JP5772172B2 - Heat recovery utilization system and heat recovery utilization method - Google Patents

Description

  The present invention relates to a heat recovery utilization system and a heat recovery utilization method.

  In recent years, heat recovery and utilization systems for recovering and using waste heat, such as heat storage devices and chemical heat pumps, have been studied.

  Generally, a heat recovery and utilization system includes a reactor filled with a chemical heat storage material that reacts reversibly with a gas, an evaporator that evaporates a gas that reacts with the chemical heat storage material, and a gas that reacts with the chemical heat storage material. Is connected to the condenser through an opening / closing mechanism. At this time, the reaction medium evaporates in the evaporator to become a reaction gas, is transferred to the reactor due to a pressure difference between the evaporator and the reactor, and the chemical heat storage material reacts with the reaction gas to dissipate heat (a heat release process). In another process, the chemical heat storage material is heated to release a reaction gas (heat storage process). In the heat storage process, the released reaction gas is transferred to the condenser due to the pressure difference between the reactor and the condenser, and cooled and condensed in the condenser to become a reaction liquid. By repeatedly performing the heat dissipation process and the heat storage process, for example, the heat stored at a low temperature can be raised in temperature and used at a high temperature output, or the heat stored at a high temperature can be increased.

  However, the operating temperature range of the heat recovery system depends on the chemical heat storage material, and there exists a lower temperature limit at which heat can be stored for each material. For example, a case where calcium sulfate is used as a chemical heat storage material, water is used as a reaction medium, and atmospheric heat of 25 degrees is used as a cooling source for water condensation. In this case, theoretically, a heat storage temperature exceeding 112 ° C. is required.

  Therefore, Patent Document 1 discloses a technique for adding an additive material to a chemical heat storage material to lower the heat storage temperature.

  However, in the configuration described in Patent Document 1, the heat dissipation temperature in the heat dissipation process also decreases as the heat storage temperature decreases. Therefore, when lowering the heat storage temperature without lowering the heat radiation temperature, it is necessary to prepare a cooling source such as a refrigerator for condensing water, which has the problem of greatly reducing the efficiency of recycling waste heat. It was.

  Therefore, in the present invention, a heat recovery and utilization system that can efficiently use waste heat by using natural energy such as ambient temperature of the atmosphere without using new energy such as a refrigerator as a cooling source. The purpose is to provide.

According to the present invention,
A first heat exchanger having a chemical heat storage material that reversibly releases heat due to a chemical reaction with the reaction medium and desorption of the reaction medium by heating, and a first heat exchanger that transfers heat to and from the chemical heat storage material. A reactor of
A second reactor having an adsorbent that reversibly releases heat by adsorption with the reaction medium and desorption of the reaction medium by heating, and a second heat exchanger that exchanges heat with the adsorbent. When,
A condenser having a heat exchanger for condensing to liquefy the reaction medium;
An evaporator having an evaporation heat exchanger for vaporizing the liquefied reaction medium;
The first reactor and the second reactor, the second reactor and the condenser, the first reactor and the evaporator are connected via an open / close mechanism, respectively. And
There is provided a heat recovery and utilization system in which the temperature of heat release due to a chemical reaction between the reaction medium and the chemical heat storage material is higher than the temperature of heating when the reaction medium is desorbed from the chemical heat storage material .

  According to the present invention, there is provided a heat recovery and utilization system that can efficiently use waste heat by using natural energy such as ambient temperature of the atmosphere without introducing new energy such as a refrigerator as a cooling source. Can be provided.

FIG. 1 is a schematic diagram showing an example of the configuration of a heat recovery and utilization system according to the present invention. FIG. 2 is a schematic diagram showing an example of a connection form in the heat storage mode of the heat recovery and utilization system of FIG. FIG. 3 is a schematic diagram illustrating an example of a connection form in the heat dissipation mode of the heat recovery utilization system of FIG. FIG. 4 is a diagram for explaining the principle of storage and heat dissipation of the chemical heat storage material, and is a pressure (P) -temperature (T) diagram showing the vapor pressure of the reaction medium B (g) at equilibrium. FIG. 5 is a schematic diagram of adsorption / desorption isotherms for explaining the adsorption / desorption of the adsorbent and the reaction gas. FIG. 6 is a schematic view illustrating the configuration of the cooling source according to the present invention. FIG. 7 is a schematic diagram showing another example of the configuration of the heat recovery utilization system according to the present invention. FIG. 8 is a schematic diagram showing an example of a connection form in the heat storage mode of the heat recovery and utilization system of FIG. FIG. 9 is a schematic diagram showing an example of a connection form in the heat dissipation mode of the heat recovery and utilization system of FIG. FIG. 10 is a schematic diagram of a configuration example of a drying apparatus for explaining a method of applying the heat recovery system according to the present invention to the drying apparatus. FIG. 11 is a schematic diagram for explaining the configuration of a conventional heat recovery and utilization system. FIG. 12 is a schematic diagram illustrating an example of a connection form in the heat storage mode of the heat recovery and utilization system in FIG. 11. FIG. 13 is a schematic diagram illustrating an example of a connection form in the heat dissipation mode of the heat recovery utilization system of FIG.

