JP6496281B2 - Absorption system - Google Patents

Description

  The present invention relates to an absorption system.

  Conventionally, an absorption refrigerator and an absorption heat pump are known as absorption systems. Among them, the absorption refrigerator has a heat release process in the absorber and the condenser, and a heat collection process in the evaporator. In addition, the absorption refrigerator requires driving heat from the outside in the regenerator, and cold water obtained in the evaporator can be used for cooling. Here, it is necessary to dripping cold water of about 7 ° C. into the heat transfer tube of the evaporator, and when using a water refrigerant and a lithium bromide absorbing liquid that are widely used in air conditioning applications. The pressure between the evaporator and the absorber is about 1 kPa. On the other hand, since the heat radiation from the absorber and the condenser is directed to the atmosphere regardless of whether it is directly air-cooled or cooled, it is necessary to dissipate heat at a temperature higher than the atmospheric temperature, and generally 38 degrees Celsius. The above is set (see Patent Documents 1 and 2).

Japanese Patent Laid-Open No. 5-99531 JP-A-8-261589

  FIG. 7 is a dueling diagram according to an example of a conventional absorption refrigerator. In addition, in FIG. 7, an example of the Duhring diagram in single effect is shown. As shown in FIG. 7, the concentration of the diluted absorbent after the absorption process is set to about 54% or more (54% in FIG. 7), and the pressure of the condenser and the regenerator is set to about 6.5 kPa or more (FIG. 7). Suppose that it is set to 6.5 kPa). In this case, as shown in FIG. 7, the regenerator temperature cannot be cycled without a heat source of about 88 degrees Celsius.

  Here, the heat source of the single-effect absorption chiller can be exhaust heat from the generator of the reciprocating engine or solar heat, but the reciprocating engine is expected to use hot water of about 80 ° C or less from the viewpoint of engine cooling. In rare cases, only hot water having a temperature lower than about 60 ° C. can be supplied even by solar heat. For this reason, it becomes difficult to use the exhaust heat or solar heat of the generator of the reciprocating engine as the heat source of the single-effect absorption refrigerator.

  Furthermore, although illustration is omitted, in the double effect, the regeneration temperature becomes higher than the regeneration temperature shown in FIG. 7, and a heat source of at least 120 ° C. is required. For this reason, utilization as a heat source for the exhaust heat or solar heat becomes more difficult.

  In addition, in areas such as the Middle East and Africa where the atmospheric temperature can be about 45 degrees Celsius, the heat radiation temperature shown in FIG. 7 will be raised from 38 degrees Celsius to about 55 degrees Celsius, and the heat source temperature will increase accordingly. End up. Therefore, even in this case, it becomes more difficult to use the exhaust heat or solar heat as a heat source.

  As described above, since it is difficult to use the heat source, it is desired to develop an absorption refrigerator that can be driven at a lower temperature. Note that the above problem is not limited to the absorption refrigerator, but is also a problem common to absorption heat pumps and absorption heat transformers that are other absorption systems.

  The present invention has been made to solve such problems, and an object of the present invention is to provide an absorption system that can be driven at a lower temperature.

  The absorption system of the present invention includes an evaporator, an absorber, a regenerator, and a condenser, and also includes a refrigerant transfer device. The refrigerant transfer device includes a first chamber through which the first absorbing liquid flows, a second chamber through which a second absorbing liquid different from the first absorbing liquid flows, and a semipermeable membrane that partitions between the first chamber and the second chamber. Have. The first absorbent absorbs the refrigerant vaporized in the absorber and reaches the first chamber, and the refrigerant is concentrated by being absorbed by the second absorbent in the second chamber through the semipermeable membrane in the first chamber. To the absorber again. In the regenerator, the refrigerant is boiled and separated in the regenerator and reaches the second chamber. In the second chamber, the refrigerant is diluted by absorbing the refrigerant from the first absorbent in the first chamber via the semipermeable membrane, and is again diluted. Leads to the regenerator.

  According to the present invention, the first absorption liquid passes from the absorber through the first chamber to the absorber again, and the second absorption liquid passes from the regenerator through the second chamber to the regenerator again. In this process, the refrigerant in the first absorption liquid in the first chamber reaches the second chamber through the semipermeable membrane and is absorbed by the second absorption liquid in the second chamber. By adopting such a configuration, it is not necessary to boil and separate the refrigerant from the first absorption liquid, and it is only necessary to boil and separate the refrigerant from the second absorption liquid. For this reason, by optimizing the saturated vapor pressure and the like of the second absorbing liquid, the regenerating process can be performed at a temperature lower than the temperature when the first absorbing liquid is regenerated, and can be driven at a lower temperature. Absorption systems can be provided.

