JP2004011928A - Absorption refrigerator - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a highly efficient absorption refrigerator with low operating pressure by improving a circulation route of absorbent solution, to eliminate a confluence causing a large pressure difference in a pipe, and to provide a stable solution circulation. <P>SOLUTION: Dilute solution La produced from an absorber A is branched, one is made to inflow in a high-temperature regenerator G<SB>3</SB>, the high-temperature and -concentration solution L<SB>3</SB>flowing out by heated and concentrated in a high-temperature regenerator G<SB>3</SB>inflows in a low-temperature regenerator G<SB>1</SB>, and the rest inflows in a middle-temperature regenerator G<SB>2</SB>. This constitution can set low the concentration of the absorbent solution in the middle-temperature regenerator G<SB>2</SB>and set low the temperature of refrigerant vapor in the high-temperature regenerator G<SB>3</SB>(namely, set the operating pressure low). The high-temperature and -concentration solution L<SB>3</SB>from the high-temperature regenerator G<SB>3</SB>is made to inflow in the low-temperature regenerator G<SB>1</SB>so as to eliminate the confluence causing the large pressure difference in the pipe. <P>COPYRIGHT: (C)2004,JPO

Description

[0001]
TECHNICAL FIELD OF THE INVENTION
The present invention relates to an absorption refrigeration apparatus, and more particularly to an absorption refrigeration apparatus including three regenerators having different operating temperatures.
[0002]
[Prior art]
Generally, an absorption refrigeration system has a condenser, an evaporator, an absorber, a solution heat exchanger, and a regenerator as basic components, and these components are sequentially and operatively connected by a solution piping system and a refrigerant piping system. It is composed.
[0003]
In such an absorption refrigeration apparatus, the diluted solution generated in the absorber is heated and concentrated in a regenerator to form a concentrated solution, which is further refluxed to the absorber, while the concentrated solution is heated and concentrated in the regenerator. The generated refrigerant vapor is condensed by a condenser into a liquid refrigerant, and the liquid refrigerant is evaporated in an evaporator, and the generated refrigerant vapor is absorbed in a concentrated solution in the absorber to generate a dilute solution. Thus, a circulation cycle of the absorbing solution and the refrigerant is realized.
[0004]
In this case, from the viewpoint of increasing the thermal efficiency of the refrigeration system by heat recovery, it is customary to perform heat exchange between the heated concentrated solution flowing out of the regenerator and the dilute solution flowing into the regenerator. .
[0005]
[Problems to be solved by the invention]
By the way, it is known that the most effective way to improve the performance of an absorption refrigeration system is to increase the thermal efficiency of a solution / refrigerant circulation system. It has been proposed to provide the heat of one external heat source repeatedly. That is, a plurality of regenerators having different operating temperatures are provided, and refrigerant vapor generated by heating a high-temperature regenerator operating at a high temperature is introduced into a low-temperature regenerator operating at a low temperature, and is introduced into the low-temperature regenerator. It is used as a heat source for heating the regenerator.
[0006]
However, in the absorption refrigeration system, the internal pressure (operating pressure), particularly the operating pressure and temperature of the regenerator on the hottest side, increase with the use of a plurality of regenerators, and the high pressure and the High temperature measures are required.
[0007]
That is, in the absorption refrigeration apparatus, when a plurality of regenerators having different operating temperatures are provided as described above, the absorption solution of the low-temperature regenerator is heated and concentrated at the refrigerant vapor temperature of the high-temperature regenerator. The refrigerant vapor temperature of the high-temperature regenerator must be equal to or higher than the boiling temperature of the absorption solution of the low-temperature regenerator, and therefore the operating pressure of the high-temperature regenerator increases in proportion to the refrigerant vapor temperature. Therefore, measures against high pressure and high temperature of the refrigeration system are required.
[0008]
In the absorption refrigerating apparatus having the above-described configuration, the concentrated solution that is heated and concentrated in each regenerator on the highest temperature side and flows out is combined with the concentrated solution that is heated and concentrated in the regenerator on the lowest temperature side and flows out. After flowing into the absorber, the concentrated solution flowing out of the hottest regenerator and the concentrated solution flowing out of the coldest regenerator have a large temperature difference and a large pressure difference. Therefore, if the pressure of the concentrated solution on the high-pressure side (in other words, the high-temperature side) is not adjusted, the merging with the concentrated solution on the low-temperature side cannot be performed smoothly. That is, some kind of pressure adjusting means is required.
[0009]
The present invention has been made in view of the above points, and by improving the circulation path of an absorbing solution, it is possible to provide an efficient absorption refrigeration apparatus having a low operating pressure and high efficiency, and a large refrigeration system in a pipe. It is an object of the present invention to eliminate the presence of a merging portion where a pressure difference exists, and to enable stable solution circulation.
[0010]
[Means for Solving the Problems]
According to the first aspect of the present invention, at least one or more condensers C, evaporators E, absorbers A, and three solution heat exchangers H are provided as means for solving the above problems. ₃ ~ H ₁ And regenerator G ₃ ~ G ₁ Is operatively connected with a solution piping system and a refrigerant piping system to form a circulation cycle, ₃ ~ G ₁ To the high-temperature regenerator G ₃ The heat of the absorption solution is heated and boiled by using the external heat source J to generate refrigerant vapor, and the heat of the refrigerant vapor is used to generate the medium temperature regenerator G. ₂ The absorption solution is heated and boiled to generate refrigerant vapor, and the heat of the refrigerant vapor is used to produce the low-temperature regenerator G. ₁ In the absorption refrigeration system configured to heat and boil the absorption solution to generate refrigerant vapor, the dilute solution La coming out of the absorber A is replaced with the low-temperature solution heat exchanger H. ₁ After passing through the side to be heated, one of which is the high-temperature solution heat exchanger H ₃ High temperature regenerator G ₃ And the high-temperature regenerator G ₃ Concentrated solution L which is heated and concentrated in ₃ Is the high-temperature solution heat exchanger H ₃ After passing through the heating side of the low-temperature regenerator G ₁ While the other is in the medium temperature solution heat exchanger H ₂ After passing through the heated side of the intermediate temperature regenerator G ₂ And the intermediate temperature regenerator G ₂ Medium concentrated solution L which is concentrated by heating in ₂ Is the medium temperature solution heat exchanger H ₂ After passing through the heating side of the low-temperature regenerator G ₁ And the low-temperature regenerator G ₁ Low temperature concentrated solution L ₁ Is the low-temperature solution heat exchanger H ₁ After passing through the heating side of the above, it flows into the absorber A.
[0011]
With the above-described configuration, the dilute solution La coming out of the absorber A is branched, and one of the dilute solutions La is a high-temperature regenerator G. ₃ And the other is a medium temperature regenerator G ₂ To the intermediate temperature regenerator G ₂ In this case, the dilute solution La in a non-concentrated state flows in as it is, so that, for example, the high-temperature regenerator G ₃ In this case, the concentration of the absorbing solution is lower than when the heat-concentrated absorbing solution is introduced, and the boiling temperature is accordingly lower. This medium temperature regenerator G ₂ High-temperature regenerator G as a heating source for the amount of the lowering of the boiling temperature of the absorbing solution of ₃ , The high temperature regenerator G proportional to the refrigerant vapor temperature can be set low. ₃ Can be set low, and as a result, it is possible to provide an absorption refrigeration system with low operating pressure and good operability.
[0012]
Further, since the dilute solution La is branched, for example, the entire amount of the dilute solution La is directly changed to the high-temperature regenerator G. ₃ High-temperature regenerator G ₃ The amount of inflow to the system will be reduced. As a result, the high temperature regenerator G ₃ In this case, the amount of sensible heat is reduced by an amount corresponding to the small amount of the absorbing solution to be heated and boiled. ₃ Heat required for heating (ie, the regenerator G) ₃ ), The coefficient of performance (COP) of the entire system is improved, and the efficiency of the absorption refrigeration system is improved. Further, the high temperature regenerator G ₃ High temperature solution heat exchanger H just before ₃ In this case, the heat transfer area can be reduced by an amount corresponding to the decrease in the amount of the absorbing solution flowing therein, thereby making it possible to reduce the size of the heat transfer device, thereby contributing to the downsizing of the absorption refrigeration apparatus.
[0013]
Further, the dilute solution La coming out of the absorber A is used as the low-temperature solution heat exchanger H. ₁ Branch after passing through the heated side of the high-temperature solution heat exchanger H ₃ High temperature regenerator G ₃ And the other is a medium temperature solution heat exchanger H ₂ Medium-temperature regenerator G after passing through the heated side of ₂ So that the high-temperature regenerator G ₃ The high-temperature solution heat exchanger H immediately before ₃ Solution La flowing through the intermediate temperature regenerator G ₂ Medium-temperature solution heat exchanger H immediately before ₂ Dilute solution La flowing through the low-temperature solution heat exchanger H ₁ At a high temperature regenerator G ₃ And the intermediate temperature regenerator G ₂ In this case, the required amount of heating heat of the absorbing solution is reduced, and improvement in the thermal efficiency of the entire system can be expected.
[0014]
In addition, high temperature regenerator G ₃ Concentrated solution L which is heated and concentrated in ₃ Is low temperature regenerator G ₁ , There is no confluence where a large pressure difference occurs in the piping, and a stable solution circulation can be obtained.
[0015]
In addition, since the number of regenerators and solution heat exchangers is set to three, the number of regenerators is increased to increase the number of concentration stages of the absorbing solution to increase the thermal efficiency, and the number of solution heat exchangers is increased. By comparing the merit of improving the performance of the absorption refrigeration system by increasing the heat recovery rate and the disadvantage of increasing the production cost by increasing the number of these regenerators and solution heat exchangers, By using three regenerators and three solution heat exchangers as in the invention, it is possible to achieve both the performance and cost aspects of the absorption refrigeration system, which is extremely useful in practice.
[0016]
According to the second aspect of the present invention, at least one or more condensers C, evaporators E, absorbers A and three solution heat exchangers H are provided as means for solving the above problems. ₃ ~ H ₁ And regenerator G ₃ ~ G ₁ Is operatively connected with a solution piping system and a refrigerant piping system to form a circulation cycle, ₃ ~ G ₁ To the high-temperature regenerator G ₃ The heat of the absorption solution is heated and boiled by using the external heat source J to generate refrigerant vapor, and the heat of the refrigerant vapor is used to generate the medium temperature regenerator G. ₂ The absorption solution is heated and boiled to generate refrigerant vapor, and the heat of the refrigerant vapor is used to produce the low-temperature regenerator G. ₁ In the absorption refrigeration apparatus configured to heat and boil the absorption solution to generate refrigerant vapor, the dilute solution La coming out of the absorber A is supplied to the low-temperature solution heat exchanger H. ₁ After passing through the heated side of the hot water solution heat exchanger H ₃ High temperature regenerator G ₃ And the high-temperature regenerator G ₃ Concentrated solution L which is heated and concentrated in ₃ Is the high-temperature solution heat exchanger H ₃ After passing through the heating side of the low-temperature regenerator G ₁ And the other is the medium-temperature solution heat exchanger H ₂ After passing through the heated side of the intermediate temperature regenerator G ₂ And the intermediate temperature regenerator G ₂ Medium concentrated solution L which is concentrated by heating in ₂ Is the medium temperature solution heat exchanger H ₂ After passing through the heating side of the low-temperature regenerator G ₁ And the other is the low-temperature regenerator G ₁ And the low-temperature regenerator G ₁ Low temperature concentrated solution L ₁ Is the low-temperature solution heat exchanger H ₁ After passing through the heating side of the above, it flows into the absorber A.
[0017]
With the above configuration, the dilute solution La coming out of the absorber A is converted into the low-temperature solution heat exchanger H. ₁ After passing through the heated side of the regenerator G ₃ ~ G ₁ So that the intermediate temperature regenerator G ₂ In this case, the dilute solution La in a non-concentrated state flows in as it is, so that, for example, the high-temperature regenerator G ₃ In this case, the concentration of the absorbing solution is lower than when the heat-concentrated absorbing solution is introduced, and the boiling temperature is accordingly lower. This medium temperature regenerator G ₂ High-temperature regenerator G as a heating source for the amount of the lowering of the boiling temperature of the absorbing solution of ₃ , The high temperature regenerator G proportional to the refrigerant vapor temperature can be set low. ₃ Can be set low, and as a result, it is possible to provide an absorption refrigeration system with low operating pressure and good operability.
[0018]
In addition, since the dilute solution La is branched into three, for example, the entire amount of the dilute solution La is directly changed to the high-temperature regenerator G. ₃ And medium temperature regenerator G ₂ High-temperature regenerator G ₃ And medium temperature regenerator G ₂ The amount of inflow to the system will be reduced. As a result, the high temperature regenerator G ₃ And medium temperature regenerator G ₂ In this case, the amount of sensible heat is reduced by an amount corresponding to the small amount of the absorbing solution to be heated and boiled. ₃ And medium temperature regenerator G ₂ Heat required for heating (ie, the regenerator G) _n ), The coefficient of performance (COP) of the entire system is improved, and the efficiency of the absorption refrigeration system is improved. Further, the high temperature regenerator G ₃ And medium temperature regenerator G ₂ High temperature solution heat exchanger H just before ₃ And medium temperature solution heat exchanger H ₂ In this case, the heat transfer area can be reduced by an amount corresponding to the decrease in the amount of the absorbing solution flowing therein, thereby making it possible to reduce the size of the heat transfer device, thereby contributing to the downsizing of the absorption refrigeration apparatus.
[0019]
Further, the dilute solution La coming out of the absorber A is used as the low-temperature solution heat exchanger H. ₁ After passing through the side to be heated, one of which is a high-temperature solution heat exchanger H ₃ High temperature regenerator G ₃ And the other is a medium temperature solution heat exchanger H ₂ Medium-temperature regenerator G after passing through the heated side of ₂ And the other is a low-temperature regenerator G ₁ So that the high-temperature regenerator G ₃ The high-temperature solution heat exchanger H immediately before ₃ Solution La flowing through the intermediate temperature regenerator G ₂ Medium-temperature solution heat exchanger H immediately before ₂ Solution La flowing through the low temperature regenerator G ₁ Together with the dilute solution La flowing into the low-temperature solution heat exchanger H ₁ Flows in a state where the reheater G ₃ ~ G ₁ The required heating heat of the absorbing solution in the above is reduced, and improvement in the thermal efficiency of the whole system can be expected.