  A mode for carrying out the present invention will be described with reference to the drawings.

[First embodiment]
[Configuration of Heat Recovery Utilization System 100a]
In FIG. 1, the schematic which shows an example of a structure of the heat recovery utilization system of this invention is shown. A heat recovery system 100 in FIG. 1 includes a first reactor 1, a second reactor 2, an evaporator 6, and a condenser 5.

  The first reactor 1 has a chemical heat storage material 10 and a first heat exchanger 20 that exchanges heat with the chemical heat storage material 10. The chemical heat storage material 10 reversibly performs desorption of the reaction medium 12 (reaction gas 12a) and reaction with the reaction medium 12. When the chemical heat storage material 10 is heated, the chemical heat storage material 10 desorbs (that is, stores heat) the reaction medium. On the other hand, when the chemical heat storage material 10 reacts with the reaction medium 12, the chemical heat storage material dissipates heat (that is, outputs heat).

  The second reactor 2 has an adsorbent 11 and a second heat exchanger 21 that exchanges heat with the adsorbent 11. The adsorbent 11 reversibly desorbs the reaction medium 12 (reaction gas 12a) and adsorbs the reaction medium 12. When the adsorbent 11 is heated, the adsorbent 11 desorbs the reaction medium, and when the adsorbent 11 adsorbs the reaction medium 12, the adsorbent 11 dissipates heat.

  The evaporator 6 has an evaporation heat exchanger 23 that heats and vaporizes the reaction medium 12 (reaction medium 12b).

  The condenser 5 has a condensation heat exchanger 22 that condenses and liquefies the reaction medium 12 (reaction gas 12a) and extracts heat.

  The first reactor 1 and the second reactor 2, the second reactor 2 and the condenser 5, and the first reactor 1 and the evaporator 6 are a second opening / closing mechanism 31 and a third opening / closing mechanism, respectively. 32, connected by a pipe 7 through a first opening / closing mechanism 30.

  Further, the reaction liquid 12 b condensed in the condenser 5 is moved to the evaporator 6. As an example of the moving means, for example, as shown in FIG. 1, it is achieved by providing a pump 8 and a fourth opening / closing mechanism 33 in a pipe between the condenser 5 and the evaporator 6. At this time, in the evaporator 6, the moved reaction liquid 12b is evaporated by a method of dropping and evaporating on the evaporating heat exchanger 23, a method of spraying and evaporating on the evaporating heat exchanger 23, or the like.

  The first opening / closing mechanism 30, the second opening / closing mechanism 31, the third opening / closing mechanism 32, and the fourth opening / closing mechanism 33 are not particularly limited as long as they can be freely opened and closed. Specifically, an opening / closing valve or the like can be used. .

  Although it does not specifically limit as the reaction medium 12, It is preferable to use water (water vapor | steam) from an environmental viewpoint. In addition, a mixture of water and alcohol can be used.

  The chemical heat storage material is not particularly limited as long as it can reversibly desorb the reaction medium 12 (reaction gas 12a) and react with the reaction medium 12. When water vapor (water) is used as the reaction medium, it has one or more compounds selected from the group consisting of calcium oxide, magnesium oxide, calcium chloride, manganese chloride, magnesium chloride, calcium sulfate, and sodium carbonate. Is preferred.

  Furthermore, the adsorbent preferably contains either zeolite or silica gel.

[Heat recovery utilization method using heat recovery utilization system 100a]
Next, a heat recovery utilization method using the heat recovery utilization system 100a which is an embodiment of the present invention will be described. Table 1 shows a combination example of the open / close state of the open / close mechanism in the heat recovery utilization system of the present invention. FIG. 2 is a schematic diagram showing an example of a connection form in the heat storage mode of the heat recovery and utilization system of FIG. Further, FIG. 3 is a schematic diagram showing an example of connection form in the heat dissipation mode of the heat recovery and utilization system of FIG.

表１におけるサイクルＡでは、図２に示すように、熱回収利用システム１００ａは、廃熱源６０ａ及び冷却源６２ａと熱的に接続される。第一の反応器１内の化学蓄熱材１０は、第一の熱交換器２０を介して加熱され、反応気体１２ａを脱離する。一方、第二の反応器２内の吸着剤１１は、反応気体１２ａを吸着して発熱する。この時、吸着剤１１は、冷却源６２ａにより第二の熱交換器２１を介して冷却され、吸着が促進される。

In cycle A in Table 1, as shown in FIG. 2, the heat recovery and utilization system 100a is thermally connected to the waste heat source 60a and the cooling source 62a. The chemical heat storage material 10 in the first reactor 1 is heated via the first heat exchanger 20 to desorb the reaction gas 12a. On the other hand, the adsorbent 11 in the second reactor 2 adsorbs the reaction gas 12a and generates heat. At this time, the adsorbent 11 is cooled by the cooling source 62a via the second heat exchanger 21, and the adsorption is promoted.