It is a lineblock diagram showing an absorption system concerning an embodiment of the present invention. It is a dueling diagram of the absorption type system concerning this embodiment. It is a dueling diagram of the absorption type system concerning a 2nd embodiment. It is a block diagram which shows the absorption type system which concerns on 3rd Embodiment. It is a dueling diagram of the absorption type system concerning a 3rd embodiment. It is a block diagram which shows the absorption type system which concerns on 4th Embodiment. It is a dueling diagram which concerns on an example of the conventional absorption refrigerator.

  Hereinafter, the present invention will be described according to preferred embodiments. Note that the present invention is not limited to the embodiments described below, and can be appropriately changed without departing from the spirit of the present invention. Further, in the embodiment described below, there is a part where illustration or description of a part of the configuration is omitted, but details of the omitted technology are within a range in which there is no contradiction with the contents described below. Needless to say, known or well-known techniques are applied as appropriate.

  FIG. 1 is a configuration diagram showing an absorption system according to an embodiment of the present invention. As shown in FIG. 1, the absorption system 1 includes an evaporator 10 that vaporizes a liquid refrigerant to obtain a cooling effect, an absorber 20 that absorbs the vaporized refrigerant with an absorption liquid and releases absorption heat, and an external device. The refrigerating machine 30 is provided with a regenerator 30 for boiling-separating the refrigerant from the absorbing liquid that has absorbed the refrigerant by the heat energy, and the condenser 40 for radiating and condensing the boiled and evaporated refrigerant. Further, in the present embodiment, the absorption system 1 includes the refrigerant transfer device 50 and uses a first absorption liquid and a second absorption liquid different from the first absorption liquid to circulate the first absorption liquid. A circulation structure R1 and a second circulation structure R2 that circulates the second absorbent are constructed. Hereinafter, each part will be described in detail.

  The refrigerant transfer device 50 includes a first chamber 51, a second chamber 52, and a semipermeable membrane 53 that separates the chambers 51 and 52. The first chamber 51 is a chamber through which the first absorption liquid flows, and the second chamber 52 is a chamber through which the second absorption liquid flows. Here, in the present embodiment, the second absorbing liquid is a liquid having a higher saturated vapor pressure than the first absorbing liquid and a liquid having an osmotic pressure higher than that of the first absorbing liquid. Preferably, the first absorption liquid contains a monovalent inorganic salt or organic salt as a main component, and the second absorption liquid contains a polyvalent inorganic salt or organic salt as a main component. In particular, the first absorbing liquid is required to have high solubility and low saturated vapor pressure, and preferably contains at least one of lithium bromide, lithium iodide, and lithium chloride as a main component. There may be. The second absorption liquid is required to have high solubility, and a saturated vapor pressure and osmotic pressure to be moderately higher than those of the first absorption liquid, and include calcium chloride, magnesium chloride, calcium bromide, magnesium bromide, and zinc bromide. It is preferable to include at least one as a main component. In the following embodiments, description will be made assuming that the first absorption liquid is a solution containing lithium bromide as a main component and the second absorption liquid is a solution containing calcium chloride as a main component. Furthermore, in the following embodiments, water will be described as an example of the refrigerant. For this reason, the liquid refrigerant is water in a liquid state, and the evaporated refrigerant and the evaporated refrigerant mean water vapor.

  The first circulation structure R <b> 1 is configured by the absorber 20 and the first chamber 51 of the refrigerant transfer device 50. The absorber 20 absorbs the refrigerant vaporized in the evaporator 10 with the first absorbing liquid. The first chamber 51 introduces the first absorbing liquid diluted by absorbing the refrigerant in the absorber 20. The concentration of the first absorbing liquid introduced is 56% (equivalent to a lithium bromide aqueous solution, regarding vapor pressure and osmotic pressure). In the first chamber 51, the refrigerant absorbed in the first absorption liquid is absorbed by the second absorption liquid in the second chamber 52 through the semipermeable membrane 53. As a result, the first absorbing liquid is concentrated and discharged from the first chamber 51. The concentration of the first absorbent discharged is 60% (corresponding to a lithium bromide aqueous solution, with respect to vapor pressure and osmotic pressure). The absorber 20 introduce | transduces said 1st absorption liquid concentrated, and makes the 1st absorption liquid absorb the refrigerant | coolant vaporized in the evaporator 10. FIG. Thereafter, this circulation is repeated.