[0020]
In addition, high temperature regenerator G ₃ Concentrated solution L which is heated and concentrated in ₃ Is low temperature regenerator G ₁ , There is no confluence where a large pressure difference occurs in the piping, and a stable solution circulation can be obtained.
[0021]
In addition, since the number of regenerators and solution heat exchangers is set to three, the number of regenerators is increased to increase the number of concentration stages of the absorbing solution to increase the thermal efficiency, and the number of solution heat exchangers is increased. By comparing the merit of improving the performance of the absorption refrigeration system by increasing the heat recovery rate and the disadvantage of increasing the production cost by increasing the number of these regenerators and solution heat exchangers, By using three regenerators and three solution heat exchangers as in the invention, it is possible to achieve both the performance and cost aspects of the absorption refrigeration system, which is extremely useful in practice.
[0022]
As in the invention of claim 3, in the absorption refrigeration apparatus according to any one of claims 1 and 2, the high-temperature regenerator G is provided. ₃ High temperature regenerator G of external heat source J for heating ₃ Is configured to heat the circulation path of the absorbing solution with residual heat Q after heating, the amount of heat input to the external heat source J can be suppressed by the residual heat of the absorbing solution due to the effective use of the residual heat Q, As a result, a further improvement in the COP of the entire system can be expected.
[0023]
As in the invention of the fourth aspect, in the absorption refrigeration apparatus of the third aspect, each of the regenerators G from the outlet of the absorber A by the residual heat Q. ₃ ~ G ₁ The absorption solution in the path leading to the absorption solution inlet of ₃ ~ G ₁ Or the high-temperature regenerator G ₃ Is configured to heat the absorption solution immediately before the absorption solution inlet of each regenerator G from the outlet of the absorber A ₃ ~ G ₁ Is designed to heat the absorbing solution in the path leading to the absorbing solution inlet, the degree of freedom in selecting the heating position is large, so that the piping design for the residual heat is easy, and each of the regenerators G ₃ ~ G ₁ Is configured to heat the absorption solution immediately before the absorption solution inlet, the preheated absorption solution emits less heat (in other words, while maintaining a higher temperature) in each regenerator G. ₃ ~ G ₁ , The heat pre-heating effect is high and the heat efficiency can be further improved. ₃ If the absorption solution immediately before the absorption solution inlet is heated, the amount of heat input to the external heat source J can be reduced by the amount of preheating, so that a further improvement in COP can be expected.
[0024]
As in the invention of claim 5, in the absorption refrigeration apparatus according to any one of claims 3 and 4, the residual heat pipe 50 for the residual heat Q is branched into two or more residual heat branch pipes 51 and 52. When the absorption solution is heated in each of the residual heat branch pipes 51 and 52, heat having a high residual heat Q can be distributed to the absorption solution, and the preheating effect on the absorption solution is promoted. Become.
[0025]
As in the invention of claim 6, in the absorption refrigeration apparatus according to any one of claims 3, 4, and 5, when the absorption solution is heated in multiple stages by the residual heat Q, the absorption refrigeration apparatus may The temperature difference between the absorbing solution to be heat-exchanged and the residual heat Q is equalized as much as possible at each of the heating positions, thereby improving the heat recovery efficiency of the entire system and further improving the thermal efficiency of the absorption refrigeration system. Can be expected.
[0026]
As in the invention of claim 7, in the absorption refrigeration apparatus according to any one of claims 3, 4, 5, and 6, the dilute solution pipe 21 from the absorber A is provided in the dilute solution pipe 21. Solution heat exchanger H ₁ A branch heat pipe H is provided in the branch pipe 21B provided in the branch pipe 21B branched from the dilute solution pipe 21. ₂ Is provided, and the absorption solution is heated by the residual heat Q in the branch pipe 47 or 48, so that the amount of the absorption solution heated by the residual heat Q is small, so that the absorption solution is efficiently absorbed. The solution can be preheated.
[0027]
As in the invention of claim 8, in the absorption refrigeration apparatus according to any one of claims 1, 2, 3, 4, 5, 6, and 7, each of the regenerators G ₂ , G ₁ Drain Dr generated in ₂ , Dr ₁ The absorption solution is heated by the ₂ , Dr ₁ Regenerator G by effectively utilizing the heat held by the ₃ , G ₂ , The thermal efficiency of the entire system can be further promoted.
[0028]
As in the ninth aspect of the present invention, in the absorption refrigeration apparatus according to the eighth aspect, each of the regenerators G ₂ , G ₁ Drain Dr generated in ₂ , Dr ₁ Are combined to heat the absorbing solution, the combined steam drain Dr ₂ , Dr ₁ Has a larger amount of heat, and can efficiently preheat the absorbing solution with the larger amount of heat.
[0029]
As in the invention of claim 10, in the absorption refrigeration apparatus according to any one of claims 8 and 9, the vapor drain Dr ₂ , Dr ₁ The regenerator G from the outlet of the absorber A ₂ , G ₁ The absorption solution in the path leading to the absorption solution inlet of ₂ , G ₁ Is configured to heat the absorption solution immediately before the absorption solution inlet of each regenerator G from the outlet of the absorber A ₂ , G ₁ Is designed to heat the absorption solution in the path leading to the absorption solution inlet, the degree of freedom in selecting the heating position is large, so that the steam drain piping design is easy and the regenerators G ₂ , G ₁ Is configured to heat the absorption solution immediately before the absorption solution inlet, the preheated absorption solution emits less heat (in other words, while maintaining a higher temperature) in each regenerator G. ₂ , G ₁ Since it flows into the air, the preheating effect is high and further improvement in thermal efficiency can be expected.
[0030]
As in the eleventh aspect, in the absorption refrigeration apparatus according to any one of the eighth, ninth, and tenth aspects, the vapor drain Dr ₂ , Dr ₁ Is branched into two or more, and the absorption solution is heated in each of the branch paths 34 and 36, the steam drain Dr ₂ , Dr ₁ Can be distributed with high heat, and the preheating effect on the absorbing solution is promoted.
[0031]
As in the twelfth aspect, in the absorption refrigeration apparatus according to any one of the eighth, ninth, tenth, and eleventh aspects, the vapor drain Dr ₂ , Dr ₁ When the absorption solution is heated in multiple stages, the absorption solution and the vapor drain Dr that exchange heat with each other are exchanged. ₂ , Dr ₁ And the temperature difference between them is equalized as much as possible at each of the heating positions, so that the heat recovery efficiency of the entire system is improved, and further improvement in the heat efficiency of the absorption refrigeration apparatus can be expected.
[0032]
As in the invention of claim 13, in the absorption refrigeration apparatus according to any one of claims 8, 9, 10, 11, and 12, a branch pipe 21B branched from the dilute solution pipe 21 from the absorber A is provided. Medium temperature solution heat exchanger H provided in branch pipe 21B ₂ A branch pipe 48 is provided which bypasses the steam drain Dr. ₂ When it is configured to heat by steam drain Dr ₂ Since the amount of the absorbing solution heated by the retained heat is small, the absorbing solution can be efficiently preheated.
[0033]
As in the invention of claim 14, the absorption refrigeration apparatus according to any one of claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, and 13, The absorber A and the evaporator E are divided into a plurality of stages having different refrigerant evaporation temperatures; ₁ And the condenser C is divided into a plurality of stages having different refrigerant condensation temperatures, or the absorber A and the evaporator E are divided into a plurality of stages having different refrigerant evaporation temperatures, and the low-temperature regenerator G is divided. ₁ When the condenser C is divided into a plurality of stages having different refrigerant condensing temperatures, the entire cycle is shifted to a low concentration side, the operating pressure of the system is reduced, and an absorption type refrigeration apparatus having good operability can be provided.
[0034]
As in the invention of claim 15, the absorption refrigeration apparatus according to any one of claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13 and 14 When cooling water Wa that circulates through the absorber A and the condenser C to cool them together is configured to flow from the condenser C side to the absorber A side, for example, the cooling water Wa Is supplied to the condenser C with cooling water Wa having a lower temperature than in the case where the water flows from the absorber A side to the condenser C side, so that the cooling capacity of the condenser C is improved. Low temperature regenerator G connected to condenser C ₁ Operating pressure of the low-temperature regenerator G ₁ , The highest operating pressure of the entire cycle governed by the operating pressure of the ₃ , The operating pressure of the refrigeration system is reduced, and an absorption refrigeration apparatus having better operability can be provided.
[0035]
BEST MODE FOR CARRYING OUT THE INVENTION
Hereinafter, the present invention will be described with reference to some preferred embodiments with reference to the accompanying drawings.
[0036]
First embodiment
FIG. 1 shows an absorption refrigeration system Z according to a first embodiment of the present invention. ₁ Is shown.
[0037]
This absorption refrigeration system Z ₁ Is an absorption refrigerating apparatus using water as a refrigerant and lithium bromide as an absorbing liquid, one condenser C, one absorber A, one evaporator E, and three three solution heat exchangers H ₃ , H ₂ , H ₁ And regenerator G ₃ , G ₂ , G ₁ Are operatively connected by a solution piping system and a refrigerant piping system to constitute a circulation cycle of the refrigerant and the absorbing solution.
[0038]
The evaporator E is provided with a heat exchange unit 7 for passing the liquid We to be cooled and a refrigerant disperser 13 for dispersing the refrigerant Re on the heat exchange unit 7 in the container 1.
[0039]
The absorber A is provided with a solution sprayer 12 for spraying the concentrated solution Lg and a heat exchange unit 8 for removing the heat of absorption generated in the absorber A in the container 2. .
[0040]
The condenser C is provided with a heat exchange unit 11 for passing the cooling water Wa into the container 6.
[0041]
Each regenerator G ₃ , G ₂ , G ₁ Are for heating and concentrating an absorbing solution containing a refrigerant to form a concentrated solution having a high concentration in sequence. The operating temperatures of these are different from each other, and a high-temperature regenerator operating at the highest temperature is used. G ₃ Is provided with an external heat source J (for example, combustion gas or steam) in the container 3, and is operated at an intermediate temperature. ₂ Is provided with a solution heating unit 9 in the container 4 and further operates at the lowest temperature. ₁ Is provided with a solution heating unit 10 in a container 5.
[0042]
Each solution heat exchanger H ₁ , H ₂ , H ₃ Is the regenerator G ₁ , G ₂ , G ₃ Low-temperature concentrated solution L produced in ₁ , Medium temperature concentrated solution L ₂ And high temperature concentrated solution L ₃ Is for recovering the heat of each of them to the dilute solution La side, and is generally a shell-and-tube type heat exchanger, but may be constituted by another type, for example, a plate type heat exchanger. Good.
[0043]
These devices are operatively connected as follows by a solution piping system and a refrigerant piping system.
[0044]
That is, the container 6 of the condenser C and the container 1 of the evaporator E are connected by a liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is supplied to the evaporator via the liquid refrigerant pipe 30. It is supplied to the E side. Further, the liquid refrigerant Rc supplied to the evaporator E is pumped up by the refrigerant sprayer 13 through the liquid refrigerant pipe 29 by the refrigerant pump RP, and as the refrigerant Re from the refrigerant sprayer 13 to the heat exchange unit 7 side. Sprayed on.
[0045]
The cooling water Wa flowing from the cooling liquid inlet pipe 41 into the heat exchange section 8 is guided to the inlet side of the heat exchange section 11 through a cooling water pipe 42 connected to the outlet side of the heat exchange section 8, After flowing out from the cooling water outlet pipe 43, the heat exchange section 8 absorbs the absorbed heat, and then the low-temperature regenerator G in the heat exchange section 11. ₁ Vapor R transferred from ₁ Is cooled and condensed.
[0046]
The liquid to be cooled (water) We flowing from the cooled liquid inlet pipe 45 into the heat exchange section 7 and flowing out from the cooled liquid outlet pipe 46 is cooled by the heat of evaporation of the refrigerant Re. Further, the vaporized refrigerant Ra generated in the evaporator E by spraying to the heat exchange unit 7 is transferred to the absorber A as it is.
[0047]
A dilute solution pipe 21 having a solution pump LP is connected to the bottom of the vessel 2 of the absorber A. The dilute solution pipe 21 is connected to the low-temperature solution heat exchanger H. ₁ After passing through the side to be heated, the first branch pipe 21A and the second branch pipe 21B are branched. The first branch pipe 21A is connected to the high-temperature solution heat exchanger H. ₃ High temperature regenerator G ₃ It is connected to the. Further, the second branch pipe 21B is connected to the medium temperature solution heat exchanger H. ₂ Through the heated side of the medium temperature regenerator G ₂ It is connected to the. Therefore, the dilute solution La flowing out of the absorber A is mixed with the low-temperature solution heat exchanger H. ₁ Branch after passing through the heated side of the high-temperature solution heat exchanger H ₃ Through the high-temperature regenerator G ₃ And the other is the medium-temperature solution heat exchanger H ₂ Through the intermediate temperature regenerator G ₂ Will flow into
[0048]
The high temperature regenerator G ₃ Connected to the high-temperature regenerator G ₃ Concentrated solution L flowing out of ₃ Is connected to the high-temperature solution heat exchanger H ₃ Through the heating side of the low-temperature regenerator G ₁ It is connected to the.
[0049]
The intermediate temperature regenerator G ₂ Connected to the intermediate temperature regenerator G ₂ Medium concentrated solution L flowing out of ₂ Is connected to the medium-temperature solution heat exchanger H ₂ Through the heating side of the low-temperature regenerator G ₁ It is connected to the.
[0050]
The low-temperature regenerator G ₁ Low-temperature concentrated solution L flowing out of ₁ Is connected to the solution sprayer 12 in the absorber A.
[0051]
The high temperature regenerator G ₃ Of the medium temperature regenerator G through a high temperature steam pipe 31. ₂ At the inlet side of the solution heating unit 9 at
[0052]
The intermediate temperature regenerator G ₂ Is connected to the low temperature regenerator G through a medium temperature steam pipe 32. ₁ At the inlet side of the solution heating unit 10 at
[0053]
The low-temperature regenerator G ₁ The outlet side of the solution heating section 10 is connected to the condenser C via a refrigerant drain pipe 35.
[0054]
The intermediate temperature regenerator G ₂ The refrigerant drain pipe 34 connected to the outlet side of the solution heating unit 9 in the above is joined to the refrigerant drain pipe 35.
[0055]
The low-temperature regenerator G ₁ Is transferred to the condenser C via the refrigerant passage 33.
[0056]
Absorption refrigeration system Z ₁ Adopts the above-described device arrangement and path configuration to constitute a circulation cycle of the refrigerant and the absorbing solution.
