JP6615619B2 - Gas separator and gas separator using the same - Google Patents

Description

  Embodiments described herein relate generally to a gas separator and a gas separation device using the same.

  In air-conditioning technology such as a home air conditioner, the technology advances in both refrigerant and energy efficiency, and a more comfortable living environment is demanded accordingly. For this reason, not only the temperature but also the multifunctionalization of air conditioners such as humidity control, ventilation, airflow adjustment, and air purification is progressing. Improving energy efficiency has become the most important issue due to recent energy shortages. In Asian countries with high temperature and high humidity, humidity adjustment, especially dehumidification, is considered to be important as living standards improve, and air conditioning with low environmental impact is required by performing this with energy saving. In dehumidification by refrigerant cooling using a compressor or the like that is currently mainstream, a large amount of energy is required because air is cooled to condense water vapor, and the cooled air is reheated to adjust the temperature. For this reason, since the power consumption increases, the size of the environmental load is a problem.

  Gas separators such as desiccant air conditioners have better energy efficiency than refrigerant-type dehumidification because they absorb moisture in the room using a moisture absorber that absorbs water vapor, and then heats it to discharge it outdoors. . However, it is necessary to regenerate the moisture absorbing material saturated by adsorbing water. The regeneration process of the hygroscopic material is performed by heating the hygroscopic material and discharging water. It has been pointed out that it is inefficient to use such a hygroscopic material regeneration treatment together with cooling. On the other hand, a dehumidifier using an inorganic separation membrane such as a zeolite membrane is known in order to dehumidify air used for instrumentation equipment and the like. A dehumidifying device using a zeolite membrane or the like is excellent in water vapor separation performance, but has a problem that the permeate flow rate of water vapor is small. Since it is necessary to secure a flow rate for air-conditioning applications and the like, a practical air-conditioning apparatus cannot be configured with a dehumidifying apparatus using a zeolite membrane or the like.

  In addition, a continuous dehumidification method using a gas separator that does not require regeneration is being studied as an energy-saving and low-cost method to replace the current air-conditioning method. As the structure of the humidity control apparatus using the gas separator, the humidity of the gas separator in which a liquid absorbent such as a lithium chloride aqueous solution is filled between two water vapor permeable membranes using polyethylene or fluororesin is conditioned. The structure arrange | positioned between spaces, such as indoors, and spaces, such as the outdoors, is mentioned, and transfer of water vapor | steam is performed between indoor air and a liquid absorbent through a water vapor permeable film. However, the water vapor permeable membrane is easily damaged, and furthermore, in this method, since the water vapor moving speed is slow, it is difficult to perform dehumidification efficiently.

JP 2002-274608 A JP 2011-041921 A JP 2013-176765 A JP 7-328375 A

  The problem to be solved by the present invention is a gas separator capable of obtaining a flow rate applicable to air conditioning or the like while maintaining a practical separation performance of a gas to be separated, and a gas separation using the same. To provide an apparatus.

The gas separator according to the embodiment is disposed between the first space and the second space, and the partial pressure of the separation target gas in the second space is set to the partial pressure of the separation target gas in the first space. A gas separator that allows gas to be separated existing in the first space to pass through the second space by lowering the first surface, and a second surface that faces the first surface; The porous body provided with. In the gas separator of the embodiment, the separation subject gas is water vapor, the porous body is a green compact of the zeolite particles having a hydrophilic. The porous body includes pores that communicate from the first surface to the second surface between the zeolite particles. Air permeability of the first surface of the green compact of the zeolite particles to the second surface is 1 × ¹⁰ -11 ^{m 2} or less 1 × ¹⁰ -14 ^{m 2} or more.

The gas separation device according to the embodiment exposes the first space, the second space communicating with the first space, the first surface to the first space, and the second surface to the second space. The gas separator of the embodiment provided to partition the first space and the second space while being exposed, and the partial pressure of water vapor as the separation target gas in the second space is the first as is lower than the partial pressure of water vapor in the space, comprising a gas pressure adjusting section for adjusting the partial pressure of water vapor in the second space, the water vapor present in the first space, the first through the gas separator 2 is a device that transmits through two spaces.

It is a figure which shows the structure of the gas separation apparatus of embodiment. It is sectional drawing which shows the gas separator used for the gas separation apparatus shown in FIG. It is sectional drawing which shows the usage example of the gas separator shown in FIG. It is a figure which shows the 1st example which used the gas separation apparatus shown in FIG. 1 as a dehumidification apparatus. It is a figure which shows the 2nd example which used the gas separation apparatus shown in FIG. 1 as a dehumidification apparatus.