  The second circulation structure R <b> 2 is configured by the regenerator 30 and the second chamber 52 of the refrigerant transfer device 50. The regenerator 30 causes the refrigerant to boil and separate from the second absorbing liquid that has absorbed the refrigerant by heat energy from the outside. The second chamber 52 introduces the second absorbing liquid that is separated and concentrated in the regenerator 30. The concentration of the second absorbent to be introduced is 58% (corresponding to calcium chloride aqueous solution, regarding osmotic pressure). In the second chamber 52, the refrigerant that has been absorbed by the first absorbent through the semipermeable membrane 53 is absorbed by the second absorbent. As a result, the second absorbent is diluted and discharged from the second chamber 52. The concentration of the second absorbent to be discharged is 56% (corresponding to an aqueous calcium chloride solution, regarding osmotic pressure). The regenerator 30 separates the refrigerant by boiling the diluted second absorption liquid with heat energy from the outside. Thereafter, this circulation is repeated.

  In the absorption system 1 shown in FIG. 1, the refrigerant (water vapor) separated in the regenerator 30 is converted into a liquid refrigerant in the condenser 40. The evaporator 10 introduces this liquid refrigerant and cools the water in the heat transfer tube by dropping it onto a heat transfer tube (not shown). On the other hand, the dropped water evaporates and is absorbed by the first absorbent in the absorber 20. The water that has not evaporated in the evaporator 10 is supplied to the regenerator 30 again because it contains a small amount of calcium chloride.

  Here, as described above, the first chamber 51 is supplied with the first absorbing liquid having a concentration of 56% (corresponding to the lithium bromide aqueous solution, with respect to the vapor pressure and the osmotic pressure). The osmotic pressure of the 56% concentration lithium bromide aqueous solution is about 190 MPa, which is equivalent to the osmotic pressure of the 54% concentration calcium chloride aqueous solution. The concentration of the first absorbent at the time of discharge from the first chamber 51 is 60% (equivalent to an aqueous lithium bromide solution, regarding vapor pressure and osmotic pressure). The osmotic pressure of the 60% aqueous lithium bromide solution is about 230 MPa, which is equivalent to the osmotic pressure of the 57% aqueous calcium chloride solution. On the other hand, the concentration of the second absorption liquid at the time of introduction and discharge of the second chamber 52 is 58% (corresponding to calcium chloride aqueous solution, osmotic pressure) and 56% (corresponding to calcium chloride aqueous solution, osmotic pressure), respectively. The pressure is 250 MPa and 220 MPa, respectively. Accordingly, in the refrigerant transfer device 50, the refrigerant moves from the first absorbent to the second absorbent with an osmotic pressure difference of 20 to 30 MPa. That is, water can be transferred from the lithium bromide aqueous solution to the calcium chloride aqueous solution by forward osmosis without requiring pressurization.

  Next, the operation of the absorption system 1 according to the present embodiment will be described with reference to the Duering diagram. FIG. 2 is a dueling diagram of the absorption system 1 according to the present embodiment. As shown in FIG. 2, it is assumed that the pressure in the evaporator 10 and the absorber 20 is 1.0 kPa, and the pressure in the regenerator 30 and the condenser 40 is 6.5 kPa.

  As shown in FIG. 2, first, a first absorbent having a concentration of 60% (corresponding to an aqueous lithium bromide solution, regarding vapor pressure and osmotic pressure) is supplied into the absorber 20 having a pressure of 1.0 kPa (see point A2). In the absorber 20, the first absorbent having a concentration of 60% (corresponding to the lithium bromide aqueous solution, vapor pressure and osmotic pressure) absorbs the water evaporated in the evaporator 10 and has a concentration of 56% (equivalent to the lithium bromide aqueous solution). , With respect to vapor pressure and osmotic pressure) (see point B2). In addition, the absorption heat which arises when the 1st absorption liquid of 60% density | concentration (equivalent to lithium bromide aqueous solution, vapor pressure and osmotic pressure) absorbed water vapor | steam is removed by heat exchange with air | atmosphere. Next, the first absorbent having a concentration of 56% (corresponding to an aqueous lithium bromide solution, regarding vapor pressure and osmotic pressure) is supplied to the first chamber 51 of the refrigerant transfer device 50 (see point C2). In the refrigerant transfer device 50, water molecules move to the second chamber 52 due to the difference in osmotic pressure (see symbol E2), so that the first absorbing liquid has a concentration of 60% again (equivalent to an aqueous lithium bromide solution, regarding vapor pressure and osmotic pressure). (See point D2). Thereafter, the absorption system 1 moves water molecules to the second chamber 52 as indicated by reference numeral E2 while repeating the cycle of points A2 to D2.

