached 0.20 g/g, exceeding the target adsorption amount difference of 0.15 g/g, It can be considered that it has sufficient capacity as an air conditioner.

In addition, depending on the region, it can be predicted that the cooling water temperature T2 will rise to about 45°C due to the severe external environment. At this time, the condition of obtaining T0 = 10°C at T1 = 90°C can be considered. The adsorption isotherm of the adsorption process at 45° C. was measured with Bellso-B 18. It is shown in Fig. 8 together with the adsorption isotherm in the desorption process at 90°C. The measurement of the adsorption isotherm at 45°C was carried out under the following conditions: air high temperature tank temperature 65°C, adsorption temperature 45°C, initial introduction pressure 3.0torr, introduction The pressure set point is 0, the saturated vapor pressure is 55.33mmHg, and the equilibrium time is 500 seconds. At T1=90°C, T2=40°C, and T0=10°C, the desorption relative humidity φ1=0.14 exceeds the suction side relative humidity φ2=0.13.

Thus, even when the relative vapor pressure on the desorption side is higher than the relative vapor pressure on the suction side, it was found that in Example 4 having a temperature dependence, the difference in adsorption amount was 0.16 g/g. It is considered that the adsorption heat pump using the water vapor adsorbent of Example 4 can operate sufficiently even in high temperature places.

Reference example

115.3 g of 85% phosphoric acid was gradually added to 173.4 g of water, and 68 g of pseudo-boehmite (25% of water, manufactured by Condea) was gradually added and stirred for 3 hours. 30 g of fumed silica was added thereto, 87.2 g of morpholine and 242.3 g of water were added and stirred for 4.5 hours. It was allowed to stand overnight at room temperature to mature, put into an induction stirring type 1 L stainless steel autoclave with a built-in polytetrafluoroethylene inner cylinder, stirred at 60 rpm, and reacted at 200° C. for 24 hours. Cool down after the reaction, and use pouring to remove the supernatant and recover the precipitate. The precipitate thus obtained was washed with water, filtered, and dried at 120°C. This was fired at 550° C. under an air flow to obtain a zeolite. The XRD of the zeolite was determined to be CHA type. Furthermore, the test material was heated and dissolved in an aqueous hydrochloric acid solution, and ICP analysis was performed. As expected, the constituent ratios (molar ratios) of each component relative to the sum of aluminum, phosphorus, and silicon in the skeleton structure were silicon 0.12, aluminum 0.49, and phosphorus 0.39.

The adsorption isotherm at 25° C. of this zeolite is shown in FIG. 9 . From Fig. 9, it can be seen that this zeolite rapidly adsorbs water vapor from the adsorption start state with an extremely low relative vapor pressure, and the variation of the adsorption amount in the relative vapor pressure range of 0.05 to 0.20 is only 0.1 g/g or less. Therefore, it is not suitable as an adsorption material for adsorption heat pumps.

The result of Si-MAS-NMR measurement under the same conditions is shown in FIG. 10 . In ^{the 29} Si-MAS-NMR spectrum, the integrated intensity area of the signal intensity from -108 ppm to -123 ppm is 13.0% of the integrated intensity area of the signal intensity from -70 ppm to -123 ppm. Also, the integrated intensity area of the signal intensity from -70 ppm to -92 ppm was 51.6%. Thus, it is considered that if the peak intensity around -110 ppm is large, even a CHA-type silicoaluminophosphate is not suitable as an adsorbent regenerated by a heat source at 100° C. or lower. The heat of adsorption is 61.3 kJ/mol.

Comparative example 1

The difference in the adsorption capacity of the intermediate porous molecular sieve (FSM-10) is greater than 0.25 g/g in the range of relative vapor pressure 0.20 and 0.35 (Graph 4 in Figure 14 of JP-A-9-178292; refer to FSM-10). However, the adsorption amount is small in the range of the relative vapor pressure of 0.05 to 0.30, which is an example of the operation of the adsorption heat pump of the present invention. In this range, the relative vapor pressure range of 0.15 to 0.30 has a large change in the adsorption amount, but the difference in the adsorption amount at this time is 0.08 g/g, and the performance as an adsorption heat pump is poor.

Comparative example 2

The adsorption temperature of silica gel type A [Fuji Silysia Chemical Co., Ltd.], which is known as an adsorbent material suitable for adsorption heat pumps, will be measured with an adsorption isotherm measurement device [Belso-bu 18: Nippon Bell Co., Ltd.] 25 The water vapor adsorption isotherms at °C are shown in Fig. 11. In addition, this measurement was performed under the same conditions as SAPO-34 of Example 1. According to the adsorption isotherm of silica gel type A in FIG. 11 , the silica gel type A obtains an adsorption amount approximately proportional to the relative vapor pressure in the range of relative vapor pressure 0 to 0.7. However, as with intermediate porous molecular sieves or porous aluminum phosphate-based molecular sieves, in the range of relative vapor pressure of 0.15 to 0.30, the adsorption amount of type A silica gel changes only by 0.08 g/g. Adsorption heat pumps using silica gel as an adsorption material have been commercialized, but the device has to be large because the difference in adsorption amount is small.