[0057]
Subsequently, the absorption refrigeration system Z ₁ The operation cycle will be described in detail.
[0058]
The dilute solution La (concentration ξ) fed from the absorber A by the solution pump LP _a ) Is the low-temperature solution heat exchanger H ₁ After passing through the side to be heated, one of which is a high-temperature solution heat exchanger H ₃ High temperature regenerator G through the heated side of ₃ And the high-temperature regenerator G ₃ At the heat concentration effect by the external heat source J ₃ High temperature concentrated solution L ₃ And the hot solution heat exchanger H ₃ Pass through the heating side of. At this time, the high-temperature solution heat exchanger H ₃ , The diluted solution La on the heated side and the high-temperature concentrated solution L on the heated side ₃ (Heat recovery), and the dilute solution La is preheated to the high-temperature regenerator G. ₃ Flows into.
[0059]
On the other hand, the other branched dilute solution La is a medium temperature solution heat exchanger H ₂ Medium-temperature regenerator G after passing through the heated side of ₂ And the intermediate temperature regenerator G ₂ And the high-temperature regenerator G ₃ Vapor R flowing into the solution heating section 9 from the side ₃ Is concentrated by heating. ₂ Medium temperature concentrated solution L ₂ And the medium-temperature solution heat exchanger H ₂ Low-temperature regenerator G through the heating side of ₁ Flows into. At this time, the medium temperature solution heat exchanger H ₂ , The diluted solution La on the heated side and the medium-temperature concentrated solution L on the heated side ₂ (Heat recovery), and the dilute solution La is preheated to the intermediate temperature regenerator G. ₂ Flows into.
[0060]
Further, the low-temperature regenerator G ₁ Medium concentrated solution L ₂ Is the low-temperature regenerator G ₁ In the medium temperature regenerator G ₂ Vapor R flowing into the solution heating unit 10 from the side ₂ Is concentrated by heating. ₁ Low temperature concentrated solution L ₁ It leaks out.
[0061]
And this low temperature regenerator G ₁ Concentration flowing out of ₁ Low temperature concentrated solution L ₁ Is the low-temperature solution heat exchanger H ₁ Flows into the absorber A through the heating side of the solution, where it is sprayed by the solution sprayer 12. At this time, the low-temperature solution heat exchanger H ₁ , The diluted solution La on the heated side and the concentration ξ on the heated side ₁ Concentrated solution L ₁ (Heat recovery), and the dilute solution La is preheated to the high-temperature regenerator G. ₃ And the intermediate temperature regenerator G ₂ Branch into each other and flow in.
[0062]
The above is the absorption refrigeration system Z of this embodiment. ₁ In this operation cycle, the following specific operation and effect can be obtained.
[0063]
Absorption refrigeration system Z according to the first embodiment. ₁ In the above, the dilute solution La coming out of the absorber A is branched and one of the dilute solutions La is separated into a high-temperature regenerator G. ₃ And the other is a medium temperature regenerator G ₂ After flowing into the low temperature regenerator G ₁ , So that the intermediate temperature regenerator G ₂ In this case, the dilute solution La in a non-concentrated state flows as it is, so that the high-temperature regenerator G ₃ The concentration of the absorbing solution is lower than when the absorbing solution (concentrated solution) heated and concentrated in the above is introduced, and the boiling temperature is accordingly lower. This medium temperature regenerator G ₂ The high-temperature regenerator G as a heating source for the amount of decrease in the boiling temperature of the absorbing solution in ₃ , The high temperature regenerator G, which is proportional to the refrigerant vapor temperature, can be set low. ₃ Can be set low, and as a result, it is possible to provide an absorption refrigeration apparatus having a low operating pressure and good operability.
[0064]
Further, the dilute solution La from the absorber A is branched and a part thereof is separated into a high-temperature regenerator G. ₃ , For example, the entire amount of the dilute solution La is directly ₃ High-temperature regenerator G ₃ The amount of the dilute solution La flowing into the tank decreases. As a result, the high temperature regenerator G ₃ In this case, since the amount of sensible heat is reduced by the amount of the absorbing solution to be heated and boiled, the high-temperature regenerator ₃ Heat required for heating the regenerator (ie, the high-temperature regenerator G) ₃ Heat input), the COP of the entire system improves, and the absorption refrigeration system Z ₁ Is to be improved in efficiency.
[0065]
Further, the dilute solution La from the absorber A is branched and a part thereof is separated into a high-temperature regenerator G. ₃ The high-temperature regenerator G ₃ Hot solution heat exchanger H immediately before ₃ In the above, the heat transfer area can be reduced by an amount corresponding to the decrease in the amount of the dilute solution La flowing therein, thereby making it possible to achieve compactness. ₁ Can contribute to the compactness of the system.
[0066]
Further, the dilute solution La coming out of the absorber A is converted into a low-temperature solution heat exchanger H. ₁ After passing through, the high-temperature regenerator G ₃ The high-temperature solution heat exchanger H immediately before ₃ Solution La flowing through the medium and the intermediate temperature regenerator G ₂ Medium-temperature solution heat exchanger H immediately before ₂ Together with the dilute solution La flowing through the low-temperature solution heat exchanger H ₁ At a high temperature regenerator G as a result. ₃ And medium temperature regenerator G ₂ In this case, the required amount of heating heat of the absorbing solution is reduced, and improvement in the thermal efficiency of the entire system can be expected.
[0067]
In addition, high temperature regenerator G ₃ Concentrated solution L which is heated and concentrated in ₃ Is low temperature regenerator G ₁ , There is no confluence where a large pressure difference occurs in the piping, and a stable solution circulation can be obtained.
[0068]
Also, three regenerators G ₁ , G ₂ , G ₃ And three solution heat exchangers H ₁ , H ₂ , H ₃ In this configuration, the number of regenerators is increased to increase the number of stages of concentration of the absorbing solution to increase thermal efficiency, and the number of solution heat exchangers is increased to improve the heat recovery rate. Comparing the merits of improving the performance of the absorption refrigeration system by increasing the number of the regenerators and the solution heat exchangers with the production cost by increasing the number of these regenerators and solution heat exchangers, the absorption refrigeration system Z ₁ It is considered to be optimal in terms of achieving both the performance aspect and the cost aspect, and is extremely useful in practice.
[0069]
Second embodiment
FIG. 2 shows an absorption refrigeration system Z according to a second embodiment of the present invention. ₂ Is shown.
[0070]
This absorption refrigeration system Z ₂ , The dilute solution La coming out of the absorber A is converted to the low-temperature solution heat exchanger H ₁ After passing through the side to be heated, one of which is a high-temperature solution heat exchanger H ₃ High temperature regenerator G ₃ And the high-temperature regenerator G ₃ Concentrated solution L which is heated and concentrated in ₃ Is the high-temperature solution heat exchanger H ₃ Low-temperature regenerator G after passing through the heating side of ₁ And the other is a medium temperature solution heat exchanger H ₂ Medium-temperature regenerator G after passing through the heated side of ₂ And the intermediate temperature regenerator G ₂ Medium concentrated solution L which is concentrated by heating in ₂ Is the medium temperature solution heat exchanger H ₂ Low-temperature regenerator G after passing through the heating side of ₁ And the other is the low-temperature regenerator G ₁ And the low-temperature regenerator G ₁ Low temperature concentrated solution L ₁ Is the low-temperature solution heat exchanger H ₁ After passing through the heating side of the above, it is configured to flow into the absorber A. Other configurations are the same as those in the first embodiment, and a description thereof will be omitted.
[0071]
Absorption refrigeration system Z configured as described above ₂ Has the following effects.
[0072]
That is, the low-temperature solution heat exchanger H ₁ After passing through the heated side of the regenerator G ₃ ~ G ₁ So that the intermediate temperature regenerator G ₂ In this case, the dilute solution La in a non-concentrated state flows in as it is, so that, for example, the high-temperature regenerator G ₃ In this case, the concentration of the absorbing solution is lower than when the heat-concentrated absorbing solution is introduced, and the boiling temperature is accordingly lower. This medium temperature regenerator G ₂ High-temperature regenerator G as a heating source for the amount of the lowering of the boiling temperature of the absorbing solution of ₃ , The high temperature regenerator G proportional to the refrigerant vapor temperature can be set low. ₃ Can be set low, and as a result, it is possible to provide an absorption refrigeration system with low operating pressure and good operability.
[0073]
In addition, since the dilute solution La is branched into three, for example, the entire amount of the dilute solution La is directly changed to the high-temperature regenerator G. ₃ And medium temperature regenerator G ₂ High-temperature regenerator G ₃ And medium temperature regenerator G ₂ The amount of inflow to the system will be reduced. As a result, the high temperature regenerator G ₃ And medium temperature regenerator G ₂ In this case, the amount of sensible heat is reduced by an amount corresponding to the small amount of the absorbing solution to be heated and boiled. ₃ And medium temperature regenerator G ₂ Heat required for heating (ie, the regenerator G) _n ), The coefficient of performance (COP) of the entire system is improved, and the efficiency of the absorption refrigeration system is improved. Further, the high temperature regenerator G ₃ And medium temperature regenerator G ₂ High temperature solution heat exchanger H just before ₃ And medium temperature solution heat exchanger H ₂ In this case, the heat transfer area can be reduced by an amount corresponding to the decrease in the amount of the absorbing solution flowing therein, thereby making it possible to reduce the size of the heat transfer device, thereby contributing to the downsizing of the absorption refrigeration apparatus.
[0074]
Further, the dilute solution La coming out of the absorber A is used as the low-temperature solution heat exchanger H. ₁ After passing through the side to be heated, one of which is a high-temperature solution heat exchanger H ₃ High temperature regenerator G ₃ And the other is a medium temperature solution heat exchanger H ₂ Medium-temperature regenerator G after passing through the heated side of ₂ And the other is a low-temperature regenerator G ₁ So that the high-temperature regenerator G ₃ The high-temperature solution heat exchanger H immediately before ₃ Solution La flowing through the intermediate temperature regenerator G ₂ Medium-temperature solution heat exchanger H immediately before ₂ Solution La flowing through the low temperature regenerator G ₁ Together with the dilute solution La flowing into the low-temperature solution heat exchanger H ₁ Flows in a state where the reheater G ₃ ~ G ₁ The required heating heat of the absorbing solution in the above is reduced, and improvement in the thermal efficiency of the whole system can be expected.
[0075]
In addition, high temperature regenerator G ₃ Concentrated solution L which is heated and concentrated in ₃ Is low temperature regenerator G ₁ , There is no confluence where a large pressure difference occurs in the piping, and a stable solution circulation can be obtained.
[0076]
Other functions and effects are the same as those in the first embodiment, and thus description thereof is omitted.
[0077]
Third embodiment
FIG. 3 shows an absorption refrigeration system Z according to a third embodiment of the present invention. ₃ Is shown.
[0078]
This absorption refrigeration system Z ₃ Is the absorption refrigeration apparatus Z according to the first embodiment. ₁ It has the same basic configuration as that of the first embodiment, except for the absorption refrigeration system Z of the first embodiment. ₁ In the above, the cooling water Wa for cooling the absorber A and the condenser C is caused to flow from the absorber A side to the condenser C side. Z ₃ Is that the cooling water Wa is caused to flow from the condenser C side to the absorber A side. Therefore, the cooling water inlet pipe 41 in the first embodiment is a cooling water outlet pipe, and the cooling water outlet pipe 43 is a cooling water inlet pipe.
[0079]
With such a cooling water circulation system, the cooling water Wa having a lower temperature is supplied to the condenser C as compared with a case where the cooling water Wa flows from the absorber A to the condenser C, for example. Therefore, the cooling capacity of the condenser C is improved, and the low-temperature regenerator G connected to the condenser C is accordingly increased. ₁ Operating pressure will decrease. As a result, the low-temperature regenerator G ₁ , The highest operating pressure of the entire cycle governed by the operating pressure of the ₃ The operating pressure of the refrigeration system is reduced, and an absorption refrigeration apparatus having better operability can be provided.
[0080]
Note that the other configuration, operation, and effect are the same as those in the first embodiment, and a description thereof will not be repeated.
[0081]
Note that the structure of the present embodiment (that is, the structure in which the flow direction of the cooling water Wa is from the condenser to the absorber) is also applicable to the second embodiment.
[0082]
Fourth embodiment
FIG. 4 shows an absorption refrigeration system Z according to a fourth embodiment of the present invention. ₄ Is shown.
[0083]
This absorption refrigeration system Z ₄ Is the absorption refrigeration apparatus Z according to the first embodiment. ₁ The difference is that both the absorber A and the evaporator E have a two-stage structure with different refrigerant evaporation temperatures, and the low-temperature regenerator G ₁ And the condenser C have a two-stage configuration having different refrigerant condensation temperatures. In addition, absorber A, evaporator E, low-temperature regenerator G ₁ Also, the condenser C may have a multi-stage configuration of two or more stages.
[0084]
With such a configuration, the absorption refrigeration system Z ₄ The entire cycle is shifted to the low concentration side, and the operating pressure of the system is reduced accordingly, so that an absorption refrigeration apparatus with good operability can be provided.
[0085]
Note that the other configuration, operation, and effect are the same as those in the first embodiment, and a description thereof will not be repeated.
[0086]
In addition, the structure of this embodiment (namely, absorber A, evaporator E, low-temperature regenerator G) ₁ And a structure in which the condenser C has two or more stages) is also applicable to the second embodiment.
[0087]
Fifth embodiment
FIG. 5 shows an absorption refrigeration system Z according to a fifth embodiment of the present invention. ₅ The working cycle is shown.
[0088]
This absorption refrigeration system Z ₅ Is a condenser C, an absorber A, an evaporator E, and three solution heat exchangers H, respectively. ₃ , H ₂ , H ₁ And regenerator G ₃ , G ₂ , G ₁ And a drain heat exchanger D in addition to the above. ₁ , D ₂ And one exhaust heat exchanger K, and these devices are operatively connected by a solution piping system and a refrigerant piping system to constitute a circulation cycle of the refrigerant and the absorbing solution.
[0089]
The low-temperature solution heat exchanger H is connected to the dilute solution pipe 21 connected to the absorber A. ₁ And the first drain heat exchanger D ₁ Of the low-temperature solution heat exchanger H ₁ Is connected to the middle solution heat exchanger H in the second branch line 21B. ₂ And the second drain heat exchanger D ₂ Through the heated side of the medium-temperature solution heat exchanger H ₂ An absorption solution branch pipe 48 connecting the front and rear of the absorption solution is provided.