  On the other hand, the regenerator 30 (6.5 kPa pressure) is supplied with a second absorbent having a concentration of 56% (corresponding to an aqueous calcium chloride solution, regarding osmotic pressure) (see point F2). The second absorbent having a concentration of 56% (corresponding to an aqueous calcium chloride solution and osmotic pressure) is heated to T (A) ° C. in the regenerator 30 to boil and separate the water vapor, and has a concentration of 58% (calcium chloride aqueous solution). (Refer to point G2). The second absorbing liquid whose concentration has increased to 58% (corresponding to an aqueous calcium chloride solution, regarding osmotic pressure) is supplied to the second chamber 52 of the refrigerant transfer device 50 (see point H2). In the refrigerant transfer device 50, water molecules move to the second chamber 52 due to the difference in osmotic pressure (see symbol E2), so that the second absorption liquid again has a concentration of 56% (corresponding to an aqueous calcium chloride solution, regarding osmotic pressure) (points). I2). Thereafter, the absorption system 1 receives water molecules in the second chamber 52 as indicated by reference numeral E2 while repeating the cycle from point F2 to point I2.

The water vapor generated in the regenerator 30 reaches the condenser 40 and is cooled to 38 ° C. by the heat exchange with the atmosphere in the condenser 40 to be liquefied (see point J2). Thereafter, water, which is a liquid refrigerant, is supplied to the evaporator 10 and vaporizes (see point K2). Thereby, the cold water for cooling will be obtained. The vaporized water is absorbed by the first absorbent at a concentration of 60% (corresponding to an aqueous lithium bromide solution, vapor pressure and osmotic pressure) in the absorber 20 (see point B2). Thereafter, the water passes through the point C2, the symbol E2, the point H2, the point I2, and the point F2 to reach the state of the point J2 again, and the above is repeated.

  Here, in the example shown in FIG. 7, the temperature at which the first absorbing liquid having a 60% concentration (corresponding to a lithium bromide aqueous solution, vapor pressure and osmotic pressure) reaches a saturated water vapor pressure in an environment of 6.5 kPa is 88 ° C. It is. For this reason, the driving heat of the regenerator requires at least 90 ° C. However, in the present embodiment, as shown in FIG. 2, the temperature at which the saturated water vapor pressure of the second absorbent having a 58% concentration (corresponding to the calcium chloride aqueous solution and osmotic pressure) is obtained is 88 ° C. in an environment of 6.5 kPa pressure. Lower T (A) ° C. (see point G2). Therefore, the driving heat of the regenerator 30 is about T (A) + 5 ° C. to 10 ° C., and can be driven at a lower temperature. T (A) can be adjusted by appropriately adjusting the component and component ratio of the second absorbent. For example, when the calcium salt is the center, it can be lowered by about 10 ° C. to 20 ° C. from the first absorbing solution centered on the lithium salt, and can be further lowered by blending with other salts.

  In the above description, the heat radiation temperature in the absorber 20 and the condenser 40 is 38 degrees Celsius, which is the outside air temperature + ΔT1. Similarly, the regeneration temperature in the regenerator 30 is T (A) ° C., which is the heat source temperature −ΔT2. These ΔT1 and ΔT2 are necessary in consideration of the heat exchange efficiency of the heat exchanger, and need to be at least 5 ° C., and preferably about 10 ° C. Further, in the case of a design in which ΔT1 and ΔT2 can be increased, the heat transfer area of the heat exchanger can be reduced in inverse proportion to the size of ΔT1 and ΔT2, which can contribute to cost reduction. .

  Thus, according to the absorption system 1 according to the present embodiment, the first circulation structure R1 in which the first absorption liquid reaches the absorber 20 again from the absorber 20 through the first chamber 51, and the second absorption liquid. Constructs the second circulation structure R2 from the regenerator 30 through the second chamber 52 to the regenerator 30 again, and in this process, the refrigerant in the first absorbing liquid in the first chamber 51 passes through the semipermeable membrane 53. It reaches the second chamber 52 and is absorbed by the second absorbent in the second chamber 52. By adopting such a configuration, it is not necessary to boil and separate the refrigerant from the first absorption liquid, and it is only necessary to boil and separate the refrigerant from the second absorption liquid. For this reason, by optimizing the saturated vapor pressure and the like of the second absorbing liquid, the regenerating process can be performed at a temperature lower than the temperature when the first absorbing liquid is regenerated, and can be driven at a lower temperature. An absorption system 1 can be provided.

  Moreover, since the 2nd absorption liquid has an osmotic pressure higher than a 1st absorption liquid, it can transfer a refrigerant | coolant by forward osmosis | permeation, without pressurizing in the refrigerant transfer device 50. FIG.

  Moreover, the 1st absorption liquid contains a monovalent inorganic salt or organic salt in a main component, and the 2nd absorption liquid contains a polyvalent inorganic salt or organic salt in a main component. In particular, the first absorption liquid contains at least one of lithium bromide, lithium iodide, and lithium chloride as a main component, and the second absorption liquid includes calcium chloride, magnesium chloride, calcium bromide, magnesium bromide, odor, The main component contains at least one of zinc fluoride. By adopting such a first absorbing liquid, it is possible to ensure high absorbability with respect to water as a refrigerant, and it is possible to contribute to cost reduction by employing the second absorbing liquid.