  Hereinafter, a gas separator according to an embodiment and a gas separator using the gas separator will be described with reference to the drawings. In each embodiment, substantially the same constituent parts are denoted by the same reference numerals, and the description thereof may be partially omitted. The drawings are schematic, and the relationship between the thickness and the planar dimensions, the ratio of the thickness of each part, and the like may differ from the actual ones. Terms indicating directions such as up and down in the description may differ from actual directions based on the direction of gravitational acceleration.

(First embodiment)
FIG. 1 shows the configuration of a gas separation apparatus according to the first embodiment. A gas separation apparatus 1 shown in FIG. 1 is a target to be treated such as air containing gas (separation target gas) such as water vapor or organic solvent-based gas (organic solvent vapor) existing in a space to be processed (processed space). It is an apparatus that separates a separation target gas from a processing gas and lowers the gas concentration in the processing space. The gas separation device 1 includes a separation chamber 2 that constitutes the first space S1, a decompression chamber 3 that constitutes the second space S2, and a connection path 4 that connects the separation chamber 2 and the decompression chamber 3 so as to communicate with each other. The gas separator 5 arranged in the connection path 4 so as to partition the separation chamber 2 and the decompression chamber 3, the blower 6 for sending the gas to be treated including the separation target gas to the separation chamber 2, and the decompression chamber 4 is provided with a decompression pump 7 for depressurizing the inside.

  The separation chamber 2 has a suction port 8A and a discharge port 9A, and the suction port 8A is connected to the blower 6 via a pipe 10. The decompression chamber 3 has a suction port 8B and a discharge port 9B, and the discharge port 9B is connected to the decompression pump 7 via a pipe 11. By operating the blower 6, a gas to be processed such as air containing separation target gas is sent to the first space S <b> 1 in the separation chamber 2 through the pipe 10. The gas to be processed is from a space to be processed (not shown) such as a room, an apparatus interior, a factory interior (sealed space, etc.), a storage, a storage, etc. It is introduced into the blower 6 through the pipe 12. The gas to be processed in which the gas to be separated is separated in the separation chamber 2 and the gas concentration is reduced is returned to the space to be processed through the pipe 13.

  The second space S2 in the decompression chamber 3 is operated by operating the decompression pump 7, so that the pressure in the separation chamber 2 (pressure in the first space S1) and the pressure in the decompression chamber 3 (in the second space S2). The pressure is reduced so as to produce a difference with the pressure. Gases such as water vapor and organic solvent-based gas separated from the gas to be processed are discharged through a pipe 14 connected to the decompression pump 7. The separated gas (the gas that has permeated through the decompression chamber 3) is released into the atmosphere or collected as necessary. A pipe 15 is connected to the suction port 8 </ b> B of the decompression chamber 3 so as to decompress while taking outside air or the like into the decompression chamber 3. You may provide a valve (not shown) in the piping 15 as needed. Moreover, the piping 15 can be omitted depending on circumstances.

  As shown in FIG. 2, the gas separator 5 includes a porous assembly 16 of inorganic material particles 15 having affinity for the separation target gas. The porous aggregate 16 has pores 17 provided between the inorganic material particles 15. The porous assembly 16 has, for example, a rectangular parallelepiped shape, and is exposed to the first surface 16a exposed in the dehumidification chamber 2 (first space S1) and the decompression chamber 3 (second space S2). And a second surface 16b. At least a part of the pores 17 provided in the porous assembly 16 communicates from the first surface 16a to the second surface 16b. The gas separator 5 forms a wet seal by holding a liquefied product of the gas to be separated in the pores 17 of the porous assembly 16, for example, water if it is water vapor, or organic solvent if it is an organic solvent-based gas. . The gas separator 5 may contain a liquefied product of the separation target gas from the beginning, or may include a liquefied product when the gas separator 5 is used. The specific configuration of the gas separator 5 will be described in detail later.

  As shown in FIG. 3, the gas separator 5 used in the gas separation device 1 may be supported by a support 18 that transmits gas. FIG. 3 shows a state in which the pair of supports 18 are arranged along both surfaces of the gas separator 5, but the support 18 may be arranged along only one surface of the gas separator 5. For the support 18, for example, paper, punching metal, a polyimide porous body, or the like is used, and a mesh-like substance other than these may be used. The support 18 preferably has a through hole having a diameter of several μm or more, but is not limited thereto. The gas separator 5 may be formed directly on the support 18. For example, the porous body 5 may be manufactured by placing the support 18 in a mold, filling the inorganic material particles 15 thereon, and press-molding the support 18.