[0090]
Also, medium temperature regenerator G ₂ The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 in the second embodiment is connected to the second drain heat exchanger D ₂ Is connected to the condenser C through the heating side of the condenser C.
[0091]
In addition, low temperature regenerator G ₁ The refrigerant drain pipe 35 connected to the outlet side of the solution heating unit 10 in the first drain heat exchanger D ₁ Is connected to the condenser C through the heating side of the condenser C.
[0092]
In addition, high temperature regenerator G ₃ Is connected to the outlet side of the solution heating unit 14 in the residual heat pipe 50 passing through the heating side of the exhaust heat exchanger K.
[0093]
The heat exchange unit 8 of the absorber A and the heat exchange unit 11 of the condenser C are connected via a cooling water pipe 42, and the cooling water Wa flowing from the cooling water inlet pipe 41 is supplied to the condenser After performing the cooling function on the C side, the cooling function is further performed on the absorber A side, and the cooling water is discharged from the cooling water outlet pipe 43.
[0094]
Other configurations are the same as those in the first embodiment, and a description thereof will be omitted.
[0095]
With the above-described configuration, the dilute solution La supplied from the absorber A by the solution pump LP is supplied to the low-temperature solution heat exchanger H ₁ , A part of which branches into the low-temperature solution heat exchanger H ₁ Low-temperature regenerator G that passes through the heated side of ₁ Low temperature concentrated solution L from ₁ And heat is exchanged with the first drain heat exchanger D. ₁ The low-temperature regenerator G passing through the heated side ₁ Drain from steam Dr ₁ Preheated by heat exchange with The dilute solutions La thus branched and individually preheated, respectively, are merged again and then branched again into the first branch pipe 21A and the second branch pipe 21B.
[0096]
The dilute solution La branched to the first branch pipe 21A is supplied to the high-temperature solution heat exchanger H. ₃ High temperature concentrated solution L passing through the heated side of ₃ And heat exchange with the residual heat Q of the external heat source J passing through the heated side of the exhaust heat exchanger K and passing through the heated side. Regenerator G ₃ Flows into.
[0097]
On the other hand, the dilute solution La branched to the side of the second branch pipe 21B is further supplied to the intermediate temperature solution heat exchanger H ₂ , A part of which is divided into the intermediate temperature solution heat exchanger H ₂ The intermediate-temperature regenerator G passing through the heated side of the ₂ Medium-temperature concentrated solution L ₂ Is preheated by heat exchange with the other part, and the other part is the second drain heat exchanger D ₂ The intermediate-temperature regenerator G passing through the heated side of the ₂ Drain from steam Dr ₂ Preheated by heat exchange with The dilute solutions La branched and individually preheated as described above are merged again, and then the intermediate temperature regenerator G ₂ Flows into.
[0098]
Absorption refrigeration system Z according to this embodiment ₅ Has the following effects.
[0099]
That is, the high-temperature regenerator G ₃ High temperature regenerator G of external heat source J for heating ₃ Is heated by the residual heat Q after heating, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and the COP of the entire system can be reduced. Further improvement can be expected.
[0100]
In addition, low temperature regenerator G ₁ And medium temperature regenerator G ₂ Drain Dr generated in ₁ , Dr ₂ Is used to heat the dilute solution La, so that the vapor drain Dr ₁ , Dr ₂ Can be effectively used for preheating the dilute solution La, and the thermal efficiency of the entire system can be further promoted.
[0101]
Further, the first drain heat exchanger D is connected to the absorption solution branch pipe 47 branched from the dilute solution pipe 21. ₁ And the second drain heat exchanger D in the absorption solution branch pipe 48 branched from the second branch pipe 21B. ₂ Then, each of the dilute solutions La is mixed with the vapor drain Dr. ₁ , Dr ₂ , So that the steam drain Dr ₁ , Dr ₂ Since the amount of the absorbing solution heated by the retained heat is small, the absorbing solution can be efficiently preheated.
[0102]
Other functions and effects are the same as those in the first embodiment, and thus description thereof is omitted.
[0103]
Sixth embodiment
FIG. 6 shows an absorption refrigeration system Z according to a sixth embodiment of the present invention. ₆ Is shown.
[0104]
This absorption refrigeration system Z ₆ Is a condenser C, an absorber A, an evaporator E, and three solution heat exchangers H, respectively. ₃ , H ₂ , H ₁ And regenerator G ₃ , G ₂ , G ₁ And a drain heat exchanger D in addition to the above. ₁ , D ₂ And one exhaust heat exchanger K, and these devices are operatively connected by a solution piping system and a refrigerant piping system to constitute a circulation cycle of the refrigerant and the absorbing solution.
[0105]
Then, the dilute solution La coming out of the absorber A is supplied to the low-temperature solution heat exchanger H. ₁ After passing through the side to be heated, one of which is a high-temperature solution heat exchanger H ₃ High temperature regenerator G ₃ And the high-temperature regenerator G ₃ Concentrated solution L which is heated and concentrated in ₃ Is the high-temperature solution heat exchanger H ₃ Low-temperature regenerator G after passing through the heating side of ₁ And the other is a medium temperature solution heat exchanger H ₂ Medium-temperature regenerator G after passing through the heated side of ₂ And the intermediate temperature regenerator G ₂ Medium concentrated solution L which is concentrated by heating in ₂ Is the medium temperature solution heat exchanger H ₂ Low-temperature regenerator G after passing through the heating side of ₁ And the other is the low-temperature regenerator G ₁ And the low-temperature regenerator G ₁ Low temperature concentrated solution L ₁ Is the low-temperature solution heat exchanger H ₁ After passing through the heating side of the above, it is configured to flow into the absorber A.
[0106]
The low-temperature solution heat exchanger H is connected to the dilute solution pipe 21. ₁ And the first drain heat exchanger D ₁ Of the low-temperature solution heat exchanger H ₁ Is connected to the middle solution heat exchanger H in the second branch line 21B. ₂ And the second drain heat exchanger D ₂ Through the heated side of the medium-temperature solution heat exchanger H ₂ An absorption solution branch pipe 48 connecting the front and rear of the absorption solution is provided.
[0107]
Also, medium temperature regenerator G ₂ The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 in the second embodiment is connected to the second drain heat exchanger D ₂ Is connected to the condenser C through the heating side of the condenser C.
[0108]
In addition, low temperature regenerator G ₁ The refrigerant drain pipe 35 connected to the outlet side of the solution heating unit 10 in the first drain heat exchanger D ₁ Is connected to the condenser C through the heating side of the condenser C.
[0109]
In addition, high temperature regenerator G ₃ Is connected to the outlet side of the solution heating unit 14 in the residual heat pipe 50 passing through the heating side of the exhaust heat exchanger K.
[0110]
The heat exchange unit 8 of the absorber A and the heat exchange unit 11 of the condenser C are connected via a cooling water pipe 42, and the cooling water Wa flowing from the cooling water inlet pipe 41 is supplied to the condenser After performing the cooling function on the C side, the cooling function is further performed on the absorber A side, and the cooling water is discharged from the cooling water outlet pipe 43.
[0111]
Other configurations are the same as those in the first embodiment, and a description thereof will be omitted.
[0112]
With the above-described configuration, the dilute solution La supplied from the absorber A by the solution pump LP is supplied to the low-temperature solution heat exchanger H ₁ , A part of which branches into the low-temperature solution heat exchanger H ₁ Low-temperature regenerator G that passes through the heated side of ₁ Low temperature concentrated solution L from ₁ And heat is exchanged with the first drain heat exchanger D. ₁ The low-temperature regenerator G passing through the heated side ₁ Drain from steam Dr ₁ Preheated by heat exchange with The dilute solutions La thus branched and individually preheated are merged again, and then again branched into the first branch pipe 21A, the second branch pipe 21B, and the third branch pipe 21C. .
[0113]
The dilute solution La branched to the first branch pipe 21A is supplied to the high-temperature solution heat exchanger H. ₃ High temperature concentrated solution L passing through the heated side of ₃ And heat exchange with the residual heat Q of the external heat source J passing through the heated side of the exhaust heat exchanger K and passing through the heated side. Regenerator G ₃ Flows into.
[0114]
Further, the dilute solution La branched to the second branch pipe 21B side is further supplied to the intermediate temperature solution heat exchanger H. ₂ , A part of which is divided into the intermediate temperature solution heat exchanger H ₂ The intermediate-temperature regenerator G passing through the heated side of the ₂ Medium-temperature concentrated solution L ₂ Is preheated by heat exchange with the other part, and the other part is the second drain heat exchanger D ₂ The intermediate-temperature regenerator G passing through the heated side of the ₂ Drain from steam Dr ₂ Preheated by heat exchange with The dilute solutions La branched and individually preheated as described above are merged again, and then the intermediate temperature regenerator G ₂ Flows into.
[0115]
Further, the dilute solution La branched to the third branch pipe 21C side is supplied to the intermediate temperature regenerator G. ₂ Effluent from the medium-temperature solution heat exchanger H ₂ Medium concentrated solution L passed through the heating side of ₂ And low-temperature regenerator G ₁ Flows into.
[0116]
Absorption refrigeration system Z according to this embodiment ₆ Has the following effects.
[0117]
That is, the low-temperature solution heat exchanger H ₁ After passing through the heated side of the regenerator G ₃ ~ G ₁ So that the intermediate temperature regenerator G ₂ In this case, the dilute solution La in a non-concentrated state flows in as it is, so that, for example, the high-temperature regenerator G ₃ In this case, the concentration of the absorbing solution is lower than when the heat-concentrated absorbing solution is introduced, and the boiling temperature is accordingly lower. This medium temperature regenerator G ₂ High-temperature regenerator G as a heating source for the amount of the lowering of the boiling temperature of the absorbing solution of ₃ , The high temperature regenerator G proportional to the refrigerant vapor temperature can be set low. ₃ Can be set low, and as a result, it is possible to provide an absorption refrigeration system with low operating pressure and good operability.
[0118]
In addition, since the dilute solution La is branched into three, for example, the entire amount of the dilute solution La is directly changed to the high-temperature regenerator G. ₃ And medium temperature regenerator G ₂ High-temperature regenerator G ₃ And medium temperature regenerator G ₂ The amount of inflow to the system will be reduced. As a result, the high temperature regenerator G ₃ And medium temperature regenerator G ₂ In this case, the amount of sensible heat is reduced by an amount corresponding to the small amount of the absorbing solution to be heated and boiled. ₃ And medium temperature regenerator G ₂ Heat required for heating (ie, the regenerator G) _n ), The coefficient of performance (COP) of the entire system is improved, and the efficiency of the absorption refrigeration system is improved. Further, the high temperature regenerator G ₃ And medium temperature regenerator G ₂ High temperature solution heat exchanger H just before ₃ And medium temperature solution heat exchanger H ₂ In this case, the heat transfer area can be reduced by an amount corresponding to the decrease in the amount of the absorbing solution flowing therein, thereby making it possible to reduce the size of the heat transfer device, thereby contributing to the downsizing of the absorption refrigeration apparatus.
[0119]
Further, the dilute solution La coming out of the absorber A is used as the low-temperature solution heat exchanger H. ₁ After passing through the side to be heated, one of which is a high-temperature solution heat exchanger H ₃ High temperature regenerator G ₃ And the other is a medium temperature solution heat exchanger H ₂ Medium-temperature regenerator G after passing through the heated side of ₂ And the other is a low-temperature regenerator G ₁ So that the high-temperature regenerator G ₃ The high-temperature solution heat exchanger H immediately before ₃ Solution La flowing through the intermediate temperature regenerator G ₂ Medium-temperature solution heat exchanger H immediately before ₂ Solution La flowing through the low temperature regenerator G ₁ Together with the dilute solution La flowing into the low-temperature solution heat exchanger H ₁ Flows in a state where the reheater G ₃ ~ G ₁ The required heating heat of the absorbing solution in the above is reduced, and improvement in the thermal efficiency of the whole system can be expected.
[0120]
In addition, high temperature regenerator G ₃ High temperature regenerator G of external heat source J for heating ₃ Is heated by the residual heat Q after heating, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and the COP of the entire system can be reduced. Further improvement can be expected.
[0121]
In addition, low temperature regenerator G ₁ And medium temperature regenerator G ₂ Drain Dr generated in ₁ , Dr ₂ Is used to heat the dilute solution La, so that the vapor drain Dr ₁ , Dr ₂ Can be effectively used for preheating the dilute solution La, and the thermal efficiency of the entire system can be further promoted.
[0122]
Further, the first drain heat exchanger D is connected to the absorption solution branch pipe 47 branched from the dilute solution pipe 21. ₁ And the second drain heat exchanger D in the absorption solution branch pipe 48 branched from the second branch pipe 21B. ₂ Then, each of the dilute solutions La is mixed with the vapor drain Dr. ₁ , Dr ₂ , So that the steam drain Dr ₁ , Dr ₂ Since the amount of the absorbing solution heated by the retained heat is small, the absorbing solution can be efficiently preheated.
[0123]
Other functions and effects are the same as those in the first embodiment, and thus description thereof is omitted.
[0124]
Seventh embodiment
FIG. 7 shows an absorption refrigeration system Z according to a seventh embodiment of the present invention. ₇ Is shown.
[0125]
This absorption refrigeration system Z ₇ Is a condenser C, an absorber A, an evaporator E, and three solution heat exchangers H, respectively. ₃ , H ₂ , H ₁ And regenerator G ₃ , G ₂ , G ₁ And three drain heat exchangers D in addition to the above. ₁ , D ₂ , D ₃ And one exhaust heat exchanger K, and these devices are operatively connected by a solution piping system and a refrigerant piping system to constitute a circulation cycle of the refrigerant and the absorbing solution.
[0126]
The low-temperature solution heat exchanger H is connected to the dilute solution pipe 21 connected to the absorber A. ₁ And the first drain heat exchanger D ₁ To be heated and the third drain heat exchanger D ₃ And the low-temperature solution heat exchanger H ₁ An absorption solution branch pipe 47 connecting the front and rear of the absorption solution is provided. In addition, the second branch pipe 21B has a medium temperature solution heat exchanger H ₂ And the second drain heat exchanger D ₂ Through the heated side of the medium-temperature solution heat exchanger H ₂ An absorption solution branch pipe 48 connecting the front and rear of the absorption solution is provided.
[0127]
Medium temperature regenerator G ₂ The refrigerant drain pipe 34 connected to the outlet side of the solution heating unit 9 is connected to the second drain heat exchanger D ₂ Heating side and the third drain heat exchanger D ₃ Are sequentially connected to the condenser C through the heating side.