  Next, a second embodiment of the present invention will be described. The absorption system 1 according to the second embodiment is the same as that of the first embodiment, but part of the operation is different from that of the first embodiment. Only differences from the first embodiment will be described below.

  FIG. 3 is a dueling diagram of the absorption system 1 according to the second embodiment. Note that the example shown in FIG. 3 assumes use in an area where the atmospheric temperature can be about 45 ° C., such as the Middle East and Africa.

  As shown in FIG. 3, since the atmospheric temperature can be about 45 ° C. in the above-mentioned area, the heat radiation temperature in the absorber 20 and the condenser 40 is also raised to 50 ° C. The pressure of the regenerator 30 and the condenser 40 is 12 kPa. Furthermore, in the second embodiment, the concentration of the second absorbing liquid is slightly higher than that of the first embodiment for the convenience of water molecule movement through the semipermeable membrane 53. On the other hand, although the concentration of the first absorbing liquid is also increased, since the crystallization point is close, even when concentrated (that is, at the upper limit), 63% (corresponding to an aqueous lithium bromide solution, regarding vapor pressure and osmotic pressure) It is set to be. In detail, it operates as follows.

  First, a first absorbing solution having a concentration of 63% (corresponding to an aqueous lithium bromide solution, vapor pressure and osmotic pressure) is supplied into the absorber 20 having a pressure of 1.0 kPa (see point A3). The water vapor from 10 is absorbed, and the concentration is reduced to 61% (corresponding to an aqueous lithium bromide solution, regarding vapor pressure and osmotic pressure) (see point B3). The absorbed heat here is removed by heat exchange with the atmosphere. Next, the first absorption liquid having a concentration of 61% (corresponding to an aqueous lithium bromide solution, regarding vapor pressure and osmotic pressure) is supplied to the first chamber 51 of the refrigerant transfer device 50 (see point C3). Water molecules move from the osmotic pressure difference to the second chamber 52 (see symbol E3), and the first absorbent again has a concentration of 63% (corresponding to a lithium bromide aqueous solution, regarding vapor pressure and osmotic pressure) (see point D3). . Thereafter, the absorption system 1 moves water molecules to the second chamber 52 as indicated by reference numeral E3 while repeating the cycle of points A3 to D3.

  On the other hand, the regenerator 30 (12 kPa pressure) is supplied with a second absorbing solution having a concentration of 57% (corresponding to an aqueous calcium chloride solution, regarding osmotic pressure) (see point F3). The second absorbent having a concentration of 57% (corresponding to an aqueous calcium chloride solution and osmotic pressure) is heated to T (B) ° C. in the regenerator 30 to boil and separate water vapor, and has a concentration of 60% (calcium chloride aqueous solution). (Refer to point G3). The second absorbing liquid whose concentration has increased to 60% (corresponding to the calcium chloride aqueous solution and osmotic pressure) is supplied to the second chamber 52 of the refrigerant transfer device 50 (see point H3). In the refrigerant transfer device 50, water molecules move to the second chamber 52 due to the osmotic pressure difference (see symbol E3), and the second absorbent again has a concentration of 57% (corresponding to an aqueous calcium chloride solution, regarding osmotic pressure) (see point I3). ). Thereafter, the absorption system 1 receives water molecules in the second chamber 52 as indicated by reference numeral E3 while repeating the cycle from point F3 to point I3.

The water vapor generated in the regenerator 30 reaches the condenser 40 and is cooled to 50 ° C. by the heat exchange with the atmosphere in the condenser 40 to be liquefied (see point J3). Thereafter, water, which is a liquid refrigerant, is supplied to the evaporator 10 and vaporizes (see point K3). Thereby, the cold water for cooling will be obtained. The vaporized water is absorbed by the first absorbent at a concentration of 63% (corresponding to an aqueous lithium bromide solution, vapor pressure and osmotic pressure) in the absorber 20 (see point B3). Thereafter, the water passes through the point C3, the symbol E3, the point H3, the point I3, and the point F3 to reach the state of the point J3 again, and the above is repeated.

  Here, as shown in FIG. 3, the temperature at which the first absorbing liquid having a concentration of 63% (corresponding to an aqueous lithium bromide solution, vapor pressure and osmotic pressure) becomes saturated water vapor pressure is 110 ° C. in an environment of 12 kPa pressure. ing. For this reason, the conventional absorption refrigerator used in a high-temperature area requires at least 110 ° C. for driving heat of the regenerator. However, in the present embodiment, as shown in FIG. 3, the temperature at which the saturated water vapor pressure of the second absorbent having a concentration of 60% (corresponding to an aqueous calcium chloride solution and osmotic pressure) is 12 (T) (B) ° C (see point G3). Therefore, the driving heat of the regenerator 30 is about T (B) + 5 ° C. to 10 ° C., and can be driven at a lower temperature. T (B) can be adjusted by appropriately adjusting the component and component ratio of the second absorbent.