  A gas to be treated such as air containing the separation target gas is sent into the dehumidifying chamber 2 by operating the blower 6 as described above. Simultaneously with the blower 3, the decompression pump 7 is operated to decompress the interior of the decompression chamber 3, thereby creating a difference between the pressure in the dehumidification chamber 2 and the pressure in the decompression chamber 3. Due to this pressure difference, the partial pressure of the separation target gas such as water vapor pressure in the decompression chamber 3 (the partial pressure of the separation target gas in the second space S2 (hereinafter also simply referred to as gas partial pressure)) in the dehumidification chamber 2 is reduced. It becomes smaller than the gas partial pressure (gas partial pressure in the second space S2) such as water vapor pressure. Since the gas separator 5 forms a wet seal with the liquefied product of the separation target gas held in the holes 17, a gas partial pressure difference is generated between the dehumidification chamber 2 and the decompression chamber 3. The separation target gas (the liquefied product) moves between the dehumidifying chamber 2 and the decompression chamber 3 arranged via the gas separator 5.

  When causing the gas to be separated (the liquefied product) to move through the gas separator 5, the decompression pump 7 adjusts the pressure in the decompression chamber 3 to be −50 kPa or less with respect to the pressure in the dehumidification chamber 2. It is preferable to decompress the inside of the decompression chamber 3. In other words, it is preferable to depressurize the decompression chamber 3 so that the difference between the pressure in the dehumidification chamber 2 and the pressure in the decompression chamber 3 is 50 kPa or more. If the pressure difference is less than 50 kPa, the movement of the separation target gas (its liquefied product) from the dehumidification chamber 2 to the decompression chamber 3 may not be sufficiently promoted. Furthermore, the pressure difference between the dehumidifying chamber 2 and the decompression chamber 3 is preferably less than 100 kPa. If the pressure difference is too large, the porous assembly 16 constituting the gas separator 5 may be damaged. More preferably, the pressure difference between the dehumidifying chamber 2 and the decompression chamber 3 is in the range of 80 to 90 kPa,

  In the gas separation device 1 shown in FIG. 1, a gas partial pressure difference is generated between the dehumidification chamber 2 and the decompression chamber 3 by the decompression pump 7 that decompresses the interior of the decompression chamber 3. It is not limited to this. For example, dry air or heated air may be introduced into the decompression chamber 3 (second space S2). Also by this, a gas partial pressure difference such as a water vapor pressure difference can be generated between the dehumidifying chamber 2 and the decompression chamber 3. In the gas separation device 1 shown in FIG. 1, the gas pressure adjusting unit that generates a gas partial pressure difference between the dehumidifying chamber 2 and the decompression chamber 3 is not particularly limited, and can generate a gas partial pressure difference. Various mechanisms can be applied.

  The separation target gas contained in the gas to be treated in the dehumidification chamber 2 having a relatively high gas partial pressure is a wet seal formed by the gas separator 5, specifically, the separation target gas held in the holes 17. Absorbed into the liquefaction. The liquefied product of the gas to be separated in the gas separator 5 permeates into the decompression chamber 3 having a relatively low gas partial pressure. The separation target gas contained in the gas to be treated in the dehumidification chamber 2 according to the balance of the gas partial pressure in the dehumidification chamber 2, the gas partial pressure in the decompression chamber 3, and the amount of liquefied substance of the separation target gas in the gas separator 5 Absorption by the gas separator 5 and the release of the gas to be separated (the liquefied product thereof) in the gas separator 5 into the decompression chamber 3 occur continuously.

  Therefore, the concentration of the separation target gas in the dehumidification chamber 2 (first space S1) and the concentration of the separation target gas in the space to be processed connected to the dehumidification chamber 2 via the blower 6 can be reduced. When the separation target gas is water vapor, it can be dehumidified by reducing the amount of water vapor in the dehumidifying chamber 2 and the space to be treated. A gas to be processed such as air having a reduced gas concentration is returned from the dehumidifying chamber 2 to the space to be processed. The separation target gas such as moisture that has permeated into the decompression chamber 3 is discharged to the outside through the pipe 11, the decompression pump 7, and the pipe 14. When the separation target gas is water vapor, the moisture that has permeated into the decompression chamber 3 may be sent to a third space such as a room that needs to be humidified.