[0128]
Low temperature regenerator G ₁ The refrigerant drain pipe 35 connected to the outlet side of the solution heating unit 10 is connected to the first drain heat exchanger D ₁ Drain heat exchanger D of the refrigerant drain pipe 34 through the heating side of ₃ It is connected to the exit side.
[0129]
High temperature regenerator G ₃ The residual heat pipe 50 passing through the heating side of the exhaust heat exchanger K is connected to the outlet side of the solution heating unit 14.
[0130]
Other configurations are the same as those in the first embodiment, and a description thereof will be omitted.
[0131]
With this configuration, the dilute solution La supplied from the absorber A by the solution pump LP is supplied to the low-temperature solution heat exchanger H ₁ , A part of which branches into the low-temperature solution heat exchanger H ₁ Low-temperature regenerator G that passes through the heated side of ₁ Low temperature solution L from ₁ Preheated by heat exchange with Another part is the first drain heat exchanger D ₁ Low-temperature regenerator G that passes through the heated side of ₁ Drain from steam Dr ₁ And heat is exchanged with the preheater, and the third drain heat exchanger D ₃ Medium-temperature regenerator G that passes through the heated side of ₂ Drain from steam Dr ₂ Preheated by heat exchange with The dilute solutions La thus branched and individually preheated, respectively, are merged again and then branched again into the first branch pipe 21A and the second branch pipe 21B.
[0132]
The dilute solution La branched to the first branch pipe 21A is supplied to the high-temperature solution heat exchanger H. ₃ High-temperature regenerator G that passes through the heated side of ₃ Hot solution L from ₃ Is preheated by heat exchange with the residual heat Q of the external heat source J passing through the heated side of the exhaust heat exchanger K and passing through the heated side. Bowl G ₃ Flows into.
[0133]
Further, the dilute solution La branched to the second branch pipe 21B side is further supplied to the intermediate temperature solution heat exchanger H. ₂ , A part of which is divided into the intermediate temperature solution heat exchanger H ₂ The intermediate-temperature regenerator G passing through the heated side of the ₂ Medium-temperature concentrated solution L ₂ Is preheated by heat exchange with the other part, and the other part is the second drain heat exchanger D ₂ The intermediate-temperature regenerator G passing through the heated side of the ₂ Drain from steam Dr ₂ Preheated by heat exchange with The dilute solutions La branched and individually preheated as described above are merged again, and then the intermediate temperature regenerator G ₂ Flows into.
[0134]
Absorption refrigeration system Z according to this embodiment ₇ Has the following effects.
[0135]
That is, the high-temperature regenerator G ₃ High temperature regenerator G of external heat source J for heating ₃ Is heated by the residual heat Q after heating, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and the COP of the entire system can be reduced. Further improvement can be expected.
[0136]
In addition, low temperature regenerator G ₁ And medium temperature regenerator G ₂ Drain Dr generated in ₁ , Dr ₂ Is used to heat the dilute solution La, so that the vapor drain Dr ₁ , Dr ₂ Can be effectively used for preheating the dilute solution La, and the thermal efficiency of the entire system can be further promoted.
[0137]
Further, the first and third drain heat exchangers D are connected to the dilute solution La in the absorption solution branch pipe 47 branched from the dilute solution pipe 21. ₁ , D ₃ In the absorption solution branch pipe 48 branched from the second branch pipe 21B, the second drain heat exchanger D ₂ Then, each of the dilute solutions La is mixed with the vapor drain Dr. ₁ , Dr ₂ , So that the steam drain Dr ₁ , Dr ₂ Since the amount of the absorbing solution heated by the retained heat is small, the absorbing solution can be efficiently preheated.
[0138]
Also, the steam drain Dr ₂ 2nd drain heat exchanger D ₂ And third drain heat exchanger D ₃ Is configured to perform heating of the absorption solution in multiple stages, so that the dilute solution La and the vapor drain Dr, which exchange heat with each other, ₂ And the temperature difference between them is equalized as much as possible at each of the heating positions, so that the heat recovery efficiency of the entire system is improved, and further improvement in the heat efficiency of the absorption refrigeration apparatus can be expected.
[0139]
Other functions and effects are the same as those in the first embodiment, and thus description thereof is omitted.
[0140]
Eighth embodiment
FIG. 8 shows an absorption refrigeration system Z according to an eighth embodiment of the present invention. ₈ Is shown.
[0141]
This absorption refrigeration system Z ₈ Is a condenser C, an absorber A, an evaporator E, and three solution heat exchangers H, respectively. ₃ , H ₂ , H ₁ And regenerator G ₃ , G ₂ , G ₁ And three drain heat exchangers D in addition to the above. ₁ , D ₂ , D ₃ And one exhaust heat exchanger K, and these devices are operatively connected by a solution piping system and a refrigerant piping system to constitute a circulation cycle of the refrigerant and the absorbing solution.
[0142]
The low-temperature solution heat exchanger H is connected to the dilute solution pipe 21 connected to the absorber A. ₁ And the first drain heat exchanger D ₁ To be heated and the third drain heat exchanger D ₃ And the low-temperature solution heat exchanger H ₁ An absorption solution branch pipe 47 connecting the front and rear of the absorption solution is provided. In addition, the second branch pipe 21B has a medium temperature solution heat exchanger H ₂ And the second drain heat exchanger D ₂ Through the heated side of the medium-temperature solution heat exchanger H ₂ An absorption solution branch pipe 48 connecting the front and rear of the absorption solution is provided.
[0143]
Medium temperature regenerator G ₂ The refrigerant drain pipe 34 connected to the outlet side of the solution heating unit 9 is connected to the second drain heat exchanger D ₂ Is branched off to the refrigerant drain pipe 36 immediately before. The refrigerant drain pipe 34 is connected to the second drain heat exchanger D ₂ And the refrigerant drain pipe 36 is connected to a third drain heat exchanger D ₃ After that, these two pipes 34 and 36 are merged and connected to the condenser C.
[0144]
Low temperature regenerator G ₁ The refrigerant drain pipe 35 connected to the outlet side of the solution heating unit 10 is connected to the first drain heat exchanger D ₁ Drain heat exchanger D of the refrigerant drain pipe 34 through the heating side of ₃ It is connected to the exit side.
[0145]
High temperature regenerator G ₃ The residual heat pipe 50 passing through the heating side of the exhaust heat exchanger K is connected to the outlet side of the solution heating unit 14.
[0146]
Other configurations are the same as those in the first embodiment, and a description thereof will be omitted.
[0147]
With this configuration, the dilute solution La supplied from the absorber A by the solution pump LP is supplied to the low-temperature solution heat exchanger H ₁ , A part of which branches into the low-temperature solution heat exchanger H ₁ Low-temperature regenerator G that passes through the heated side of ₁ Low temperature solution L from ₁ Preheated by heat exchange with Another part is the first drain heat exchanger D ₁ Low-temperature regenerator G that passes through the heated side of ₁ Drain from steam Dr ₁ And heat is exchanged with the preheater, and the third drain heat exchanger D ₃ Medium-temperature regenerator G that passes through the heated side of ₂ From the second drain heat exchanger D ₂ Drain Dr branched on the inlet side of the ₂ Preheated by heat exchange with The dilute solutions La thus branched and individually preheated, respectively, are merged again and then branched again into the first branch pipe 21A and the second branch pipe 21B.
[0148]
The dilute solution La branched to the first branch pipe 21A is supplied to the high-temperature solution heat exchanger H. ₃ High-temperature regenerator G that passes through the heated side of ₃ Hot solution L from ₃ Is preheated by heat exchange with the residual heat Q of the external heat source J passing through the heated side of the exhaust heat exchanger K and passing through the heated side. Bowl G ₃ Flows into.
[0149]
Further, the dilute solution La branched to the second branch pipe 21B side is further supplied to the intermediate temperature solution heat exchanger H. ₂ , A part of which is divided into the intermediate temperature solution heat exchanger H ₂ The intermediate-temperature regenerator G passing through the heated side of the ₂ Medium-temperature concentrated solution L ₂ Is preheated by heat exchange with the other part, and the other part is the second drain heat exchanger D ₂ The intermediate-temperature regenerator G passing through the heated side of the ₂ From the second drain heat exchanger D ₂ Drain Dr branched on the inlet side of the ₂ Preheated by heat exchange with The dilute solutions La branched and individually preheated as described above are merged again, and then the intermediate temperature regenerator G ₂ Flows into.
[0150]
Absorption refrigeration system Z according to this embodiment ₈ Has the following effects.
[0151]
That is, the high-temperature regenerator G ₃ High temperature regenerator G of external heat source J for heating ₃ Is heated by the residual heat Q after heating, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and the COP of the entire system can be reduced. Further improvement can be expected.
[0152]
In addition, low temperature regenerator G ₁ And medium temperature regenerator G ₂ Drain Dr generated in ₁ , Dr ₂ Is used to heat the dilute solution La, so that the vapor drain Dr ₁ , Dr ₂ Can be effectively used for preheating the dilute solution La, and the thermal efficiency of the entire system can be further promoted.
[0153]
Further, the first and third drain heat exchangers D are connected to the dilute solution La in the absorption solution branch pipe 47 branched from the dilute solution pipe 21. ₁ , D ₃ In the absorption solution branch pipe 48 branched from the second branch pipe 21B, the second drain heat exchanger D ₂ Then, each of the dilute solutions La is mixed with the vapor drain Dr. ₁ , Dr ₂ , So that the steam drain Dr ₁ , Dr ₂ Since the amount of the absorbing solution heated by the retained heat is small, the absorbing solution can be efficiently preheated.
[0154]
Also, the steam drain Dr ₂ Is branched into a refrigerant drain pipe 34 side and a refrigerant drain pipe 36 side, and the dilute solution La is heated in each of the refrigerant drain pipes 34 and 36. ₂ Can distribute the heating of the dilute solution La with high heat, and the preheating effect on the dilute solution La is promoted.
[0155]
Other functions and effects are the same as those in the first embodiment, and thus description thereof is omitted.
[0156]
Ninth embodiment
FIG. 9 shows an absorption refrigeration system Z according to a ninth embodiment of the present invention. ₉ The working cycle is shown.
[0157]
This absorption refrigeration system Z ₉ Is a condenser C, an absorber A, an evaporator E, and three solution heat exchangers H, respectively. ₃ , H ₂ , H ₁ And regenerator G ₃ , G ₂ , G ₁ And a drain heat exchanger D in addition to the above. ₁ , D ₂ And three waste heat exchangers K ₁ , K ₂ , K ₃ These devices are operatively connected to each other by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.
[0158]
The dilute solution pipe 21 connected to the absorber A is a low-temperature solution heat exchanger H ₁ After passing through the side to be heated, the first branch pipe 21A and the second branch pipe 21B are branched. The first branch pipe 21A is connected to the high-temperature solution heat exchanger H ₃ High-temperature exhaust heat exchanger K ₃ High temperature regenerator G through the heated side of ₃ It is connected to the. The second branch pipe 21B is provided with a medium temperature solution heat exchanger H. ₂ Pass through the heated side of the ₂ Medium-temperature regenerator G ₂ It is connected to the. Therefore, the dilute solution La flowing out of the absorber A is supplied to the low-temperature solution heat exchanger H. ₁ Branch after passing through the heated side of the high-temperature solution heat exchanger H ₃ And high-temperature exhaust heat exchanger K ₃ Via high temperature regenerator G ₃ And the other is a medium temperature solution heat exchanger H ₂ And medium temperature exhaust heat exchanger K ₂ Medium temperature regenerator G via ₂ Will flow into
[0159]
The low-temperature solution heat exchanger H is connected to the dilute solution pipe 21. ₁ And the first drain heat exchanger D ₁ Of the low-temperature solution heat exchanger H ₁ Is connected to the middle solution heat exchanger H in the second branch line 21B. ₂ And the second drain heat exchanger D ₂ Through the heated side of the medium-temperature solution heat exchanger H ₂ An absorption solution branch pipe 48 connecting the front and rear of the absorption solution is provided.
[0160]
Also, medium temperature regenerator G ₂ The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 in the second embodiment is connected to the second drain heat exchanger D ₂ Is connected to the condenser C through the heating side of the condenser C.
[0161]
In addition, low temperature regenerator G ₁ The refrigerant drain pipe 35 connected to the outlet side of the solution heating unit 10 in the first drain heat exchanger D ₁ Through the heating side of the second drain heat exchanger D ₂ Is connected to the refrigerant drain pipe 34 at the outlet side.
[0162]
Further, the intermediate temperature regenerator G ₂ Connected to the intermediate temperature regenerator G ₂ Medium concentrated solution L flowing out of ₂ Is connected to the medium-temperature solution heat exchanger H ₂ And the low-temperature exhaust heat exchanger K ₁ Low-temperature regenerator G through the heated side of ₁ It is connected to the.
[0163]
The high temperature regenerator G ₃ The residual heat pipe 50 is connected to the outlet side of the solution heating unit 14 in the above. The residual heat pipe 50 is connected to the high-temperature exhaust heat exchanger K. ₃ Immediately before the first residual heat branch pipe 51 and the second residual heat branch pipe 52, the first residual heat branch pipe 51 is connected to the high-temperature exhaust heat exchanger K. ₃ Pass through the heating side of. On the other hand, the second residual heat branch pipe 52 is further provided with the intermediate-temperature exhaust heat exchanger K. ₂ And the low-temperature exhaust heat exchanger K ₁ And a path that passes through the heating side.
[0164]
Other configurations are the same as those in the first embodiment, and a description thereof will be omitted.
[0165]
With the above-described configuration, the dilute solution La supplied from the absorber A by the solution pump LP is supplied to the low-temperature solution heat exchanger H ₁ , A part of which branches into the low-temperature solution heat exchanger H ₁ Low-temperature regenerator G that passes through the heated side of ₁ Low temperature concentrated solution L from ₁ And heat is exchanged with the first drain heat exchanger D. ₁ The low-temperature regenerator G passing through the heated side ₁ Drain from steam Dr ₁ Preheated by heat exchange with The dilute solutions La thus branched and individually preheated, respectively, are merged again and then branched again into the first branch pipe 21A and the second branch pipe 21B.
[0166]
The dilute solution La branched to the first branch pipe 21A is supplied to the high-temperature solution heat exchanger H. ₃ High temperature concentrated solution L passing through the heated side of ₃ And heat is exchanged with the preheated heat exchanger K. ₃ Is preheated by exchanging heat with the residual heat Q of the external heat source J passing through the heated side of the external heat source J. ₃ Flows into.