  Thus, according to the absorption system 1 which concerns on 2nd Embodiment, the effect similar to 1st Embodiment can be acquired.

  Furthermore, in 2nd Embodiment, the driving | operation which does not have a trouble at low temperature can be performed also in the area where atmospheric temperature becomes high, such as the Middle East and Africa.

  In particular, as shown in the example of FIG. 3, if the heat radiation temperature can be designed at about 50 ° C. or higher while supplying cold water at about 7 ° C., precious water will not be consumed by the cooling tower in the above area. An air cooler can also be realized.

  Next, a third embodiment of the present invention will be described. The absorption system according to the third embodiment is the same as that of the first embodiment, but a part of the configuration and operation is different from that of the first embodiment. Only differences from the first embodiment will be described below.

  FIG. 4 is a configuration diagram showing an absorption system according to the third embodiment. As shown in FIG. 4, the absorption system 2 according to the third embodiment is the same as that of the first embodiment, but the configurations of the regenerator 30 and the condenser 40 are different.

  As shown in FIG. 4, in the third embodiment, the regenerator 30 includes a high temperature regenerator 31 and a low temperature regenerator 32. The condenser 40 includes a high temperature condenser 41 and a low temperature condenser 42.

  The high temperature regenerator 31 heats and boils the second absorbent diluted through the refrigerant transfer device 50 to separate the refrigerant and generate an intermediate concentrated solution of the second absorbent. The low temperature regenerator 32 re-boils the intermediate concentrated solution from the high temperature regenerator 31 to separate the refrigerant and generate a concentrated solution of the second absorbent. The concentrated solution is supplied to the second chamber 52 of the refrigerant transfer device 50. The high-temperature condenser 41 condenses and liquefies the refrigerant (water vapor) separated by the high-temperature regenerator 31. The heat of condensation in the high temperature condenser 41 is used for the regeneration process in the low temperature regenerator 32. The low-temperature condenser 42 condenses and liquefies the refrigerant (water vapor) separated by the low-temperature regenerator 32. The water refrigerant obtained by these condensers 41 and 42 is supplied to the evaporator 10.

  As described above, in the third embodiment, a so-called double-effect absorption refrigerator is configured.

  FIG. 5 is a dueling diagram of the absorption system 1 according to the third embodiment. As shown in FIG. 5, in the third embodiment, the pressure in the evaporator 10 and the absorber 20 is 1.0 kPa, the pressure in the high temperature regenerator 31 and the high temperature condenser 41 is 21 kPa, and the low temperature regenerator 32 and the low-pressure condenser 42 are assumed to have a pressure of 6.5 kPa.

  As shown in FIG. 5, first, the first absorbent having a concentration of 60% (corresponding to the lithium bromide aqueous solution, vapor pressure and osmotic pressure) is supplied into the absorber 20 having a pressure of 1.0 kPa (see point A5). In the absorber 20, the water vapor from the evaporator 10 is absorbed and the concentration is reduced to 54% (corresponding to a lithium bromide aqueous solution, regarding vapor pressure and osmotic pressure) (see point B5). The absorbed heat here is removed by heat exchange with the atmosphere. Next, the 54% concentration (corresponding to the lithium bromide aqueous solution, vapor pressure and osmotic pressure) is supplied to the first chamber 51 of the refrigerant transfer device 50 (see point C5). Water molecules move from the pressure difference to the second chamber 52 (see symbol E5), and the first absorbent again has a concentration of 60% (corresponding to an aqueous lithium bromide solution, regarding vapor pressure and osmotic pressure) (see point D5). Thereafter, the absorption system 1 moves water molecules to the second chamber 52 as indicated by reference numeral E5 while repeating the cycle of points A5 to D5.

  On the other hand, a low-concentration second absorbent is supplied to the high-temperature regenerator 31 (21 kPa pressure) (see point F5). The low-concentration second absorbing liquid is heated to T (HGE) ° C. in the high-temperature regenerator 31 to boil and separate water vapor, and is concentrated to an intermediate concentration (see point G5). The second absorbing liquid whose concentration has been increased to the medium concentration is supplied to the low temperature regenerator 32 (see point H5), and is heated to T (LGE) ° C. by the heat of condensation of the high temperature condenser 41, so that the water vapor is again separated by boiling. And concentrated to a high density (see point I5). The high-concentration second absorbing liquid is supplied to the second chamber 52 of the refrigerant transfer device 50 (see point J5). In the refrigerant transfer device 50, water molecules move to the second chamber 52 due to the difference in osmotic pressure (see symbol E3), and the second absorbent becomes low again (see point K5). Thereafter, the absorption system 1 receives water molecules in the second chamber 52 as indicated by reference numeral E3 while repeating the cycle of points F5 to K3.