Comparative example 3

³)沸石的ALPO-5的吸附等温线[Colloid PolymSci 277，p83-88(1999)，从Fig.1(吸附温度30℃)引用]的吸附等温线，则虽然ALPO-5在相对蒸气压0.25～0.40的范围吸附量急剧上升，在相对蒸气压0.05～0.3的范围可吸附/解吸，但在相对蒸气压0.15～0.30的范围的吸附量变化是0.14g/g。If the AFI type (skeleton density=17.5T/1,000

³ ) The adsorption isotherm of zeolite ALPO-5 [Colloid PolymSci 277, p83-88 (1999), quoted from Fig.1 (adsorption temperature 30°C)], although ALPO-5 has a relative vapor pressure of 0.25 The adsorption capacity rises sharply in the range of ~0.40, and adsorption/desorption is possible in the range of relative vapor pressure 0.05-0.3, but the change of adsorption capacity in the range of relative vapor pressure 0.15-0.30 is 0.14g/g.

Although the present invention has been described in detail with reference to specific embodiments, it should be understood by those skilled in the art that various changes and modifications can be added without departing from the spirit and scope of the present invention.

This application is based on the Japanese patent application filed on February 21, 2001 (Japanese Patent Application No. 2001-045677), the Japanese patent application filed on April 10, 2001 (Japanese Patent Application No. 2001-111902), and the Japanese patent application filed on June 25, 2001. Japanese Patent Application (Japanese Patent Application No. 2001-191893) and Japanese Patent Application (Japanese Patent Application No. 2001-293990) filed on September 26, 2001, the contents of which are hereby incorporated by reference.

Possibility of industrial use

One of the characteristics of the present invention is that an adsorbent having the above characteristics is used, and this adsorbent can be used in an adsorbing portion of an adsorbing heat pump. Because a large change in adsorption capacity can be obtained under a narrow range of relative vapor pressure changes, it is suitable for adsorption heat pumps that limit the filling amount of adsorbent materials, such as vehicle air conditioners.

The adsorption heat pump of the present invention can regenerate (desorb) the adsorbent at a low temperature because the difference in the amount of water absorbed by the adsorbent/desorb is large, so that the adsorption heat pump can be efficiently driven by a low-temperature heat source compared to conventional ones. In addition, the adsorption material used in the present invention has more variation in the adsorption capacity in the same relative vapor pressure range than conventional silica gel or zeolite, so the use of approximately the same weight of the adsorption material can produce more dehumidification effect .

That is, if the adsorbent of the present invention is used, it is possible to provide an adsorption heat pump driven by a relatively low temperature heat source of 100°C or lower.

Claims (17)