  In the gas separation device 1 of the embodiment, since the gas separator 5 forms a wet seal, only the separation target gas (its liquefied product) contained in the gas to be treated such as air in the dehumidification chamber 2 is decompressed. It can be moved into the chamber 3. For example, when the gas separation device 1 is used as a dehumidifying device, basically only moisture in the air moves between the dehumidifying chamber 2 and the decompression chamber 3, and dry air in the air hardly moves. Therefore, the temperature of the space to be dehumidified is hardly changed. By dehumidifying the interior of the space without changing the temperature of the space to be treated, there is no risk of lowering the thermal efficiency even when used together with cooling of the space, for example. It is possible to increase the thermal efficiency when the dehumidifier is used in combination with cooling.

  Next, the gas separator 5 will be described in detail. The porous aggregate 16 constituting the gas separator 5 is a particle aggregate such as an unsintered green compact or a sintered compact of the inorganic material particles 15. The aggregate is not limited to an unsintered green compact and a sintered body, and various particle aggregate structures that can form appropriate pores 17 between the inorganic material particles 15 can be applied. A method for producing the porous assembly 16 will be described later. A material having affinity for the separation target gas is used for the inorganic material particles 15 constituting the porous aggregate 16. The inorganic material particles 15 may be either single crystal particles or polycrystalline particles, and may be particles formed by hydrothermal synthesis. By constituting the porous assembly 16 with the inorganic material particles 15 having affinity for the separation target gas, the liquefied product of the separation target gas is held in the pores 17 of the porous assembly 16, and the gas separator 5. A wet seal can be formed therein.

  The inorganic material particles 15 are selected according to the separation target gas. Examples of the separation target gas include water vapor and organic solvent-based gas. Examples of the gas to be treated containing the separation target gas include air containing the separation target gas, but are not necessarily limited thereto. Examples of organic solvent gases include methanol, ethanol, n-propanol, i-propanol, n-butanol, i-butanol, s-butanol, t-butanol, ethyl acetate, n-ethyl acetate, i-butyl formate, acetone, Examples thereof include vapors of methyl ethyl ketone, methyl isobutyl ketone, diethyl ether, diisopropanol, trichloroethylene, n-hexane and the like.

  When the separation target gas is water vapor, a hydrophilic material is used for the inorganic material particles 15. Examples of the hydrophilic material constituting the inorganic material particles 15 include oxidation of aluminum (Al), silicon (Si), titanium (T), zirconium (Zr), zinc (Zn), magnesium (Mg), iron (Fe), and the like. Products, aluminosilicates containing alkali metals and alkaline earth metals, carbonates such as magnesium (Mg), calcium (Ca), strontium (Sr), phosphates such as Mg, Ca, Sr, and Mg, Ca, Examples thereof include compounds such as titanates such as Sr and Al, and composites and mixtures thereof. Specific examples of the hydrophilic material include, but are not limited to, alumina, silica, titania, zirconia, magnesia, zinc oxide, ferrite, zeolite, hydroxyapatite, and barium titanate.

  When the separation target gas is an organic solvent gas, the inorganic material particles 15 include the composite material particles in which the additive element that breaks the charge balance is introduced into the lattice of the hydrophilic compound particles, or the lattice of the hydrophilic compound particles. Defect-introducing material particles into which atomic vacancies such as oxygen vacancies are introduced are used. The hydrophilic compound is as described above, and the additive elements introduced into the lattice of such compound particles include titanium (Ti), zirconium (Zr), hafnium (Hf), vanadium (V), and chromium (Cr). , Manganese (Mn), iron (Fe), cobalt (Co), nickel (Ni), copper (Cu), zinc (Zn) and the like. However, elements that overlap with the cationic elements constituting the compound particles are excluded. By introducing these elements into the lattice or introducing oxygen vacancies or the like into the lattice, affinity for the organic solvent can be obtained.

  The average primary particle diameter of the inorganic material particles 15 constituting the porous aggregate 16 is preferably 10 nm to 10 μm. By using the inorganic material particles 15 having such an average primary particle diameter, it becomes easy to obtain the porous aggregate 16 in which the pores 17 having an appropriate size are present in an appropriate amount. If the average primary particle diameter of the inorganic material particles 15 exceeds 10 μm, the size of the pores 17 in the porous aggregate 16 tends to increase, and the wet seal formability may be reduced. If the average primary particle diameter of the inorganic material particles 15 is less than 10 nm, the amount of the pores 17 in the porous aggregate 16 is reduced or the size of the pores 17 tends to be small, so that the permeation of the separation target gas The flow rate may be reduced. The average primary particle diameter of the inorganic material particles 15 is more preferably 50 to 1000 nm. Further, two or more kinds of inorganic material particles 15 having different average primary particle diameters may be used to control the size and amount of the pores 17 in the porous aggregate 16. This makes it easy to achieve both the separation rate of the separation target gas and the permeation flow rate.