  In cycle B in Table 1, as shown in FIG. 3, the heat recovery and utilization system 100a is thermally connected to the waste heat sources 60a and 60b, the cooling source 62b, and the heating load 61a. The reaction liquid 12b in the evaporator 6 is heated and vaporized, and is supplied to the first reactor 1 as a reaction gas 12a. The chemical heat storage material 10 in the first reactor 1 reacts with the supplied reaction gas 12a to generate heat, and the heating output is supplied to the heating load 61a through the first heat exchanger 20. On the other hand, the adsorbent 11 in the second reactor 2 is heated by the waste heat source 60b via the second heat exchanger 21, and the reaction gas 12a is desorbed. The desorbed reaction gas 12a is supplied to the condenser 5, cooled by the cooling source 62b via the condenser heat exchanger 22, and liquefied to become the reaction liquid 12b.

  That is, in cycle A, the chemical heat storage material 10 releases the reaction gas 12a due to waste heat input and enters a heat storage state. In cycle B, the chemical heat storage material 10 reacts with the reaction gas 12a and enters a heat dissipation state. By repeating this, the heat storage and recovery of waste heat and the use of heat dissipation in the reverse process become possible.

  The method of thermally connecting the heat recovery utilization system 100a to the waste heat source, the cooling source, and the heating load is not particularly limited, and examples thereof include a method of transporting a heat medium using a transport means such as a pump. It is done. When switching between the cycle A and the cycle B by operating the opening / closing mechanism, connection switching between the heat recovery utilization system 100a and the waste heat source, the cooling source, and the heating load is required. However, when the heat connection is transported by the above-described heat medium, the heat connection corresponding to cycle A and cycle B can be switched by switching the flow path of the heat medium.

[Thermal storage principle at a low-temperature heat source using the heat recovery utilization system 100a]
In the process of cycle B, the evaporator 6 is heated by the waste heat source 60a to increase the pressure of the reaction gas 12a in the evaporator. Thereby, the heat generation temperature in the reaction between the chemical heat storage material 10 and the reaction gas 12a in the first reactor 1 can be made higher than the input temperature by the waste heat source 60a (utilization of temperature increase). In the present embodiment, in the process of cycle A, heat can be stored in the chemical heat storage material 10 using a low-temperature heat source by utilizing the adsorption phenomenon of the reaction gas 12a by the adsorbent 11.

  In order to store the chemical heat storage material 10 with a low-temperature heat source, it is generally necessary to cool and liquefy the reaction gas 12a desorbed from the chemical heat storage material 10, which requires a cooling source such as a refrigerator. However, the configuration as in the present embodiment enables low-temperature heat storage to the chemical heat storage material 10 using natural energy such as ambient temperature of the atmosphere as a cooling source. That is, the heat storage temperature of the chemical heat storage material 10 can be lowered.

  FIG. 4 is a diagram for explaining the principle of chemical heat storage material storage and heat dissipation, and shows a pressure (P) -temperature (T) diagram showing the vapor pressure of the reaction medium B (g) at equilibrium. The horizontal axis represents the reciprocal of temperature, and the vertical axis represents the logarithm of vapor pressure.

  The line X in FIG. 4 shows the relationship between the temperature of the reaction material and the vapor pressure of the reaction medium B (g) at the time of equilibrium of the following formula (1), and the line Y shows the reaction in the following formula (2). The saturated vapor pressure of the medium B (g) is shown. In the formulas (1) and (2), the activity of the solid and liquid is assumed to be 1.

A + B (g) ⇔AB Formula (1)
B (l) ⇔B (g) Equation (2)
In FIG. 4, the chemical heat storage material 10 reacts with the reaction gas 12a to generate heat under the temperature and pressure conditions on the right side of the line X. On the other hand, under the temperature and pressure conditions on the left side of the line X, heat is absorbed and the desorption reaction of the reaction gas 12a proceeds. In general, a case where the heat release temperature is higher than the heat storage temperature as shown in FIG. 4A is called a temperature raising mode, and a case where the heat release temperature is lower than the heat storage temperature as shown in FIG. 4B. This is called the heat increase mode.

FIG. 5 shows a schematic diagram of the adsorption / desorption isotherm for explaining the adsorption / desorption of the adsorbent and the reaction gas. The horizontal axis of FIG. 5 shows the relative pressure P / P ₀ , which is the ratio of “the pressure P of the reaction gas 12a in the system” and “the saturation pressure P ₀ of the reaction gas 12a” at a certain temperature. Indicates the weight of the reaction liquid 12b on which the adsorbent can be adsorbed. In the present system, on the adsorption isotherm, first, there is a portion where the relative pressure is 0 to a steep slope, and then gradually shifts to a gentle slope. At this time, the relative pressure at the point where the gradient becomes the largest is called the boundary relative pressure. As shown in FIG. 5, when the relative pressure is lower than a certain boundary relative pressure, the reaction gas 12a is desorbed from the adsorbent. On the other hand, when the relative pressure is higher than a certain boundary relative pressure, the adsorbent adsorbs the reaction gas 12a. The boundary relative pressure can be controlled by those skilled in the art depending on the material design of the adsorbent, and can be set to 0.17, for example.