The water vapor generated in the high temperature regenerator 31 reaches the high temperature condenser 41 and is cooled to T (HCON) ° C. in the high temperature condenser 41 to be liquefied (see point L5). The water vapor generated in the low temperature regenerator 32 reaches the low temperature condenser 42 and is cooled to T (LCON) ° C. in the low temperature condenser 42 to be liquefied (see point M5). Thereafter, water as these liquid refrigerants is supplied to the evaporator 10 and vaporized (see point N5). Thereby, the cold water for cooling will be obtained. The vaporized water is absorbed by the first absorbent at a concentration of 60% (corresponding to an aqueous lithium bromide solution, vapor pressure and osmotic pressure) in the absorber 20 (see point B5). Thereafter, the water passes through the point C5, the symbol E5, the point J5, the point K5, the point F5, the point G5, the point H5, and the point M5 to reach the state of the point N5 again, and the above is repeated.

  Thus, according to the absorption system 2 which concerns on 3rd Embodiment, the effect similar to 1st Embodiment can be acquired.

  If it demonstrates in detail, according to 3rd Embodiment, even if it is a drive heat source of about T (HGE) degree C + 5-10 degree C, a double effect absorption refrigerator can be materialized. By setting T (HGE) to about 80 ° C. by adjusting the second absorbent, a double-effect absorption refrigerator can be established with hot water of 85 ° C. to 90 ° C. at most. The energy efficiency COP of a water / lithium bromide double effect absorption refrigerator is generally about 1.3, and can have an energy efficiency approximately twice that of a single effect (COP 0.7). In the prior art, a water / lithium bromide type double effect drive requires a heat source of at least about 120 ° C., whereas in the third embodiment, the double effect is performed at a temperature lower than the conventional single effect drive temperature. The cooling energy efficiency that uses the exhaust heat of the reciprocating engine is approximately doubled, and the cooling energy efficiency that uses solar hot water at a temperature that can coexist with the solar cell is also approximately doubled.

  Next, a fourth embodiment of the present invention will be described. The absorption system according to the fourth embodiment is the same as that of the first embodiment, but a part of the configuration and operation is different from that of the first embodiment. Only differences from the first embodiment will be described below.

  FIG. 6 is a configuration diagram showing an absorption system according to the fourth embodiment. As shown in FIG. 6, the absorption system 3 according to the fourth embodiment includes a storage unit 60 in addition to that of the first embodiment. The storage unit 60 includes a first tank (storage tank) 61 that stores the second absorbent and a second tank 62 that stores the liquid refrigerant.

  In the example shown in FIG. 6, the regenerator 30 is connected to the first tank 61. For this reason, the first tank 61 stores the second absorbing liquid concentrated by the regenerator 30. Further, the first tank 61 is connected to the second chamber 52 of the refrigerant transfer device 50. For this reason, the concentrated second absorbent stored in the first tank 61 is supplied to the second chamber 52 of the refrigerant transfer device 50.

  The condenser 40 is connected to the second tank 62. For this reason, the second tank 62 stores the liquid refrigerant liquefied by the condenser 40. Further, the second tank 62 is connected to the evaporator 10. For this reason, the liquid refrigerant stored in the second tank 62 is supplied to the evaporator 10.

  The absorption system 3 according to the fourth embodiment is the same as that shown in the first embodiment. However, since the storage unit 60 is provided, the second absorption liquid and the liquid refrigerant can be stored. Therefore, it is possible to perform the regeneration process in the regenerator 30 when there is no cooling demand and to perform the cooling without operating the regenerator 30 when there is a cooling demand. That is, in 4th Embodiment, it becomes synonymous with storing energy, and efficient energy storage can be performed. Here, when compared with the case where high-temperature water serving as a heat source is stored in a hot water tank, the temperature of the high-temperature water decreases due to heat dissipation from the hot water tank, and long-term storage becomes difficult. However, in the fourth embodiment, the high temperature water is not stored, but the concentrated second absorption liquid is stored. Therefore, it is not necessary to consider heat dissipation, and energy storage can be performed in a state where energy release is small. it can.

  Thus, according to the absorption system 3 which concerns on 4th Embodiment, the effect similar to 1st Embodiment can be acquired.

  Furthermore, according to the fourth embodiment, since the first tank 61 for storing the second absorbent is further provided, for example, when storing the second absorbent concentrated in the regenerator 30, energy is stored. It is synonymous with storing, and energy storage can be performed in a state in which energy release due to heat radiation or the like is small compared to the case of storing a heat source (for example, storing hot water in a hot water tank).