  Examples of the porous aggregate 16 using the inorganic material particles 15 as described above include green compacts (unsintered green compacts) and sintered bodies of the inorganic material particles 15. The green compact of the inorganic material particles 15 can be obtained, for example, by filling the inorganic material particles 15 in a mold and compression molding. The sintered body of the inorganic material particles 15 is obtained by sintering the green compact. By adjusting the compression molding conditions and sintering conditions of the inorganic material particles 15, a green compact and a sintered body having an appropriate porous state can be obtained. Further, when zeolite is used as the inorganic material particles 15, a hydrothermally synthesized porous body or the like may be used. Further, the porous material 16 may be produced by mixing the inorganic material particles 15 with a binder resin and molding the mixture. In this case, it is preferable to adjust the amount of resin so as to obtain appropriate pores 17 or to use a resin that becomes a porous body in advance. The molding method of the mixture is not limited to the compression molding method, and a sheet molding method such as a doctor blade or an extrusion molding method may be applied. The molded body of the mixture may be used as the porous assembly 16 as it is, or may be used in a degreased state by heat treatment at an appropriate temperature.

  In the gas separator 5 of the embodiment, the average pore diameter of the pores 17 existing between the inorganic material particles 15 is preferably in the range of 50 nm to 5 μm. By setting the average pore diameter of the holes 17 in the range of 50 nm to 5 μm, it becomes easier to hold the liquefied material of the separation target gas in the holes 17 that are the passages of the separation target gas, and a wet seal is formed on the gas separator 5. At the same time, an appropriate permeate flow rate of the liquefied product of the separation target gas can be ensured. When the average hole diameter of the air holes 17 exceeds 5 μm, the wet sealability is deteriorated, and the balance between the absorption of the separation target gas from the dehumidification chamber 2 and the release of the separation target gas into the decompression chamber 3 is reduced. Separation performance tends to decrease. When the average pore diameter of the holes 17 is less than 50 nm, the permeation flow rate of the separation target gas (its liquefied product) such as water vapor or organic solvent-based gas tends to decrease. The average pore diameter of the pores 17 is more preferably in the range of 50 to 500 nm.

  The volume porosity of the porous assembly 16 (volume ratio of the pores 17 in the porous assembly 16) is preferably in the range of 20 to 60%. If the volume porosity of the porous aggregate 16 is less than 20%, the amount of the liquefied substance of the separation target gas that can pass through the pores 17 decreases, so that the absorption amount of the separation target gas from the dehumidification chamber 2 and the decompression chamber 3 are reduced. There is a risk that the release amount of the separation target gas will become insufficient. When the volume porosity of the porous assembly 16 exceeds 60%, the strength of the porous assembly 16 is lowered, and the continuous operation of the gas separation device 1 is hindered, and the wet sealability of the gas separator 5 is deteriorated. There is a risk. The volume porosity of the porous aggregate 16 is more preferably in the range of 30 to 50%. The volume porosity of the porous aggregate 16 and the shape of the pores 17 (average pore diameter, etc.) are values measured by a mercury intrusion method.

In the porous aggregate 16 constituting the gas separator 5, based on the average primary particle diameter of the inorganic material particles 15 described above, the molding conditions of the inorganic material particles 15, the average pore diameter of the pores 17, the volume porosity, etc. The air permeability from the first surface 16a to the second surface 16b is adjusted to a range of 1 × 10 ⁻¹⁴ to 1 × 10 ⁻¹¹ m ² . Thus, it is possible to improve the permeation flow rate of the separation target gas (its liquefied product) while maintaining a practical separation ratio α of the separation target gas, for example, a separation ratio α of about 3 to 100. When the air permeability of the porous aggregate 16 is less than 1 × 10 ⁻¹⁴ m ² , the permeation flow rate of the separation target gas (its liquefied product) decreases. When the air permeability exceeds 1 × 10 ⁻¹¹ m ² , the wet sealability is lowered and the separation rate α of the separation target gas is likely to be lowered. The air permeability of the porous aggregate 16 is preferably in the range of 1 × 10 ⁻¹⁴ to 1 × 10 ⁻¹³ m ² . By using the gas separator 5 having both the separation rate α and the permeation flow rate of the separation target gas, it is possible to improve the continuous gas separation performance without regeneration treatment. Therefore, it is possible to provide a practical and efficient gas separation device 1.