[0167]
On the other hand, the dilute solution La branched to the side of the second branch pipe 21B is further supplied to the intermediate temperature solution heat exchanger H ₂ , A part of which is divided into the intermediate temperature solution heat exchanger H ₂ The intermediate-temperature regenerator G passing through the heated side of the ₂ Medium-temperature concentrated solution L ₂ Is preheated by heat exchange with the other part, and the other part is the second drain heat exchanger D ₂ The intermediate-temperature regenerator G passing through the heated side of the ₂ Drain from steam Dr ₂ Preheated by heat exchange with The dilute solutions La branched in this way and individually preheated are merged again, and then mixed with the intermediate-temperature exhaust heat exchanger K. ₂ Is preheated by exchanging heat with the residual heat Q passing through the heated side of the medium-temperature regenerator G. ₂ Flows into. The medium temperature regenerator G ₂ Medium concentrated solution L flowing out of ₂ Is the medium temperature solution heat exchanger H ₂ After passing through the heating side of the low-temperature exhaust heat exchanger K ₁ Through the heated side of the low-temperature regenerator G ₁ Flows into.
[0168]
Absorption refrigeration system Z according to this embodiment ₉ Has the following effects.
[0169]
That is, the high-temperature regenerator G ₃ High temperature regenerator G of external heat source J for heating ₃ Is heated by the residual heat Q after heating, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and the COP of the entire system can be reduced. Further improvement can be expected.
[0170]
Further, the residual heat pipe 50 through which the residual heat Q flows is branched into a first residual heat branch pipe 51 and a second residual heat branch pipe 52, and heating of the dilute solution La is performed in each of the residual heat branch pipes 51 and 52. Is performed, the heat having a high residual heat Q can be distributed to the dilute solution La, and the preheating effect on the absorption solution is promoted.
[0171]
In addition, low temperature regenerator G ₁ And medium temperature regenerator G ₂ Drain Dr generated in ₁ , Dr ₂ Is used to heat the dilute solution La, so that the vapor drain Dr ₁ , Dr ₂ Can be effectively used for preheating the dilute solution La, and the thermal efficiency of the entire system can be further promoted.
[0172]
Further, the first drain heat exchanger D is connected to the absorption solution branch pipe 47 branched from the dilute solution pipe 21. ₁ And the second drain heat exchanger D in the absorption solution branch pipe 48 branched from the second branch pipe 21B. ₂ Then, each of the dilute solutions La is mixed with the vapor drain Dr. ₁ , Dr ₂ , So that the steam drain Dr ₁ , Dr ₂ Since the amount of the absorbing solution heated by the retained heat is small, the absorbing solution can be efficiently preheated.
[0173]
Other functions and effects are the same as those in the first embodiment, and thus description thereof is omitted.
[0174]
Tenth embodiment
FIG. 10 shows an absorption refrigeration system Z according to a tenth embodiment of the present invention. ₁₀ The working cycle is shown.
[0175]
This absorption refrigeration system Z ₁₀ Is a condenser C, an absorber A, an evaporator E, and three solution heat exchangers H, respectively. ₃ , H ₂ , H ₁ And regenerator G ₃ , G ₂ , G ₁ And a drain heat exchanger D in addition to the above. ₁ , D ₂ And two waste heat exchangers K ₃ , K ₂ These devices are operatively connected to each other by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.
[0176]
The dilute solution pipe 21 connected to the absorber A is a low-temperature solution heat exchanger H ₁ After passing through the side to be heated, the first branch pipe 21A and the second branch pipe 21B are branched. The first branch pipe 21A is connected to the high-temperature solution heat exchanger H ₃ High-temperature exhaust heat exchanger K ₃ High temperature regenerator G through the heated side of ₃ It is connected to the. The second branch pipe 21B is provided with a medium temperature solution heat exchanger H. ₂ Medium-temperature regenerator G ₂ It is connected to the. Therefore, the dilute solution La flowing out of the absorber A is supplied to the low-temperature solution heat exchanger H. ₁ Branch after passing through the heated side of the high-temperature solution heat exchanger H ₃ And high-temperature exhaust heat exchanger K ₃ Via high temperature regenerator G ₃ And the other is a medium temperature solution heat exchanger H ₂ Medium temperature regenerator G via ₂ Will flow into
[0177]
The low-temperature solution heat exchanger H is connected to the dilute solution pipe 21. ₁ And the first drain heat exchanger D ₁ Of the low-temperature solution heat exchanger H ₁ Is connected to the middle solution heat exchanger H in the second branch line 21B. ₂ And the second drain heat exchanger D ₂ To be heated and the intermediate-temperature exhaust heat exchanger K ₂ And the medium-temperature solution heat exchanger H ₂ An absorption solution branch pipe 48 connecting the front and rear of the absorption solution is provided.
[0178]
Also, medium temperature regenerator G ₂ The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 in the second embodiment is connected to the second drain heat exchanger D ₂ Is connected to the condenser C through the heating side of the condenser C.
[0179]
In addition, low temperature regenerator G ₁ The refrigerant drain pipe 35 connected to the outlet side of the solution heating unit 10 in the first drain heat exchanger D ₁ Through the heating side of the second drain heat exchanger D ₂ Is connected to the refrigerant drain pipe 34 at the outlet side.
[0180]
The high temperature regenerator G ₃ The residual heat pipe 50 is connected to the outlet side of the solution heating unit 14 in the above. The residual heat pipe 50 is connected to the high-temperature exhaust heat exchanger K. ₃ Immediately before the first residual heat branch pipe 51 and the second residual heat branch pipe 52, the first residual heat branch pipe 51 is connected to the high-temperature exhaust heat exchanger K. ₃ Pass through the heating side of. On the other hand, the second residual heat branch pipe 52 is further provided with the intermediate-temperature exhaust heat exchanger K. ₂ And the intermediate-temperature exhaust heat exchanger K ₂ And a path that passes through the heating side.
[0181]
Other configurations are the same as those in the first embodiment, and a description thereof will be omitted.
[0182]
With the above-described configuration, the dilute solution La supplied from the absorber A by the solution pump LP is supplied to the low-temperature solution heat exchanger H ₁ , A part of which branches into the low-temperature solution heat exchanger H ₁ Low-temperature regenerator G that passes through the heated side of ₁ Low temperature concentrated solution L from ₁ And heat is exchanged with the first drain heat exchanger D. ₁ The low-temperature regenerator G passing through the heated side ₁ Drain from steam Dr ₁ Preheated by heat exchange with The dilute solutions La thus branched and individually preheated, respectively, are merged again and then branched again into the first branch pipe 21A and the second branch pipe 21B.
[0183]
The dilute solution La branched to the first branch pipe 21A is supplied to the high-temperature solution heat exchanger H. ₃ High temperature concentrated solution L passing through the heated side of ₃ And heat is exchanged with the preheated heat exchanger K. ₃ Is preheated by exchanging heat with the residual heat Q of the external heat source J passing through the heated side of the external heat source J. ₃ Flows into.
[0184]
On the other hand, the dilute solution La branched to the side of the second branch pipe 21B is further supplied to the intermediate temperature solution heat exchanger H ₂ , A part of which is divided into the intermediate temperature solution heat exchanger H ₂ The intermediate-temperature regenerator G passing through the heated side of the ₂ Medium-temperature concentrated solution L ₂ Is preheated by heat exchange with the other part, and the other part is the second drain heat exchanger D ₂ The intermediate-temperature regenerator G passing through the heated side of the ₂ Drain from steam Dr ₂ And heat is exchanged with the intermediate heat exhaust heat exchanger K. ₂ Is preheated by exchanging heat with the residual heat Q of the external heat source J passing through the heating side. The dilute solutions La thus branched and individually preheated, respectively, merge again, and then form the intermediate temperature regenerator G. ₂ Flows into.
[0185]
Absorption refrigeration system Z according to this embodiment ₁₀ Has the following effects.
[0186]
That is, the high-temperature regenerator G ₃ High temperature regenerator G of external heat source J for heating ₃ Is heated by the residual heat Q after heating, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and the COP of the entire system can be reduced. Further improvement can be expected.
[0187]
Further, the residual heat pipe 50 through which the residual heat Q flows is branched into a first residual heat branch pipe 51 and a second residual heat branch pipe 52, and heating of the dilute solution La is performed in each of the residual heat branch pipes 51 and 52. Is performed, the heat having a high residual heat Q can be distributed to the dilute solution La, and the preheating effect on the absorption solution is promoted.
[0188]
In addition, low temperature regenerator G ₁ And medium temperature regenerator G ₂ Drain Dr generated in ₁ , Dr ₂ Is used to heat the dilute solution La, so that the vapor drain Dr ₁ , Dr ₂ Can be effectively used for preheating the dilute solution La, and the thermal efficiency of the entire system can be further promoted.
[0189]
Further, the first drain heat exchanger D is connected to the absorption solution branch pipe 47 branched from the dilute solution pipe 21. ₁ And the second drain heat exchanger D in the absorption solution branch pipe 48 branched from the second branch pipe 21B. ₂ Then, each of the dilute solutions La is mixed with the vapor drain Dr. ₁ , Dr ₂ , So that the steam drain Dr ₁ , Dr ₂ Since the amount of the absorbing solution heated by the retained heat is small, the absorbing solution can be efficiently preheated.
[0190]
Other functions and effects are the same as those in the first embodiment, and thus description thereof is omitted. In the present embodiment, the solution heat exchanger H provided in the branch pipe 21B is connected to the branch pipe 21B branched from the dilute solution pipe 21. ₂ Is provided, and a waste heat exchanger K provided in the branch pipe 48 is provided. ₂ In the above, the absorbing solution is heated by the residual heat Q, but the solution heat exchanger H provided in the diluted solution pipe 21 is connected to the diluted solution pipe 21. ₁ A branch pipe 47 is provided around the pipe, and the exhaust heat exchanger K provided in the branch pipe 47 is provided. ₁ In, the absorbing solution may be heated by the residual heat Q.
[0191]
Eleventh embodiment
FIG. 11 shows an absorption refrigeration system Z according to an eleventh embodiment of the present invention. ₁₁ The working cycle is shown.
[0192]
This absorption refrigeration system Z ₁₁ Is a condenser C, an absorber A, an evaporator E, and three solution heat exchangers H, respectively. ₃ , H ₂ , H ₁ And regenerator G ₃ , G ₂ , G ₁ And a drain heat exchanger D in addition to the above. ₁ , D ₂ And three waste heat exchangers K ₁ , K ₂ , K ₃ These devices are operatively connected to each other by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.
[0193]
The dilute solution pipe 21 connected to the absorber A is a low-temperature solution heat exchanger H ₁ After passing through the side to be heated, the first branch pipe 21A and the second branch pipe 21B are branched. The first branch pipe 21A is connected to the high-temperature solution heat exchanger H ₃ High-temperature exhaust heat exchanger K ₃ High temperature regenerator G through the heated side of ₃ It is connected to the. The second branch pipe 21B is provided with a medium temperature solution heat exchanger H. ₂ Pass through the heated side of the ₂ Medium-temperature regenerator G ₂ It is connected to the. Therefore, the dilute solution La flowing out of the absorber A is supplied to the low-temperature solution heat exchanger H. ₁ Branch after passing through the heated side of the high-temperature solution heat exchanger H ₃ And high-temperature exhaust heat exchanger K ₃ Via high temperature regenerator G ₃ And the other is a medium temperature solution heat exchanger H ₂ And medium temperature exhaust heat exchanger K ₂ Medium temperature regenerator G via ₂ Will flow into
[0194]
The low-temperature solution heat exchanger H is connected to the dilute solution pipe 21. ₁ And the first drain heat exchanger D ₁ Of the low-temperature solution heat exchanger H ₁ Is connected to the middle solution heat exchanger H in the second branch line 21B. ₂ And the second drain heat exchanger D ₂ Through the heated side of the medium-temperature solution heat exchanger H ₂ An absorption solution branch pipe 48 connecting the front and rear of the absorption solution is provided.
[0195]
Also, medium temperature regenerator G ₂ The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 in the second embodiment is connected to the second drain heat exchanger D ₂ Is connected to the condenser C through the heating side of the condenser C.
[0196]
In addition, low temperature regenerator G ₁ The refrigerant drain pipe 35 connected to the outlet side of the solution heating unit 10 in the first drain heat exchanger D ₁ Through the heating side of the second drain heat exchanger D ₂ Is connected to the refrigerant drain pipe 34 at the outlet side.
[0197]
Further, the intermediate temperature regenerator G ₂ Connected to the intermediate temperature regenerator G ₂ Medium concentrated solution L flowing out of ₂ Is connected to the medium-temperature solution heat exchanger H ₂ And the low-temperature exhaust heat exchanger K ₁ Low-temperature regenerator G through the heated side of ₁ It is connected to the.
[0198]
The high temperature regenerator G ₃ The residual heat pipe 50 is connected to the outlet side of the solution heating unit 14 in the above. The residual heat pipe 50 is connected to the high-temperature exhaust heat exchanger K. ₃ Heating side, the intermediate-temperature exhaust heat exchanger K ₂ Heating side and the low-temperature exhaust heat exchanger K ₁ Sequentially pass through the heating side.
[0199]
Other configurations are the same as those in the first embodiment, and a description thereof will be omitted.
[0200]
With the above-described configuration, the dilute solution La supplied from the absorber A by the solution pump LP is supplied to the low-temperature solution heat exchanger H ₁ , A part of which branches into the low-temperature solution heat exchanger H ₁ Low-temperature regenerator G that passes through the heated side of ₁ Low temperature concentrated solution L from ₁ And heat is exchanged with the first drain heat exchanger D. ₁ The low-temperature regenerator G passing through the heated side ₁ Drain from steam Dr ₁ Preheated by heat exchange with The dilute solutions La thus branched and individually preheated, respectively, are merged again and then branched again into the first branch pipe 21A and the second branch pipe 21B.
[0201]
The dilute solution La branched to the first branch pipe 21A is supplied to the high-temperature solution heat exchanger H. ₃ High temperature concentrated solution L passing through the heated side of ₃ And heat is exchanged with the preheated heat exchanger K. ₃ Is preheated by exchanging heat with the residual heat Q of the external heat source J passing through the heated side of the external heat source J. ₃ Flows into.