1. An adsorption heat pump comprising (a) an adsorbate, (b) an adsorption/desorption section having an adsorption material for adsorbing/desorbing the adsorbate, (c) a device connected to the adsorption/desorption section for performing an evaporation section for evaporation of the adsorbate, and (d) a condensation section connected to the adsorption/desorption section for performing condensation of the adsorbate; in, (1) The adsorption material contains a zeolite comprising aluminum and phosphorus in its framework structure; (2) The adsorbent is a water vapor adsorbent having a relative vapor pressure φ2b of not less than 0.115 and not more than 0.18 during the adsorption operation of the adsorption/desorption unit, and a relative vapor pressure φ1b of at least 0.18 during the desorption operation of the adsorption/desorption unit. The region of 0.1 to 0.14 has a range in which the difference in the adsorption amount of the adsorbent obtained by the following formula is 0.15 g/g or more: Adsorption amount difference = Q2-Q1, In the formula, Q1 = The adsorption amount at φ1b obtained from the water vapor desorption isotherm measured based on the desorption operating temperature T3 of the adsorption/desorption part, Q2 = The adsorption amount at φ2b obtained from the water vapor adsorption isotherm measured based on the adsorption operation temperature T4 of the adsorption/desorption part, and Relative vapor pressure φ1b during the desorption operation of the adsorption/desorption part=[equilibrium water vapor pressure at the temperature T2 of the refrigerant cooling the condenser]/[equilibrium water vapor pressure at the temperature T1 of the heating medium that heats the adsorption/desorption part ], Relative vapor pressure φ2b during adsorption operation of the adsorption/desorption unit=[equilibrium vapor pressure at the refrigeration temperature T0 generated by the evaporation unit]/[equilibrium vapor pressure at the refrigerant temperature T2 that cools the adsorption/desorption unit], However, T0 = 5 to 10°C, T1 = T3 = 90°C, and T2 = T4 = 40 to 45°C. 2. The adsorption heat pump according to claim 1, wherein T0 is 10°C and T2 is 40°C. 3. The adsorption heat pump according to claim 1, characterized in that T0 is 5°C and T2 is 40°C. 4. The adsorption heat pump according to claim 1, characterized in that: T0 is 10°C, T2 is 45°C. 5. The adsorption heat pump according to claim 1, characterized in that: in the region where both φ1b and φ2b are between 0.115 and 0.18, and φ1b is equal to or greater than φ2b, there is a difference in the amount of adsorption that reaches 0.15 g/g or more scope. 6. The adsorption heat pump according to claim 1, characterized in that: the zeolite contains heteroatoms in the framework structure. 7. The adsorption heat pump according to claim 6, characterized in that: the ratio of aluminum, phosphorus and heteroatoms of the zeolite is: 001≤x≤0.3 Where, x = molar ratio of heteroatoms relative to the sum of aluminum and phosphorus and heteroatoms of the framework structure 3≤y≤0.6 Wherein, y=the molar ratio of aluminum relative to the sum of phosphorus and heteroatoms of the skeleton structure 3≤z≤0.6 Where, z = the molar ratio of phosphorus relative to the sum of aluminum and phosphorus and heteroatoms of the framework structure 8. The adsorption heat pump according to claim 1, characterized in that: the zeolite has a skeleton density of 10.0T/

Above, 16.0T/

The following zeolites. 9. Use of a water vapor adsorbent (1) containing a zeolite containing aluminum and phosphorus in its skeleton structure, (2) relative vapor pressure at the time of adsorption operation of the adsorption/desorption part as an adsorbent for an adsorption heat pump In the region where φ2 is 0.115 to 0.18 and the relative vapor pressure φ1 is 0.1 to 0.14 during the desorption operation of the adsorption/desorption part, there is a range in which the difference in the adsorption amount of the adsorbent obtained by the following formula is 0.15 g/g or more: Adsorption amount difference = Q2-Q1, In the formula, Q1 = The adsorption amount at φ1 obtained from the water vapor desorption isotherm measured at the desorption operating temperature T3 of the adsorption/desorption part, Q2 = The adsorption amount at φ2 obtained from the water vapor adsorption isotherm measured at the adsorption operation temperature T4 of the adsorption/desorption part, and Relative vapor pressure φ1 during the desorption operation of the adsorption/desorption part=[equilibrium water vapor pressure at the temperature T2 of the refrigerant cooling the condenser]/[equilibrium water vapor pressure at the temperature T1 of the heating medium that heats the adsorption/desorption part ], Relative vapor pressure φ2 during the adsorption operation of the adsorption/desorption unit=[equilibrium vapor pressure at the refrigeration temperature T0 generated by the evaporation unit]/[equilibrium vapor pressure at the refrigerant temperature T2 that cools the adsorption/desorption unit], However, T0 = 5 to 10°C, T1 = T3 = 90°C, and T2 = T4 = 40 to 45°C. 10. The use according to claim 9, characterized in that T0 is 10°C and T2 is 40°C. 11. The use according to claim 9, characterized in that: T0 is 5°C, T2 is 40°C. 12. The use according to claim 9, characterized in that T0 is 10°C and T2 is 45°C. 13. The use as claimed in claim 9, characterized in that: in the area where both φ1 and φ2 are between 0.115 and 0.18, and φ1 is greater than or equal to φ2, there is a range in which the difference in adsorption amount reaches 0.15 g/g or more . 14. The use according to claim 9, characterized in that the zeolite contains heteroatoms in the framework structure. 15. use as claimed in claim 14, is characterized in that: the existence ratio of the aluminum of this zeolite and phosphorus and heteroatom is: 001≤x≤0.3 Where, x = molar ratio of heteroatoms relative to the sum of aluminum and phosphorus and heteroatoms of the framework structure 3≤y≤0.6 Wherein, y=the molar ratio of aluminum relative to the sum of phosphorus and heteroatoms of the skeleton structure 3≤z≤0.6 Where, z = the molar ratio of phosphorus relative to the sum of aluminum and phosphorus and heteroatoms of the framework structure 16. The use according to claim 14, characterized in that: the zeolite has a skeleton density of 10.0T/

Above, 16.0T/

The following zeolites. 17. An air conditioner for vehicles, characterized in that it adopts the adsorption heat pump according to claim 1.

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