Although an example of temperature conditions in the case where a material having a boundary relative pressure of 0.17 is used as the adsorbent 11 and calcium sulfate is used as the chemical heat storage material 10 is shown, the present invention is not limited to this. In the cycle A, the “pressure P of the reaction gas 12a in the system” depends on the temperature in the system (≈the temperature of the chemical heat storage material 10), and when the temperature of the chemical heat storage material 10 is 90 degrees, At times 0.96 kPa is assumed. On the other hand, when it is assumed that the ambient temperature is 30 ° C. and this is the temperature of the adsorbent 11, the “saturation pressure P ₀ of the reaction gas 12a” is 4.24 kPa. At this time, the relative pressure is 0.226, which is larger than the boundary relative pressure 0.17. At this time, the adsorbent 11 adsorbs the reaction gas 12a, and the desorption of the reaction gas 12a from the chemical heat storage material 10 is promoted on the first reactor 1 side. That is, the heat storage of the chemical heat storage material 10 proceeds.

  As described above, the chemical heat storage material 10 that has been stored at low temperature in the process of cycle A generates heat at a high temperature by increasing the pressure of the reaction gas 12a in the process of cycle B in the apparatus configuration shown in FIG. In parallel with the high temperature heat generation of the chemical heat storage material 10, the adsorbent 11 in the second reactor 2 is heated by the waste heat source 60b to desorb the reaction gas 12a. The desorbed reaction gas 12a is cooled and liquefied by the cooling source 62b through the condenser heat exchanger 22 in the condenser 5, and the reaction gas 12a desorbed from the chemical heat storage material 10 is removed in the process of the next cycle A. Adsorb.

  The waste heat sources 60a and 60b may be independent individual heat sources, or may be configured to use, for example, cascade use of heat extracted from one waste heat source by circulation of the heat medium.

  FIG. 6 is a schematic view illustrating the configuration of a cooling source that can be used in the present invention. As the cooling source, for example, a configuration in which room temperature air 52 is circulated through the duct 53 by the fan 51 and is carried by the gas-liquid heat exchanger 50 installed in the duct 53 can be used, but the present invention is not limited to this.

[Second Embodiment]
[Configuration of Heat Recovery Utilization System 100b]
In FIG. 7, the schematic which shows the other example of a structure of the heat recovery utilization system which concerns on this invention is shown. The heat recovery system 200 of FIG. 7 further includes a third reactor 3 and a fourth reactor 4 in the system of FIG.

  The third reactor 3 has a chemical heat storage material 10 and a third heat exchanger 24 that exchanges heat with the chemical heat storage material 10. The chemical heat storage material 10 reversibly performs desorption of the reaction medium 12 (reaction gas 12a) and reaction with the reaction medium 12. When the chemical heat storage material 10 is heated, the chemical heat storage material 10 desorbs (that is, stores heat) the reaction medium. On the other hand, when the chemical heat storage material 10 reacts with the reaction medium 12, the chemical heat storage material dissipates heat (that is, outputs heat).

  The fourth reactor 4 has an adsorbent 11 and a fourth heat exchanger 25 that exchanges heat with the adsorbent 11. The adsorbent 11 reversibly desorbs the reaction medium 12 (reaction gas 12a) and adsorbs the reaction medium 12. When the adsorbent 11 is heated, the adsorbent 11 desorbs the reaction medium, and when the adsorbent 11 adsorbs the reaction medium 12, the adsorbent 11 dissipates heat.

  The evaporator 6 and the third reactor 3, the third reactor 3 and the fourth reactor 4, the fourth reactor 4 and the condenser 5 are a fifth opening / closing mechanism 34 and a sixth opening / closing mechanism, respectively. 35, connected by a pipe 7 via a seventh opening / closing mechanism 36.

[Heat recovery utilization method using heat recovery utilization system 100b]
Next, a heat recovery and utilization method using a heat recovery and utilization system 100b according to another embodiment of the present invention will be described. Table 2 shows a combination example of the open / close state of the open / close mechanism in the heat recovery utilization system 100b.

熱回収利用システム１００ｂは、表２に示す開閉機構の開閉状態の組み合わせにより、サイクルＣとサイクルＤの二つのモードで動作する。各々モードでの動作は、図１のシステムと同様であり、図１のシステム１００では、化学蓄熱材１０の蓄熱と放熱を交互に行う形態であるのに対して、図７のシステム２００では、蓄熱と放熱の交互動作する手段を２つ有し、各々が補完し合って蓄熱と放熱を連続して行うことが可能である。

The heat recovery and utilization system 100b operates in two modes, cycle C and cycle D, depending on the combination of the open / close states of the open / close mechanisms shown in Table 2. The operation in each mode is the same as the system of FIG. 1. In the system 100 of FIG. 1, heat storage and heat dissipation of the chemical heat storage material 10 are alternately performed, whereas in the system 200 of FIG. It is possible to have two means for alternately performing heat storage and heat dissipation, each of which complements each other and continuously performs heat storage and heat dissipation.