  In particular, calcium chloride and magnesium chloride are also used as antifreezing agents for roads, and can be supplied in large quantities and are inexpensive. Therefore, when a calcium chloride aqueous solution or a magnesium chloride aqueous solution is used as the second absorption liquid, a large amount of the calcium chloride aqueous solution or the magnesium chloride aqueous solution, which is the second absorption liquid that has been concentrated and regenerated, and a water refrigerant are stored and air-conditioned. It can be economically realized for long-term storage of energy.

  As described above, the present invention has been described based on the embodiments, but the present invention is not limited to the above-described embodiments, and may be modified without departing from the spirit of the present invention, and may be appropriately changed within a possible range. These techniques may be combined. Furthermore, known or well-known techniques may be combined within a possible range.

  For example, in the above embodiment, the second absorption liquid has a higher osmotic pressure than the first absorption liquid, but is not limited thereto. For example, when the second absorbent has an osmotic pressure equal to or lower than that of the first absorbent, a pressurizing mechanism may be provided for the refrigerant transfer device 50. In addition, an example of a lithium salt that is generally used as a first absorbent that is required to have a low saturated vapor pressure is given, and the lithium salt has a higher osmotic pressure because it has a higher osmotic pressure. However, the selection range of the preferred second absorbent component is narrowed, but is not limited thereto. For example, if an ionic liquid is used for a part or all of the first absorbing liquid, a low saturated vapor pressure can be realized while suppressing the osmotic pressure, and T (A), T (B), and T (HGE) can be easily lowered. Can be set.

  Furthermore, in the fourth embodiment, the concentrated second absorbing liquid after regeneration is stored. However, the present invention is not limited to this. For example, in the case where the high temperature regenerator 31 and the low temperature regenerator 32 are provided, the high temperature regeneration is performed. The intermediate concentrated solution (second absorption liquid being regenerated) from the regenerator 31 may be stored, or a structure corresponding to the refrigerant transfer device 50 is separately provided to remove the refrigerant from the second absorption liquid (that is, the regenerator 30). It may be stored in a concentrated form other than

1-3: Absorption system 10: Evaporator 20: Absorber 30: Regenerator 31: High temperature regenerator 32: Low temperature regenerator 40: Condenser 41: High temperature condenser 42: Low temperature condenser 50: Refrigerant transporter 51: 1st chamber 52: 2nd chamber 53: Semipermeable membrane 60: Storage part 61: 1st tank (storage tank)
62: Second tank R1: First circulation structure R2: Second circulation structure

Claims (5)

Evaporator that evaporates liquid refrigerant to obtain cooling effect, Absorber that absorbs vaporized refrigerant with absorption liquid and releases absorption heat, Boiling separation of absorption liquid from absorption liquid that absorbed refrigerant by external heat energy An absorptive system comprising: a regenerator for generating heat; and a condenser for radiating and condensing the boiled and evaporated refrigerant,
A refrigerant having a first chamber through which the first absorbent liquid flows, a second chamber through which a second absorbent liquid different from the first absorbent liquid flows, and a semipermeable membrane separating the first chamber and the second chamber. Equipped with a transfer device,
The absorber and the first chamber absorb the vaporized refrigerant in the first absorber in the absorber, introduce the first absorption liquid that has absorbed the refrigerant in the absorber into the first chamber, and A refrigerant is transferred to the second chamber through the semipermeable membrane, and a first circulation structure is introduced that introduces the first absorption liquid concentrated by the transfer of the refrigerant into the absorber.
The regenerator and the second chamber boil-separate the refrigerant from the second absorption liquid in the regenerator, introduce the second absorption liquid boiled and separated in the regenerator into the second chamber, and Absorbing the refrigerant from the first chamber with the second absorbing liquid through the semipermeable membrane and forming a second circulation structure for introducing the second absorbing liquid diluted by the absorption of the refrigerant into the regenerator,
The absorption system, wherein the second absorption liquid has a higher saturated vapor pressure than the first absorption liquid. The absorption system according to claim 1, wherein the second absorption liquid has a higher osmotic pressure than the first absorption liquid. The first absorption liquid contains a monovalent inorganic salt or organic salt as a main component,
The absorption system according to claim 2, wherein the second absorption liquid contains a polyvalent inorganic salt or organic salt as a main component. The first absorption liquid contains at least one of lithium bromide, lithium iodide, and lithium chloride as a main component,
The absorption system according to claim 3, wherein the second absorption liquid contains at least one of calcium chloride, magnesium chloride, calcium bromide, magnesium bromide, and zinc bromide as a main component. The absorption system according to any one of claims 1 to 4, further comprising a storage tank that stores the second absorption liquid.