The air permeability K is determined as follows from a pressure difference ΔP [unit: kPa] and a flow velocity Q _air [unit: cm ³ / min] between inflow and outflow of a fixed volume of air in the vertical direction of the sample. Calculated based on equation (1). In the equation (1), δ is the thickness of the sample, A is the area of the sample, and μ _air is the viscosity of the air (18.57 μPa · s).
K = (Q _air / ΔP) · (μ _air / A) · δ (1)

The gas separation rate α is the ratio of the amount of permeated dry air that constitutes the gas to be treated and the liquefied gas such as water, and is defined by the following equation (2).
α = (N4 _liquid / N4 _air ) / (N3 _liquid / N3 _air ) (2)
In the formula (1), (N3 _liquid / N3 _air ) is a molar ratio between the liquefied gas of the gas to be treated (air) supplied to the dehumidifying chamber 2 (first space S1) and dry air, and (N4 _water / N4 _air ) is the molar ratio of the liquefied gas of the gas contained in the gas to be processed (air) discharged from the decompression chamber 3 (second space S2) and dry air. If α is 1, it means that a gas liquefied product (water or the like) and dry air flow from the dehumidification side space S1 to the decompression side space S2 at the same rate. If α is 100, it means that the permeation of dry air is reduced to 1/100 with respect to the permeation of gas liquefaction (water or the like) from the dehumidification side space S1 to the decompression side space S2.

The gas (liquefied product) permeation speed V is defined by the following equation (3).
V = ΔM _liquid / A / Δt (3)
In equation (2), ΔM _liquid is the amount of gas liquefied material recovered in the decompression side space S2, A is the area of the gas separator 5, and Δt is time.

(Second Embodiment)
Next, a configuration example in which the gas separation device 1 according to the first embodiment is used as a dehumidifying device will be described with reference to FIGS. 4 and 5. In FIG. 4, R indicates a room constituting the dehumidifying target space Rx, and the room R has an intake port Ra. The dehumidifier 1 is provided in the room R in order to remove water vapor (water) from the air in the space Rx to be dehumidified. The dehumidifying device 1 shown in FIG. 4 has a structure in which a pipe 15 for taking in external air is connected to the decompression chamber 3 (second space S2). In the dehumidifying device 1, the inside of the decompression chamber 3 is decompressed while taking outside air into the decompression chamber 3. The pipe 15 has a valve 21.

  The air in the space Rx is basically composed of water vapor (water) and dry air. In the dehumidifying chamber 2 of the dehumidifying device 1, the air in the space Rx is sent through the pipes 12 and 10 by operating the blower 6. The air dehumidified in the dehumidifying chamber 2 is returned to the space Rx via the pipe 13. The dehumidifying operation (gas separating operation) using the gas separator 5 is as described in detail in the first embodiment. That is, only moisture permeates from the dehumidification chamber 2 to the decompression chamber 3 through the gas separator 5 in which a wet seal is formed. Since the absorption of moisture in the air by the gas separator 5 and the release of moisture in the gas separator 5 to the decompression chamber 3 occur continuously, the dehumidification performance by continuous dehumidification without regeneration treatment is improved. it can. Therefore, it is possible to provide a practical and efficient dehumidifying device 1.

  The application structure of the dehumidifying device 1 of the embodiment is not limited to the structure shown in FIG. The dehumidifying device 1 of the embodiment can be variously modified. Although the first space S1 is set in the dehumidifying chamber 2 of the dehumidifying device 1 in FIG. 4, the first space S1 is not limited to this. As shown in FIG. 5, the first space S1 may be the dehumidifying target space Rx itself. That is, the decompression chamber 3 serving as the second space S2 may be disposed via the target space Rx serving as the first space S1 and the gas separator 5. In this case, by reducing the pressure in the decompression chamber 3, water vapor (water) is directly removed from the air in the dehumidification target space Rx (first space S1). The settings of the first space S1 and the second space S2 can be variously changed.

  Next, examples and evaluation results thereof will be described.