[0202]
On the other hand, the dilute solution La branched to the side of the second branch pipe 21B is further supplied to the intermediate temperature solution heat exchanger H ₂ , A part of which is divided into the intermediate temperature solution heat exchanger H ₂ The intermediate-temperature regenerator G passing through the heated side of the ₂ Medium-temperature concentrated solution L ₂ Is preheated by heat exchange with the other part, and the other part is the second drain heat exchanger D ₂ The intermediate-temperature regenerator G passing through the heated side of the ₂ Drain from steam Dr ₂ Preheated by heat exchange with The dilute solutions La branched in this way and individually preheated are merged again, and then mixed with the intermediate-temperature exhaust heat exchanger K. ₂ Of the external heat source J passing through the heated side of the intermediate heat regenerator G after being exchanged with the residual heat Q of the external heat source J and preheated. ₂ Flows into. The medium temperature regenerator G ₂ Medium concentrated solution L flowing out of ₂ Is the medium temperature solution heat exchanger H ₂ After passing through the heating side of the low-temperature exhaust heat exchanger K ₁ Through the heated side of the low-temperature regenerator G ₁ Flows into.
[0203]
Absorption refrigeration system Z according to this embodiment ₁₁ Has the following effects.
[0204]
That is, the high-temperature regenerator G ₃ High temperature regenerator G of external heat source J for heating ₃ Is heated by the residual heat Q after heating, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and the COP of the entire system can be reduced. Further improvement can be expected.
[0205]
In addition, since the dilute solution La is heated in multiple stages by the residual heat Q of the external heat source J, that is, in series with the flow direction of the residual heat Q, the dilute solution La and the residual solution Q are exchanged with each other. The temperature difference with the heat Q is equalized as much as possible at each of the heating positions, the heat recovery efficiency of the entire system is improved, and further improvement in the heat efficiency of the absorption refrigeration apparatus can be expected.
[0206]
In addition, low temperature regenerator G ₁ And medium temperature regenerator G ₂ Drain Dr generated in ₁ , Dr ₂ Is used to heat the dilute solution La, so that the vapor drain Dr ₁ , Dr ₂ Can be effectively used for preheating the dilute solution La, and the thermal efficiency of the entire system can be further promoted.
[0207]
Further, the first drain heat exchanger D is connected to the absorption solution branch pipe 47 branched from the dilute solution pipe 21. ₁ And the second drain heat exchanger D in the absorption solution branch pipe 48 branched from the second branch pipe 21B. ₂ Then, each of the dilute solutions La is mixed with the vapor drain Dr. ₁ , Dr ₂ , So that the steam drain Dr ₁ , Dr ₂ Since the amount of the absorbing solution heated by the retained heat is small, the absorbing solution can be efficiently preheated.
[0208]
Other functions and effects are the same as those in the first embodiment, and thus description thereof is omitted.
[0209]
Although described in each of the above embodiments, the number of drain heat exchangers and exhaust heat exchangers does not necessarily need to be the same as the number of each embodiment, and may be different from this. The embodiments may be combined.
[0210]
【The invention's effect】
According to the invention of claim 1, the dilute solution La coming out of the absorber A is branched, and one of the dilute solutions La is a high-temperature regenerator G. ₃ And the other is a medium temperature regenerator G ₂ So that the intermediate temperature regenerator G ₂ In this case, the dilute solution La in a non-concentrated state flows in as it is, so that, for example, the high-temperature regenerator G ₃ As compared with the case where the heat-concentrated absorption solution flows into the medium-temperature regenerator G, the concentration of the absorption solution becomes lower and the boiling temperature thereof becomes lower accordingly. ₂ High-temperature regenerator G as a heating source for the amount of the lowering of the boiling temperature of the absorbing solution of ₃ , The high temperature regenerator G proportional to the refrigerant vapor temperature can be set low. ₃ Can be set low, and as a result, there is an effect that it is possible to provide an absorption type refrigerating apparatus having a low operating pressure and good operability.
[0211]
Further, since the dilute solution La is branched, for example, the entire amount of the dilute solution La is directly changed to the high-temperature regenerator G. ₃ High-temperature regenerator G ₃ As a result, the high-temperature regenerator G ₃ In this case, the amount of sensible heat is reduced by an amount corresponding to the small amount of the absorbing solution to be heated and boiled. ₃ Heat required for heating (ie, the regenerator G) ₃ (The amount of heat input into the system) is also reduced, so that the coefficient of performance (COP) of the entire system is improved, and the efficiency of the absorption refrigeration system can be improved.
[0212]
The high-temperature regenerator G ₃ High temperature solution heat exchanger H just before ₃ In the above, the heat transfer area can be reduced by an amount corresponding to the decrease in the amount of the absorbing solution flowing therein, thereby making it possible to reduce the size of the heat transfer area, thereby contributing to the downsizing of the absorption refrigeration apparatus. .
[0213]
Further, the dilute solution La coming out of the absorber A is used as the low-temperature solution heat exchanger H. ₁ Branch after passing through the heated side of the high-temperature solution heat exchanger H ₃ High temperature regenerator G ₃ And the other is a medium temperature solution heat exchanger H ₂ Medium-temperature regenerator G after passing through the heated side of ₂ So that the high-temperature regenerator G ₃ The high-temperature solution heat exchanger H immediately before ₃ Solution La flowing through the intermediate temperature regenerator G ₂ Medium-temperature solution heat exchanger H immediately before ₂ Dilute solution La flowing through the low-temperature solution heat exchanger H ₁ At a high temperature regenerator G ₃ And the intermediate temperature regenerator G ₂ In this case, the required amount of heating heat of the absorbing solution is reduced, and an improvement in the thermal efficiency of the entire system can be expected.
[0214]
In addition, high temperature regenerator G ₃ Concentrated solution L which is heated and concentrated in ₃ Is low temperature regenerator G ₁ Is formed, there is no confluence where a large pressure difference occurs in the piping, and there is also an effect that a stable solution circulation can be obtained.
[0215]
In addition, since the number of regenerators and solution heat exchangers is set to three, the number of regenerators is increased to increase the number of concentration stages of the absorbing solution to increase the thermal efficiency, and the number of solution heat exchangers is increased. By comparing the merit of improving the performance of the absorption refrigeration system by increasing the heat recovery rate and the disadvantage of increasing the production cost by increasing the number of these regenerators and solution heat exchangers, By setting the number of regenerators and solution heat exchangers to three as in the present invention, it is possible to achieve both the performance and cost aspects of the absorption refrigeration system, and there is also an effect that it is extremely useful in practice.
[0216]
According to the invention of claim 2, the dilute solution La coming out of the absorber A is used as the low-temperature solution heat exchanger H. ₁ After passing through the heated side of the regenerator G ₃ ~ G ₁ So that the intermediate temperature regenerator G ₂ In this case, the dilute solution La in a non-concentrated state flows in as it is, so that, for example, the high-temperature regenerator G ₃ As compared with the case where the heat-concentrated absorption solution flows into the medium-temperature regenerator G, the concentration of the absorption solution becomes lower and the boiling temperature thereof becomes lower accordingly. ₂ High-temperature regenerator G as a heating source for the amount of the lowering of the boiling temperature of the absorbing solution of ₃ , The high temperature regenerator G proportional to the refrigerant vapor temperature can be set low. ₃ Can be set low, and as a result, there is an effect that it is possible to provide an absorption type refrigerating apparatus having a low operating pressure and good operability.
[0219]
In addition, since the dilute solution La is branched into three, for example, the entire amount of the dilute solution La is directly changed to the high-temperature regenerator G. ₃ And medium temperature regenerator G ₂ High-temperature regenerator G ₃ And medium temperature regenerator G ₂ As a result, the high-temperature regenerator G ₃ And medium temperature regenerator G ₂ In this case, the amount of sensible heat is reduced by an amount corresponding to the small amount of the absorbing solution to be heated and boiled. ₃ And medium temperature regenerator G ₂ Heat required for heating (ie, the regenerator G) _n (The amount of heat input into the system) is also reduced, so that the coefficient of performance (COP) of the entire system is improved, and the efficiency of the absorption refrigeration system can be improved.
[0218]
The high-temperature regenerator G ₃ And medium temperature regenerator G ₂ High temperature solution heat exchanger H just before ₃ And medium temperature solution heat exchanger H ₂ In the above, the heat transfer area can be reduced by an amount corresponding to the decrease in the amount of the absorbing solution flowing therein, thereby making it possible to reduce the size of the heat transfer area, thereby contributing to the downsizing of the absorption refrigeration apparatus. .
[0219]
Further, the dilute solution La coming out of the absorber A is used as the low-temperature solution heat exchanger H. ₁ After passing through the side to be heated, one of which is a high-temperature solution heat exchanger H ₃ High temperature regenerator G ₃ And the other is a medium temperature solution heat exchanger H ₂ Medium-temperature regenerator G after passing through the heated side of ₂ And the other is a low-temperature regenerator G ₁ So that the high-temperature regenerator G ₃ The high-temperature solution heat exchanger H immediately before ₃ Solution La flowing through the intermediate temperature regenerator G ₂ Medium-temperature solution heat exchanger H immediately before ₂ Solution La flowing through the low temperature regenerator G ₁ Together with the dilute solution La flowing into the low-temperature solution heat exchanger H ₁ Flows in a state where the reheater G ₃ ~ G ₁ In this case, the amount of heat required for heating the absorbing solution in the above is reduced, and there is also an effect that improvement in thermal efficiency of the entire system can be expected.
[0220]
In addition, high temperature regenerator G ₃ Concentrated solution L which is heated and concentrated in ₃ Is low temperature regenerator G ₁ Is formed, there is no confluence where a large pressure difference occurs in the piping, and there is also an effect that a stable solution circulation can be obtained.
[0221]
In addition, since the number of regenerators and solution heat exchangers is set to three, the number of regenerators is increased to increase the number of concentration stages of the absorbing solution to increase the thermal efficiency, and the number of solution heat exchangers is increased. By comparing the merit of improving the performance of the absorption refrigeration system by increasing the heat recovery rate and the disadvantage of increasing the production cost by increasing the number of these regenerators and solution heat exchangers, By setting the number of regenerators and solution heat exchangers to three as in the present invention, it is possible to achieve both the performance and cost aspects of the absorption refrigeration system, and there is also an effect that it is extremely useful in practice.
[0222]
As in the invention of claim 3, in the absorption refrigeration apparatus according to any one of claims 1 and 2, the high-temperature regenerator G is provided. ₃ High temperature regenerator G of external heat source J for heating ₃ Is configured to heat the circulation path of the absorbing solution with residual heat Q after heating, the amount of heat input to the external heat source J can be suppressed by the residual heat of the absorbing solution due to the effective use of the residual heat Q, As a result, a further improvement in the COP of the entire system can be expected.
[0223]
As in the invention of the fourth aspect, in the absorption refrigeration apparatus of the third aspect, each of the regenerators G from the outlet of the absorber A by the residual heat Q. ₃ ~ G ₁ The absorption solution in the path leading to the absorption solution inlet of ₃ ~ G ₁ Or the high-temperature regenerator G ₃ Is configured to heat the absorption solution immediately before the absorption solution inlet of each regenerator G from the outlet of the absorber A ₃ ~ G ₁ Is designed to heat the absorbing solution in the path leading to the absorbing solution inlet, the degree of freedom in selecting the heating position is large, so that the piping design for the residual heat is easy, and each of the regenerators G ₃ ~ G ₁ Is configured to heat the absorption solution immediately before the absorption solution inlet, the preheated absorption solution emits less heat (in other words, while maintaining a higher temperature) in each regenerator G. ₃ ~ G ₁ , The heat pre-heating effect is high and the heat efficiency can be further improved. ₃ If the absorption solution immediately before the absorption solution inlet is heated, the amount of heat input to the external heat source J can be reduced by the amount of preheating, so that a further improvement in COP can be expected.
[0224]
As in the invention of claim 5, in the absorption refrigeration apparatus according to any one of claims 3 and 4, the residual heat pipe 50 for the residual heat Q is branched into two or more residual heat branch pipes 51 and 52. When the absorption solution is heated in each of the residual heat branch pipes 51 and 52, heat having a high residual heat Q can be distributed to the absorption solution, and the preheating effect on the absorption solution is promoted. Become.
[0225]
As in the invention of claim 6, in the absorption refrigeration apparatus according to any one of claims 3, 4, and 5, when the absorption solution is heated in multiple stages by the residual heat Q, the absorption refrigeration apparatus may The temperature difference between the absorbing solution to be heat-exchanged and the residual heat Q is equalized as much as possible at each of the heating positions, thereby improving the heat recovery efficiency of the entire system and further improving the thermal efficiency of the absorption refrigeration system. Can be expected.
[0226]
As in the invention of claim 7, in the absorption refrigeration apparatus according to any one of claims 3, 4, 5, and 6, the dilute solution pipe 21 from the absorber A is provided in the branch pipe 21. Solution heat exchanger H ₁ A branch heat pipe H is provided in the branch pipe 21B provided in the branch pipe 21B branched from the dilute solution pipe 21. ₂ Is provided, and the absorption solution is heated by the residual heat Q in the branch pipe 47 or 48, so that the amount of the absorption solution heated by the residual heat Q is small, so that the absorption solution is efficiently absorbed. The solution can be preheated.
[0227]
As in the invention of claim 8, in the absorption refrigeration apparatus according to any one of claims 1, 2, 3, 4, 5, 6, and 7, each of the regenerators G ₂ , G ₁ Drain Dr generated in ₂ , Dr ₁ The absorption solution is heated by the ₂ , Dr ₁ Regenerator G by effectively utilizing the heat held by the ₃ , G ₂ , The thermal efficiency of the entire system can be further promoted.
[0228]
As in the ninth aspect of the present invention, in the absorption refrigeration apparatus according to the eighth aspect, each of the regenerators G ₂ , G ₁ Drain Dr generated in ₂ , Dr ₁ Are combined to heat the absorbing solution, the combined steam drain Dr ₂ , Dr ₁ Has a larger amount of heat, and can efficiently preheat the absorbing solution with the larger amount of heat.
[0229]
As in the invention of claim 10, in the absorption refrigeration apparatus according to any one of claims 8 and 9, the vapor drain Dr ₂ , Dr ₁ The regenerator G from the outlet of the absorber A ₂ , G ₁ The absorption solution in the path leading to the absorption solution inlet of ₂ , G ₁ Is configured to heat the absorption solution immediately before the absorption solution inlet of each regenerator G from the outlet of the absorber A ₂ , G ₁ Is designed to heat the absorption solution in the path leading to the absorption solution inlet, the degree of freedom in selecting the heating position is large, so that the steam drain piping design is easy and the regenerators G ₂ , G ₁ Is configured to heat the absorption solution immediately before the absorption solution inlet, the preheated absorption solution emits less heat (in other words, while maintaining a higher temperature) in each regenerator G. ₂ , G ₁ Since it flows into the air, the preheating effect is high and further improvement in thermal efficiency can be expected.