  In FIG. 8, the schematic which shows the connection example in the heat storage mode of the heat recovery utilization system of FIG. 7 is shown. Further, FIG. 9 is a schematic view showing an example of connection form in the heat dissipation mode of the heat recovery and utilization system of FIG. The heat recovery utilization system 100b is thermally connected to the waste heat sources 60a, 60b, 60c, the cooling sources 62a, 62b, and the heating load 61a. The method of thermally connecting is not particularly limited, as in the case of the heat recovery and utilization system 100a, and examples thereof include a method of transporting a heat medium using a transport means such as a pump.

  In the cycle C shown in FIG. 8, the chemical heat storage material 10 in the first reactor 1 is heated via the first heat exchanger 20 by the waste heat source 60a to desorb the reaction gas 12a. On the other hand, the adsorbent 11 in the second reactor 2 adsorbs the reaction gas 12a and generates heat. At this time, the adsorbent 11 is cooled by the cooling source 62a via the second heat exchanger 21, and the adsorption is promoted. Moreover, in the evaporator 6, the reaction liquid 12b is heated and vaporized, and is supplied to the 3rd reactor 3 as the reaction gas 12a. In the third reactor 3, the chemical heat storage material 10 reacts with the reaction gas 12 a supplied to generate heat, and the heating output is supplied to the heating load 61 a through the third heat exchanger 24. The adsorbent 11 in the fourth reactor 4 is heated by the waste heat source 60c via the fourth heat exchanger 25, and the reaction gas 12a is desorbed. The desorbed reaction gas 12a is supplied to the condenser 5, and cooled and liquefied by the cooling source 62b via the condenser heat exchanger 22 to become the reaction liquid 12b.

  In cycle D shown in FIG. 9, the chemical heat storage material 10 in the third reactor 3 is heated via the third heat exchanger 24 by the waste heat source 60a to desorb the reaction gas 12a. In the fourth reactor 4, the adsorbent 11 adsorbs the reaction gas 12b and generates heat. Since the adsorbent 11 is cooled by the cooling source 62a via the fourth heat exchanger 25, the adsorption is promoted. In the evaporator 6, the reaction liquid 12b is heated and vaporized, and is supplied to the first reactor 1 as the reaction gas 12a. In the first reactor 1, the chemical heat storage material 10 reacts with the supplied reaction gas 12 a to generate heat, and a heating output is supplied to the heating load 61 a through the first heat exchanger 20. In the second reactor 2, the adsorbent 11 is heated via the second heat exchanger 21 by the waste heat source 60c, and the reaction gas 12a is desorbed. The desorbed reaction gas 12a is supplied to the condenser 5, and cooled and liquefied by the cooling source 62b via the condenser heat exchanger 22 to become the reaction liquid 12b.

  That is, in cycle C, the chemical heat storage material 10 in the first reactor 1 releases the reaction gas 12a by the waste heat input to enter the heat storage state, and the chemical heat storage material 10 in the third reactor 3 reacts. It reacts with the gas 12a and enters a heat dissipation state. In cycle D, the chemical heat storage material 10 in the third reactor 3 releases the reaction gas 12a to be in a heat storage state, and the chemical heat storage material 10 in the first reactor 1 reacts with the reaction gas 12a. And it becomes a heat dissipation state. By repeating cycles C and D and operating alternately, continuous operation in the heat dissipation process and continuous operation in the heat storage process can be achieved.

  In the heat recovery and utilization system 100b, the evaporator 6 is heated by the waste heat source 60b to increase the pressure of the reaction gas 12a in the container. Thereby, the heat_generation | fever temperature in reaction of the chemical thermal storage material 10 and the reaction gas 12a can be made higher than the temperature of the waste heat source 60a used for heat storage (temperature rising utilization). In the present embodiment, by further utilizing the adsorption phenomenon of the reaction gas 12a by the adsorbent 11, it is possible to store heat in the chemical heat storage material 10 with a low-temperature heat source.

  In order to store the chemical heat storage material 10 with a low-temperature heat source, it is generally necessary to cool and liquefy the reaction gas 12a desorbed from the chemical heat storage material 10, which requires a cooling source such as a refrigerator. However, the configuration as in the present embodiment enables low-temperature heat storage to the chemical heat storage material 10 using natural energy such as ambient temperature of the atmosphere as a cooling source. That is, the heat storage temperature of the chemical heat storage material 10 can be lowered.

  The principle of the low-temperature heat storage is the same as that of the heat recovery system 100 in FIG. 1 described above, and therefore the description is omitted here.

  The waste heat sources 60a, 60b, and 60c may be independent individual heat sources, or may be configured to use, for example, cascade use of heat extracted from one waste heat source by heat medium circulation.