(Example 1)
A 4A zeolite particle (LTA type, pore size: 0.3 to 0.4 nm) having an average particle size of 3 μm is filled in a mold, and compression-molded at a pressure of 1 t / cm ² , thereby obtaining a pressure of 2 mm. A powder (porous assembly) was prepared. When the pore shape and the like of the green compact were measured by a mercury intrusion method, the average pore diameter was 170 nm and the volume porosity was 40%. The air permeability of the green compact was 3 × 10 ⁻¹⁴ m ² . When the green compact was used as a gas separator, the water vapor separation rate α and the water vapor transmission rate V were measured, and when the temperature of the supply air to the dehumidification (adsorption) side was 40 ° C. and saturated steam, The rate α was 3, and the water vapor transmission rate V was 300 g / h / m ² . Even when the test was conducted for several hours, the water vapor separation rate α and the water vapor transmission rate V were not decreased. Furthermore, no change was observed even after the same measurement after one month.

(Example 2)
4A zeolite particles having an average particle diameter of 3 μm and small-sized particles obtained by pulverizing the 4A zeolite particles with a bead mill and adjusting the average particle diameter to 300 nm were prepared. 4A zeolite particles having an average particle diameter of 3 μm and 4A zeolite particles (small diameter particles) having an average particle diameter of 300 nm were mixed at a volume ratio of 100: 7. The mixed powder was filled in a mold and compression molded at a pressure of 1 t / cm ² to produce a 2 mm-thick green compact (porous assembly). When the pore shape and the like of the green compact were measured by a mercury intrusion method, the average pore diameter was 180 nm and the volume porosity was 30%. The air permeability of the green compact was 5 × 10 ⁻¹⁴ m ² . When the green compact was used as a gas separator, the water vapor separation rate α and the water vapor transmission rate V were measured, and when the temperature of the supply air to the dehumidification (adsorption) side was 40 ° C. and saturated steam, The rate α was 6, and the water vapor transmission rate V was 500 g / h / m ² . Even when the test was conducted for several hours, the water vapor separation rate α and the water vapor transmission rate V were not decreased. Furthermore, no change was observed even after the same measurement after one month.

(Example 3)
4A zeolite was produced by a hydrothermal synthesis method, and after molding this 4A zeolite, heat treatment was performed at 90 ° C. to obtain a porous body. When the pore shape and the like of the porous body were measured by a mercury intrusion method, the average pore diameter was 100 nm and the volume porosity was 30%. The air permeability of the porous body was 1.5 × 10 ⁻¹⁴ m ² . When the water vapor separation rate α and the water vapor transmission rate V were measured when this porous body was used as a gas separator, the water vapor separation rate was obtained under the conditions of the temperature of the supply air to the dehumidification (adsorption) side being 40 ° C. and saturated steam. α = 50, water vapor transmission rate V = 250 g / h / m ² . Even when the test was conducted for several hours, the water vapor separation rate α and the water vapor transmission rate V were not decreased. Furthermore, no change was observed even after the same measurement after one month.

(Example 4)
Using the gas separator produced in Example 2, the gas separator shown in FIG. 4 was constructed. By depressurizing the second space, the amount of moisture in the air supplied to the first space is reduced. Thereby, the target space in the room is dehumidified. Although the initial temperature of the dehumidification target space was 40 ° C. and the relative humidity was 70%, the relative humidity decreased to 60% by operating the gas separation device for 1 hour. The gas separator was operated with the second space pressure relative to the first space set to -80 kPa. At this time, the temperature of the target space was stable in the range of 40 ° C. ± 1 ° C. Moreover, when the same dehumidification test was implemented using the gas separator produced in Example 1, the same result was obtained. The same was true when the gas separator produced in Example 3 was used.

(Comparative Example 1)
4A zeolite is rubbed against the surface of the alumina substrate, and this is immersed in a hydrothermal synthesis solution (90 ° C.) for 1 hour to form a 4A zeolite film having a thickness of 5 μm on the surface of the alumina substrate. did. The obtained zeolite membrane had a volume porosity of 25% and an air permeability of 1 × 10 ⁻¹⁵ m ² . When the water vapor separation rate α and the water vapor transmission rate V when the zeolite membrane was used as a gas separator were measured, the water vapor separation rate α > 100, water vapor transmission rate V = 100 g / h / m ² , but thereafter the entire substrate was damaged.

(Comparative Example 2)
After adding an acetone solution of polyvinyl butyral (PVB) having a concentration of 5% to alumina particles having an average particle diameter of 0.4 μm, mixing in a mortar, filling in a mold and molding at a pressure of 1 t / cm ² , Furthermore, by sintering at 1000 ° C., a porous sintered body having a thickness of 2 mm was produced. When the pore shape and the like of the porous sintered body were measured by a mercury intrusion method, the average pore diameter was 480 nm and the volume porosity was 40%. The air permeability of the porous sintered body was 4 × 10 ⁻¹⁰ m ² . When the water vapor separation rate α and the water vapor transmission rate V were measured when the porous sintered body was used as a gas separator, the water vapor was supplied under the conditions of a temperature of the supply air to the dehumidification (adsorption) side of 40 ° C. and saturated steam. The separation rate α was 1, and the water vapor transmission rate V was 4000 g / h / m ² .