[0230]
As in the eleventh aspect, in the absorption refrigeration apparatus according to any one of the eighth, ninth, and tenth aspects, the vapor drain Dr ₂ , Dr ₁ Is branched into two or more, and the absorption solution is heated in each of the branch paths 34 and 36, the steam drain Dr ₂ , Dr ₁ Can be distributed with high heat, and the preheating effect on the absorbing solution is promoted.
[0231]
As in the twelfth aspect, in the absorption refrigeration apparatus according to any one of the eighth, ninth, tenth, and eleventh aspects, the vapor drain Dr ₂ , Dr ₁ When the absorption solution is heated in multiple stages, the absorption solution and the vapor drain Dr that exchange heat with each other are exchanged. ₂ , Dr ₁ And the temperature difference between them is equalized as much as possible at each of the heating positions, so that the heat recovery efficiency of the entire system is improved, and further improvement in the heat efficiency of the absorption refrigeration apparatus can be expected.
[0232]
As in the invention of claim 13, in the absorption refrigeration apparatus according to any one of claims 8, 9, 10, 11, and 12, a branch pipe 21B branched from the dilute solution pipe 21 from the absorber A is provided. Medium temperature solution heat exchanger H provided in branch pipe 21B ₂ A branch pipe 48 is provided which bypasses the steam drain Dr. ₂ When it is configured to heat by steam drain Dr ₂ Since the amount of the absorbing solution heated by the retained heat is small, the absorbing solution can be efficiently preheated.
[0233]
As in the invention of claim 14, the absorption refrigeration apparatus according to any one of claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, and 13, The absorber A and the evaporator E are divided into a plurality of stages having different refrigerant evaporation temperatures; ₁ And the condenser C is divided into a plurality of stages having different refrigerant condensation temperatures, or the absorber A and the evaporator E are divided into a plurality of stages having different refrigerant evaporation temperatures, and the low-temperature regenerator G is divided. ₁ When the condenser C is divided into a plurality of stages having different refrigerant condensing temperatures, the entire cycle is shifted to a low concentration side, the operating pressure of the system is reduced, and an absorption type refrigeration apparatus having good operability can be provided.
[0234]
As in the invention of claim 15, the absorption refrigeration apparatus according to any one of claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13 and 14 When cooling water Wa that circulates through the absorber A and the condenser C to cool them together is configured to flow from the condenser C side to the absorber A side, for example, the cooling water Wa Is supplied to the condenser C with cooling water Wa having a lower temperature than in the case where the water flows from the absorber A side to the condenser C side, so that the cooling capacity of the condenser C is improved. Low temperature regenerator G connected to condenser C ₁ Operating pressure of the low-temperature regenerator G ₁ , The highest operating pressure of the entire cycle governed by the operating pressure of the ₃ , The operating pressure of the refrigeration system is reduced, and an absorption refrigeration apparatus having better operability can be provided.
[Brief description of the drawings]
FIG. 1 is an operation cycle diagram of an absorption refrigeration apparatus according to a first embodiment of the present invention.
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FIG. 2 is an operation cycle diagram of an absorption refrigeration apparatus according to a second embodiment of the present invention.
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FIG. 3 is an operation cycle diagram of an absorption refrigeration apparatus according to a third embodiment of the present invention.
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FIG. 4 is an operation cycle diagram of an absorption refrigeration apparatus according to a fourth embodiment of the present invention.
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FIG. 5 is an operation cycle diagram of an absorption refrigeration apparatus according to a fifth embodiment of the present invention.
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FIG. 6 is an operation cycle diagram of an absorption refrigeration apparatus according to a sixth embodiment of the present invention.
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FIG. 7 is an operation cycle diagram of an absorption refrigeration apparatus according to a seventh embodiment of the present invention.
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FIG. 8 is an operation cycle diagram of an absorption refrigeration apparatus according to an eighth embodiment of the present invention.
FIG. 9 is an operation cycle diagram of an absorption refrigeration apparatus according to a ninth embodiment of the present invention.
FIG. 10 is an operation cycle diagram of the absorption refrigeration apparatus according to the tenth embodiment of the present invention.
FIG. 11 is an operation cycle diagram of an absorption refrigeration apparatus according to an eleventh embodiment of the present invention.
[Explanation of symbols]
1 to 6 are containers, 7 and 8 are heat exchanging units, 9 and 10 are solution heating units, 11 is a heat exchanging unit, 12 is a solution sprayer, 13 is a refrigerant sprayer, 14 is a solution heating unit, and 21 is a dilute solution. Piping, 21A is a first branch pipe, 21B is a second branch pipe, 21C is a third branch pipe, 25 is a low temperature solution pipe, 26 is a medium temperature solution pipe, 27 is a high temperature solution pipe, 29 is a liquid refrigerant pipe, and 30 is a liquid refrigerant pipe. A refrigerant pipe, 31 is a high-temperature steam pipe, 32 is a medium-temperature steam pipe, 33 is a refrigerant pipe, 34 is a refrigerant drain pipe, 35 is a refrigerant drain pipe, 36 is a refrigerant drain pipe, 41 is a cooling water inlet pipe, and 42 is a cooling water pipe. , 43 is a cooling water outlet pipe, 45 is a cooled liquid inlet pipe, 46 is a cooled liquid outlet pipe, 50 is a residual heat pipe, 51 is a first residual heat branch pipe, 52 is a second residual heat branch pipe, and A is Absorber, C is condenser, D ₁ ~ D ₃ Is a drain heat exchanger, Dr ₁ And Dr ₂ Is steam drain, E is evaporator, G ₁ ~ G ₃ Is a regenerator, H ₁ ~ H ₃ Is a solution heat exchanger, J is an external heat source, K and K ₁ ~ K ₃ Is the waste heat exchanger, L ₁ ~ L ₃ Is a concentrated solution, La is a dilute solution, LP is a solution pump, R ₁ ~ R ₃ Is refrigerant vapor, Ra is vaporized refrigerant, Rc is liquid refrigerant, Re is refrigerant, RP is refrigerant pump, Q is residual heat, Z ₁ ~ Z ₁₁ Is an absorption type refrigerator.

Claims (15)

At least one or more condensers (C), an evaporator (E), absorber (A) and three solution heat exchanger _(H 3 to H ₁₎ and regenerator _(G 3 ~G ₁₎ A solution piping and operatively connected in the system and the refrigerant piping system constitute a circulation cycle, supplying the absorption solution containing refrigerant to said high temperature generator (G 3 _{~G 1),} outside the high temperature generator (G ₃₎ The absorption solution is heated and boiled using the heat source (J) to generate refrigerant vapor, and the heat of the refrigerant vapor is used to heat and boil the absorption solution in the medium temperature regenerator (G ₂ ) to generate refrigerant vapor, An absorption refrigerating apparatus configured to heat and boil the absorption solution in the low-temperature regenerator (G ₁ ) using the heat of the refrigerant vapor to generate refrigerant vapor, which is discharged from the absorber (A). dilute solution (La) is branched after passing through the heated side of the low-temperature solution heat exchanger (H ₁₎ One of which flows into the high-temperature solution heat exchanger (H ₃₎ the high temperature generator passes through the heated side of the (G _3), concentrated high temperature flows are heated and concentrated in said high temperature generator (G ₃₎ The solution (L ₃ ) flows into the low-temperature regenerator (G ₁ ) after passing through the heating side of the high-temperature solution heat exchanger (H ₃ ), while the other flows into the medium-temperature solution heat exchanger (H ₂ ). medium temperature regenerator after passing through the heated side flows into the (G _2), middle temperature regenerator (G ₂₎ medium temperature concentrated solution flowing out is heated and concentrated in the (L _2), the intermediate temperature solution heat exchanger ( the flows into the low-temperature regenerator (G ₁₎ after passing through the heating side of the H _2), low-temperature concentrated solution (L 1 flowing is heated and concentrated in the cold regenerator (G _1)), the low-temperature solution heat After passing through the heating side of the exchanger (H ₁ ), it flows into the absorber (A). An absorption refrigeration apparatus characterized in that: At least one or more condensers (C), an evaporator (E), absorber (A) and three solution heat exchanger _(H 3 to H ₁₎ and regenerator _(G 3 ~G ₁₎ A solution piping and operatively connected in the system and the refrigerant piping system constitute a circulation cycle, supplying the absorption solution containing refrigerant to said high temperature generator (G 3 _{~G 1),} outside the high temperature generator (G ₃₎ The absorption solution is heated and boiled using the heat source (J) to generate refrigerant vapor, and the heat of the refrigerant vapor is used to heat and boil the absorption solution in the medium temperature regenerator (G ₂ ) to generate refrigerant vapor, An absorption refrigerating apparatus configured to heat and boil the absorption solution in the low-temperature regenerator (G ₁ ) using the heat of the refrigerant vapor to generate refrigerant vapor, which is discharged from the absorber (A). dilute solution (La) is three after passing through the heated side of the low-temperature solution heat exchanger (H ₁₎ Is branched, one of which flows into the high-temperature solution heat exchanger (H ₃₎ the high temperature generator passes through the heated side of the (G _3), the outflow is heated and concentrated in said high temperature generator (G ₃₎ The high-temperature concentrated solution (L ₃ ) flows into the low-temperature regenerator (G ₁ ) after passing through the heating side of the high-temperature solution heat exchanger (H ₃ ), and the other is the medium-temperature solution heat exchanger (H _2). medium temperature regenerator after passing through the heated side) (flows into the G _2), the medium-temperature concentrated solution (L 2 flowing is heated and concentrated in the middle temperature regenerator (G _2)), the intermediate temperature solution heat exchanger vessel the flows into the low-temperature regenerator (G ₁₎ after passing through the heating side of the (H _2), the other flows into the low temperature generator (G _1), heating concentrated in the cold regenerator (G ₁₎ cold concentrated solution (L ₁₎ is pressurized in the low-temperature solution heat exchanger (H ₁₎ which flows out is Absorption refrigerating apparatus characterized by being configured to flow into the absorber (A) after passing through the side. It is configured to heat the circulation path of the absorption solution in the residual heat after heating (Q) said high temperature regenerator (G ₃₎ of the external heat source (J) for heating the hot regenerator (G ₃₎ The absorption refrigeration apparatus according to any one of claims 1 and 2, characterized in that: Wherein the residual heat (Q), the absorption solution in the absorption solution inlet leading path of the absorber (A) wherein each regenerator from the outlet of (G 3 _{~G 1),} or each regenerator (G ₃ ~G The absorption solution immediately before the absorption solution inlet of ₁ ) or the absorption solution immediately before the absorption solution inlet of the high-temperature regenerator (G ₃ ) is heated. Absorption refrigeration equipment. The residual heat pipe (50) for the residual heat (Q) is branched into two or more residual heat branch pipes (51, 52), and the absorption solution is heated in each of the residual heat branch pipes (51, 52). The absorption refrigeration apparatus according to any one of claims 3 and 4, wherein the absorption refrigeration apparatus is configured as follows. The absorption refrigeration apparatus according to any one of claims 3, 4 and 5, wherein the absorption heat is heated in multiple stages by the residual heat (Q). The absorber (A) dilute solution pipe (21) to the rare solution pipe (21) with the solution heat exchanger in the (H ₁₎ branch line bypassing the (47) provided from, or the rare solution pipe The branch pipe (21B) branched from (21) is provided with a branch pipe (48) bypassing the solution heat exchanger (H ₂ ) provided in the branch pipe (21B), and the branch pipe (47) or (48) is provided. 7) The absorption refrigeration apparatus according to any one of claims 3, 4, 5, and 6, wherein the absorption solution is heated by the residual heat (Q). Each regenerator _(G 2), steam drain _(Dr 2) produced in _{(G 1),} claim 1, characterized in that it is configured to heat the absorption solution by (Dr ₁₎ 8. The absorption refrigeration apparatus according to any one of 3, 4, 5, 6, and 7. Each regenerator (G _2), the preceding claims, characterized by being composed (G ₁₎ with the resulting steam drain (Dr _2), so as to heat the absorption solution is merging _{(Dr 1)} 8. The absorption refrigeration apparatus according to 8. By the vapor drains (Dr ₂ ) and (Dr ₁ ), the absorption solution in the path from the outlet of the absorber (A) to the absorption solution inlet of the regenerators (G ₂ ) and (G ₁ ) or the regenerated solution vessel _{(G 2), (G 1} ) the claims 8 and 9 claims absorption according to one of to, characterized in that it is configured to heat the absorption solution immediately before the absorption solution inlet of Refrigeration equipment. The steam drains (Dr ₂ ) and (Dr ₁ ) are branched into two or more, and the branch solution (34) and (36) are configured to heat the absorbing solution in each of the branches (34) and (36). The absorption refrigeration apparatus according to any one of claims 8, 9 and 10, wherein The steam drain (Dr _2), absorption of _{(Dr 1)} according to any one of claims 8, 9, 10 and 11, characterized in that the heating of the absorption solution is configured to perform a multi-stage Type refrigeration equipment. A branch pipe (48) that bypasses a medium-temperature solution heat exchanger (H ₂ ) provided in the branch pipe (21B) to a branch pipe (21B) branched from the dilute solution pipe (21) from the absorber (A). 13. The apparatus according to claim 8, wherein the branch pipe (48) is configured to heat the absorbing solution by the vapor drain (Dr ₂ ). 14. The absorption refrigeration apparatus according to any one of the preceding claims. The absorber (A) and the evaporator (E) are divided into a plurality of stages having different refrigerant evaporation temperatures, or the low-temperature regenerator (G ₁ ) and the condenser (C) are divided into a plurality of stages having different refrigerant condensation temperatures. Or the absorber (A) and the evaporator (E) are divided into a plurality of stages having different refrigerant evaporation temperatures, and the low-temperature regenerator (G ₁ ) and the condenser (C) have the refrigerant condensing temperature. 14. Absorption refrigeration according to any one of claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, and 13, wherein the absorption refrigeration is divided into a plurality of different stages. apparatus. Cooling water (Wa), which circulates through the absorber (A) and the condenser (C) and cools them together, flows from the condenser (C) side to the absorber (A) side. The absorption refrigeration apparatus according to any one of claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13 and 14. .

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