  As in the case of the heat recovery system 100 described above, the cooling source uses a configuration in which, for example, room temperature air 52 is circulated through the duct 53 by the fan 51 and is carried by the gas-liquid heat exchanger 50 installed in the duct 53. However, the present invention is not limited to this.

[Drying equipment]
In FIG. 10, the schematic of the structural example of a drying apparatus for demonstrating the method of applying the heat recovery system 100 of this invention to a drying apparatus is shown. In the present embodiment, the drying air 52 is heated by the hot air generating heat exchanger 70 with the generated heat of the heating source 65 through the duct 53, and then guided to the drying chamber 72 to exhaust the material to be dried after drying. An example of the drying apparatus 200 will be described. Further, as the cooling source, it is assumed that the above-described form of FIG. 6 is used.

  In the following description, it is assumed that the waste heat source 60a in a separate process from the drying apparatus 200 is used, but the heat recovered by the waste heat recovery heat exchanger 71 is cascaded for the waste heat source 60a. It is also possible.

  The heat recovery and utilization system 100 a is thermally connected to the drying device 200 via the heat medium flow path 81. In switching between cycle A and cycle B, flow path switching valves 80 a, 80 b, 80 c, 80 d, 80 e, 80 f, 80 g, and 80 h are installed in the heat medium flow path 81.

  In the cycle A, the heat medium flow path 81 indicated by a solid line in FIG. The first reactor 1 and the second reactor are connected to a waste heat recovery heat exchanger 71 and a gas-liquid heat exchanger 50, respectively. The chemical heat storage material 10 in the first reactor 1 is heated and stored with heat recovered by the waste heat recovery heat exchanger 71.

  After the heat storage is completed, the operation shifts to cycle B. At this time, as indicated by a dotted line in FIG. 10, the first reactor 1 is used as the heat exchanger 70 for generating hot air, the second reactor 2 is used as the heat exchanger 71 for recovering waste heat, and the condenser 5 is used. Are connected to the gas-liquid heat exchanger 50, and the evaporator 6 is connected to the waste heat source 60a. By auxiliary heating of the heat exchanger 70 for generating hot air with the heat output of the chemical heat storage material 10, the energy consumption of the heating source 65 of the drying apparatus 200 can be reduced.

  Hereinafter, based on an Example, this invention is demonstrated concretely.

[Example 1]
The heat recovery utilization system 100a shown in FIG. 1 was operated by switching the conditions of cycles A and B shown in Table 1. The connection form of the external waste heat source, the cooling source, and the heating load is the connection form of FIG. 2 in the cycle A and the connection form of FIG. 3 in the cycle B. The heat connection was switched by switching the flow path of the heat medium using a flow path switching valve (not shown).

  Calcium sulfate was used for the chemical heat storage material 10, a zeolite-based adsorbent having a boundary relative pressure of 0.17 was used for the adsorbent 11, and water was used for the reaction medium 12.

  In the operation of the heat recovery utilization system 100a, the heat medium at 97 ° C. obtained by heating the waste heat source 60a is supplied to the heat recovery utilization system 100a, and the heat medium that can be input to the heating load 61a in the process of cycle B The temperature of was measured. The cooling sources 62a and 62b supplied the heat medium at 23 ° C. to the heat recovery utilization system 100a using the gas-liquid heat exchanger 50 having the configuration shown in FIG. In cycle B, the evaporator 6 is heated by the 97 ° C. input heat medium from the waste heat source 60a, and the input heat medium whose temperature has dropped by 5 ° C. due to the heat exchange in the evaporator 6 is subjected to the second heat exchange. It was made to distribute | circulate to the container 2. That is, by using the waste heat in cascade, the waste heat source 60a has the function of the waste heat source 60b.

[Example 2]
The heat recovery utilization system 100b shown in FIG. 7 was operated by changing the conditions of cycles C and D in Table 2. The connection form of the external waste heat source, the cooling source, and the heating load is the connection form of FIG. 8 in cycle C and the connection form of FIG. 9 in cycle D. The heat connection was switched by switching the flow path of the heat medium using a flow path switching valve (not shown).

  As in Example 1, the chemical heat storage material 10 uses calcium sulfate, the adsorbent 11 uses a zeolite-based adsorbent having a boundary relative pressure of 0.17, and the reaction medium 12 contains water. Using.

  In the operation of the heat recovery and utilization system 100b, a heat medium of 97 ° C. obtained by heating the waste heat source 60a is supplied to the heat recovery and utilization system 100b, and in the process of cycle D, a heat medium that can be continuously input to the heating load 61a. The temperature was measured. In cycle C, the 97 ° C. input heat medium from the waste heat source 60 a was circulated in the order of the first reactor 1, the evaporator 6, and the fourth reactor 4. That is, by using waste heat in cascade, the waste heat source 60a has the functions of the waste heat source 60b and the waste heat source 60c. In cycle D, the 97 ° C. input heat medium from the waste heat source 60 a was circulated in the order of the third reactor 3, the evaporator 6, and the second reactor 2. That is, by using waste heat in cascade, the waste heat source 60a has the functions of the waste heat source 60b and the waste heat source 60c.