(Comparative Example 3)
When the dehumidification test was carried out in the same manner as in Example 4 using the gas separators produced in Comparative Example 1 and Comparative Example 2, the humidity did not decrease after operating the gas separator for 1 hour.

(Example 5)
A ZSM-5 zeolite particle having an average particle diameter of 5 μm was impregnated with an iron nitrate solution, dried, filled in a mold, and compression-molded at a pressure of 1 t / cm ² to obtain a pressure of 2 mm in thickness. A powder (porous assembly) was prepared. When the pore shape and the like of the green compact were measured by a mercury intrusion method, the average pore diameter was 3 μm and the volume porosity was 40%. The air permeability of the green compact was 9 × 10 ⁻¹² m ² . When this green compact was used as a gas separator, a vapor separation test of an aqueous ethanol solution was performed. As a result, a 5% by mass ethanol solution was concentrated to about 80% by mass.

  In addition, although several embodiment of this invention was described, these embodiment is shown as an example and is not intending limiting the range of invention. These novel embodiments can be implemented in various other forms, and various omissions, replacements, and changes can be made without departing from the scope of the invention. These embodiments and modifications thereof are included in the scope and gist of the invention, and are included in the invention described in the claims and the equivalents thereof.

  DESCRIPTION OF SYMBOLS 1 ... Gas separation apparatus, 2 ... Dehumidification chamber, 3 ... Decompression chamber, 4 ... Connection path, 5 ... Gas separation body, 6 ... Blower, 7 ... Decompression pump, 15 ... Inorganic material particle, 16 ... Porous aggregate, 17 ... Hole, 18 ... Support, S1 ... First space, S2 ... Second space S2.

Claims (10)

By being arranged between the first space and the second space, and making the partial pressure of the separation target gas in the second space lower than the partial pressure of the separation target gas in the first space, In the gas separator that allows the separation target gas existing in the first space to pass through the second space,
Comprising a porous body comprising a first surface and a second surface facing the first surface;
The separation target gas is water vapor, and the porous body is an unsintered compact of zeolite particles having hydrophilicity,
The porous body includes pores communicating from the first surface to the second surface between the zeolite particles,
The air permeability of from the first surface of the green compact of the zeolite particles to said second surface is 1 × ¹⁰ -11 ^{m 2} or less 1 × ¹⁰ -14 ^{m 2} or more, the gas separator .   The gas separator according to claim 1, wherein an average pore diameter of the pores existing in the porous body is 50 nm or more and 5 µm or less.   The gas separator according to claim 1 or 2, wherein a volume porosity of the porous body is 20% or more and 60% or less.   The gas separator according to any one of claims 1 to 3, wherein an average primary particle size of the zeolite particles is 10 nm or more and 10 µm or less.   The gas separator according to any one of claims 1 to 4, wherein the porous body includes water retained in the pores. A first space;
A second space leading to the first space;
The first surface is exposed to the first space, and the second surface is exposed to the second space, and the first space and the second space are partitioned. A gas separator according to any one of claims 1 to 5, which is provided,
Gas pressure for adjusting the partial pressure of the water vapor in the second space so that the partial pressure of the water vapor as the separation target gas in the second space is lower than the partial pressure of the water vapor in the first space. An adjustment unit,
A gas separation device that allows the water vapor existing in the first space to pass through the second space through the gas separator.   The gas separation device according to claim 6, wherein the gas pressure adjusting unit includes a pressure adjusting mechanism that reduces the pressure in the second space from the pressure in the first space.   The gas pressure adjusting unit includes a pipe for taking in external air into the second space, a valve provided in the pipe, and a pressure adjustment for reducing the pressure in the second space from the pressure in the first space. The gas separation device according to claim 6, comprising a mechanism. The first space is constituted by a dehumidification chamber, the second space is constituted by a decompression chamber,
The gas pressure adjustment unit is connected to the decompression chamber so as to take in external air into the second space, a valve provided in the piping, and connected to the decompression chamber. The gas separation device according to claim 6, further comprising: a pressure adjusting mechanism that depressurizes the inside of the second space together with the external air taken in through a valve.   The gas separator according to any one of claims 6 to 9, wherein the gas separator is supported by a support that allows gas to pass therethrough.

Images