[Comparative Example 1]
In FIG. 11, the schematic for demonstrating the structure of the conventional heat recovery utilization system 100c is shown. The heat recovery utilization system 100 c includes a first reactor 1, an evaporator 6, and a condenser 5.

  The first reactor 1 has a chemical heat storage material 10 and a first heat exchanger 20 that exchanges heat with the chemical heat storage material 10. The chemical heat storage material 10 reversibly performs desorption of the reaction medium 12 (reaction gas 12a) and reaction with the reaction medium 12. When the chemical heat storage material 10 is heated, the chemical heat storage material 10 desorbs (that is, stores heat) the reaction medium. On the other hand, when the chemical heat storage material 10 reacts with the reaction medium 12, the chemical heat storage material dissipates heat (that is, outputs heat).

  The evaporator 6 has an evaporation heat exchanger 23 that heats and vaporizes the reaction medium 12 (reaction medium 12b).

  The condenser 5 has a condensation heat exchanger 22 that condenses and liquefies the reaction medium 12 (reaction gas 12a) and extracts heat.

  The first reactor 1 and the evaporator 6, and the first reactor 1 and the condenser 6 were connected by a first opening / closing mechanism 30 and an eighth opening / closing mechanism 37, respectively. Further, the pump 8 and the fourth opening / closing mechanism 33 are provided in a pipe between the condenser 5 and the evaporator 6.

  This heat recovery utilization system 100c was operated by switching the conditions of cycles E and F shown in Table 3. FIG. 12 shows an example of a connection form in the heat storage mode of the heat recovery use system of FIG. 11, and FIG. 13 shows an example of a connection form in the heat dissipation mode of the heat recovery use system of FIG. An external waste heat source, a cooling source, and a heating load were connected as in the connection form shown in FIGS. The heat connection was switched by switching the flow path of the heat medium using a flow path switching valve (not shown).

  Calcium sulfate was used for the chemical heat storage material 10 and water was used for the reaction medium 12.

熱回収利用システム１００ｃの運転においては、廃熱源６０ａの加熱により得られた９７℃の熱媒を熱回収利用システム１００ｃへ供給し、サイクルＦの過程において、加熱負荷６１ａへ入力できる熱媒体の温度を計測した。なお、冷却源６２ａは、図６で示した形態の気液熱交換器５０を使用して、熱回収利用システム１００ｃに対して２３℃の熱媒を供給した。また、サイクルＦにおいては、廃熱源６０ａからの９７℃の入力熱媒により蒸発器６を加熱した。

In the operation of the heat recovery and utilization system 100c, the temperature of the heat medium that can be input to the heating load 61a in the process of cycle F by supplying the heat medium of 97 ° C. obtained by heating the waste heat source 60a to the heat recovery and utilization system 100c. Was measured. In addition, the cooling source 62a supplied the heat medium of 23 degreeC with respect to the heat recovery utilization system 100c using the gas-liquid heat exchanger 50 of the form shown in FIG. Further, in cycle F, the evaporator 6 was heated by the 97 ° C. input heat medium from the waste heat source 60a.

[Comparative Example 2]
As a cooling source 62a of Comparative Example 1, a cooling device capable of generating and supplying a 1 ° C. cooling medium was used, and a 1 ° C. heating medium was supplied to the heat recovery utilization system 100c. According to the process, the temperature of the heat medium that can be input to the heating load 61a was measured.

  Table 4 shows the measurement results of the temperature of the heat medium that can be input to the heating load 61a in each example and each comparative example.

実施例１及び２においては、９７℃の低温の熱媒入力によっても、化学蓄熱材１０の蓄熱が行うことができ、逆過程において、実施例１では間欠的な１７５℃の、実施例２では連続した１７０℃の昇温出力が得られた。これは、本発明における、吸着剤１１の効果によるものである。実施例１及び２においては、新規エネルギーが必要となる冷却源を使用せず、図６に示す形態の室温空気５２による冷却により、十分な蓄熱効果を奏することができる。

In Examples 1 and 2, heat storage of the chemical heat storage material 10 can be performed even by a low-temperature heat medium input of 97 ° C., and in the reverse process, in Example 1, the temperature is intermittent at 175 ° C. A continuous heating output of 170 ° C. was obtained. This is due to the effect of the adsorbent 11 in the present invention. In Examples 1 and 2, a sufficient heat storage effect can be achieved by cooling with room temperature air 52 in the form shown in FIG. 6 without using a cooling source that requires new energy.

  On the other hand, in Comparative Example 1, heat storage to the chemical heat storage material 10 in the cycle A cannot be performed without a cooling source by introducing new energy. Therefore, the heat radiation output could not be obtained even in the reverse process.

  In Comparative Example 2, the same low-temperature heat storage and temperature rising output as in Example 1 were obtained, but a cooling source using new energy input was necessary, and it was not put into practical use from the viewpoint of heat recovery utilization.

DESCRIPTION OF SYMBOLS 1 1st reactor 2 2nd reactor 3 3rd reactor 4 4th reactor 5 Condenser 6 Evaporator 7 Piping 8 Pump 10 Chemical heat storage material 11 Adsorbent 12 Reaction medium 20 1st heat exchange Unit 21 Second heat exchanger 22 Condensing heat exchanger 23 Evaporating heat exchanger 30 First switching mechanism 31 Second switching mechanism 32 Third switching mechanism 33 Fourth switching mechanism 100a, 100b, 100c Collection and utilization system

JP 2009-186119 A

Claims (4)

A first heat exchanger having a chemical heat storage material that reversibly releases heat due to a chemical reaction with the reaction medium and desorption of the reaction medium by heating, and a first heat exchanger that transfers heat to and from the chemical heat storage material. A reactor of
A second reactor having an adsorbent that reversibly releases heat by adsorption with the reaction medium and desorption of the reaction medium by heating, and a second heat exchanger that exchanges heat with the adsorbent. When,
A condenser having a heat exchanger for condensing to liquefy the reaction medium;
An evaporator having an evaporation heat exchanger for vaporizing the liquefied reaction medium;
The first reactor and the second reactor, the second reactor and the condenser, the first reactor and the evaporator are connected via an open / close mechanism, respectively. And
The temperature of heat release due to a chemical reaction between the reaction medium and the chemical heat storage material is higher than the temperature of heating when the reaction medium is desorbed from the chemical heat storage material ,
Heat recovery system. A first heat exchanger having a chemical heat storage material that reversibly releases heat by reaction with the reaction medium and desorption of the reaction medium by heating, and a first heat exchanger that transfers heat to and from the chemical heat storage material. A reactor,
A second reactor having an adsorbent that reversibly releases heat by adsorption with the reaction medium and desorption of the reaction medium by heating, and a second heat exchanger that exchanges heat with the adsorbent. When,
A third heat exchanger having a chemical heat storage material that reversibly releases heat by reaction with the reaction medium and desorption of the reaction medium by heating, and a third heat exchanger that transfers heat to and from the chemical heat storage material. A reactor,
A fourth reactor comprising an adsorbent that reversibly releases heat by adsorption with the reaction medium and desorption of the reaction medium by heating, and a fourth heat exchanger that exchanges heat with the adsorbent. When,
A condenser having a heat exchanger for condensing to liquefy the reaction medium;
An evaporator having an evaporation heat exchanger for vaporizing the liquefied reaction medium;
The first reactor and the second reactor, the second reactor and the condenser, the first reactor and the evaporator, the third reactor and the fourth The reactor, the fourth reactor and the condenser, the third reactor and the evaporator, respectively, are connected via an open / close mechanism ,
A heat recovery and utilization system in which a temperature of heat radiation by a chemical reaction between the reaction medium and the chemical heat storage material is higher than a heating temperature when the reaction medium is desorbed from the chemical heat storage material . The chemical heat storage material has one or two or more compounds selected from the group of calcium oxide, magnesium oxide, calcium chloride, manganese chloride, magnesium chloride, calcium sulfate, sodium carbonate,
The adsorbent contains either zeolite or silica gel,
The heat recovery utilization system according to claim 1 or 2, wherein the reaction medium is water. A first heat exchanger having a chemical heat storage material that reversibly releases heat due to a chemical reaction with the reaction medium and desorption of the reaction medium by heating, and a first heat exchanger that transfers heat to and from the chemical heat storage material. A reactor of
A second reactor comprising: an adsorbent that reversibly releases heat by adsorption with the reaction medium and desorption of the reaction medium by heating; and a second heat exchanger that exchanges heat with the adsorbent. ,
A condenser having a heat exchanger for condensing to liquefy the reaction medium;
An evaporator having an evaporation heat exchanger for vaporizing the liquefied reaction medium;
Have a temperature of the heat dissipation due to a chemical reaction between the chemical heat storage material and the reaction medium, the reaction medium from the chemical thermal storage medium in usage of high heat recovery and utilization system than the temperature of the heating when desorbing There,
The first reactor and the second reactor have the same atmosphere through an opening / closing mechanism,
The chemical heat storage material chemically reacted with the reaction medium is heated through the first heat exchanger with heat from a waste heat source to desorb the reaction medium, thereby storing heat from the waste heat source, A first step of promoting the heat storage by cooling the adsorbent through the second heat exchanger and adsorbing the reaction medium;
The first reactor and the evaporator have the same atmosphere through an opening and closing mechanism;
The second reactor and the condenser have the same atmosphere through an opening and closing mechanism;
The adsorbent is heated through the second heat exchanger to desorb the reaction medium, and the desorbed reaction medium is liquefied by the condensation heat exchanger,
The reaction medium in the evaporator is vaporized by an evaporation heat exchanger, the vaporized reaction medium and the chemical heat storage material are chemically reacted to generate heat, and the heat generated through the first heat exchanger is generated. A second step of outputting
A third step of transporting the reaction medium in the condenser to the evaporator;
A heat recovery utilization method comprising:

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