JP2003294334A - Absorption refrigerator - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide an absorption refrigerator for reducing working pressure, and superior in efficiency by improving a circulating passage of an absorbing solution. <P>SOLUTION: A dilute solution La coming out of an absorber A is branched off, and one is allowed to flow in the highest temperature side regenerator G<SB>n</SB>by the whole quantity or a part of a branch quantity, and the other is allowed to flow in a low temperature side regenerator G<SB>n-1</SB>by the whole quantity or a part of a branch quantity, and is then further allowed to flow in a low temperature side regenerator G<SB>n-2</SB>. Such constitution reduces the concentration of the absorbing solution in the low temperature side regenerator G<SB>n-1</SB>, and also lowers a boiling temperature. A refrigerant vapor temperature is set low in the high temperature side regenerator G<SB>n</SB>being a heating source to the low temperature side regenerator G<SB>n-1</SB>, that is, the working pressure is set low in response to this, so that the absorption refrigerator for reducing the working pressure, and superior in operability is provided. <P>COPYRIGHT: (C)2004,JPO

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an absorption refrigeration system, and more particularly to an absorption refrigeration system equipped with a plurality of regenerators having different operating temperatures.

[0002]

2. Description of the Related Art Generally, an absorption refrigerating apparatus has a condenser, an evaporator, an absorber, a solution heat exchanger and a regenerator as basic constituent elements, and these constituent elements by a solution piping system and a refrigerant piping system. It is constructed by sequentially operatively connecting.

In such an absorption refrigerating apparatus, the dilute solution produced in the absorber is heated and concentrated in the regenerator to give a concentrated solution, which is then refluxed to the absorber while the dilute solution in the regenerator is diluted. The refrigerant vapor generated by heating and condensing the solution is condensed in the condenser to form a liquid refrigerant, the liquid refrigerant is evaporated in the evaporator, and the refrigerant vapor generated here is absorbed in the concentrated solution in the absorber. By generating a dilute solution by doing so, a circulation cycle of the absorbing solution and the refrigerant is realized.

Further, in this case, from the viewpoint of increasing the thermal efficiency of the refrigerating apparatus by recovering heat, heat exchange is performed between the heated concentrated solution flowing out from the regenerator and the dilute solution flowing into the regenerator. It is customary.

[0005]

In the absorption refrigeration system, it is known that increasing the thermal efficiency of the solution / refrigerant circulation system is the most effective in order to improve its performance. It has been proposed that a plurality of regenerators be provided and the heat of one external heat source be repeatedly reused as a method for realizing the above. That is, a plurality of regenerators having different operating temperatures are provided, and the refrigerant vapor generated by heating of the high temperature side regenerator operating at high temperature is introduced into the low temperature side regenerator operating at low temperature, and the regenerator is operated at the low temperature side. It is used as a heat source for heating the regenerator.

However, in the absorption type refrigerating apparatus, the internal pressure (operating pressure), particularly the operating pressure and temperature of the regenerator on the highest temperature side, increases with the plurality of regenerators, and the refrigerating apparatus High pressure and high temperature measures are required.

That is, in the absorption refrigeration system, when a plurality of regenerators having different operating temperatures are provided as described above, the absorption solution of the low temperature side regenerator is heated and concentrated at the refrigerant vapor temperature of the high temperature side regenerator. Therefore, the refrigerant vapor temperature of the high temperature side regenerator must be equal to or higher than the boiling temperature of the absorbing solution of the low temperature side regenerator, and therefore the operating pressure of the high temperature side regenerator is proportional to the refrigerant vapor temperature. Therefore, it becomes necessary to take measures against high pressure and high temperature of refrigeration equipment.

Therefore, the present invention has been made for the purpose of providing an absorption type refrigerating apparatus having a low operating pressure and high efficiency by improving the circulation route of the absorbing solution.

[0009]

In the present invention, the following constitution is adopted as a concrete means for solving such a problem.

In the first invention of the present application, at least one or more condenser C, evaporator E, absorber A and n (n ≧ 3)
Solution heat exchangers H _{n to} H ₁ and regenerators G _{n to} G ₁ are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle, and are generated in the high temperature side regenerator G _n . Refrigerant vapor is sequentially introduced into the low temperature side regenerator G _n-1 , and the low temperature side regenerator G _n
In an absorption type refrigerating apparatus, which is used as a heat source for _{n- 1} to repeat heating and concentration of the absorption solution of the low temperature side regenerator G _{n-1 to} a regenerator G _{1 having} the lowest operating temperature, The dilute solution La discharged from the absorber A is branched, and one side of the diluted solution La is the regenerator G _n on the highest temperature side in all or part of the branched amount.
The other is characterized in that all or part of the branch amount flows into the low temperature side regenerator G _n-1 and then further flows into the low temperature side regenerator G _n-2 . .

In a second invention of the present application, in the absorption refrigerating apparatus according to the first invention, the dilute solution La discharged from the absorber A is branched after passing through the solution heat exchanger H ₁ at the lowest temperature side. One of which is the regenerator G _n on the highest temperature side.
The preceding solution heat exchanger is flown through the H _n, it the other configured such that flow through the solution heat exchanger H _n-1 immediately preceding the regenerator G _n-1 of the low-temperature side Is characterized by.

According to a third invention of the present application, in the absorption refrigerating apparatus according to the first invention, the dilute solution La discharged from the absorber A is branched just before the solution heat exchanger H ₁ on the lowest temperature side. , One of which is the regenerator G _n on the highest temperature side
Just before the solution heat exchanger is flown through the H _n, the other is the lowest temperature side of the solution heat exchanger H ₁ a after passing through the cold side of the regenerator the preceding solution heat exchanger to G _n-1 It is characterized in that it is configured to flow in via H _n-1 .

In the fourth invention of the present application, the above-mentioned second or third invention is provided.
In the absorption refrigerating apparatus according to the invention described above, the dilute solution La on the other side is further branched just before the solution heat exchanger H _n-1 , and the one re-branching solution La ₁ is the solution heat exchanger. After flowing into the low temperature side regenerator G _n-1 via H _n-1 , it merges with the other re-branching solution La ₂ and further flows into the low temperature side regenerator G _n-2. It is characterized by having done.

In the fifth invention of the present application, at least one or more condensers C, evaporators E, absorbers A and n (n ≧ 3)
Solution heat exchangers H _{n to} H ₁ and regenerators G _{n to} G ₁ are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle, and are generated in the high temperature side regenerator G _n . Refrigerant vapor is sequentially introduced into the low temperature side regenerator G _n-1 , and the low temperature side regenerator G _n
In an absorption type refrigerating apparatus, which is used as a heat source for _{n- 1} to repeat heating and concentration of the absorption solution of the low temperature side regenerator G _{n-1 to} a regenerator G _{1 having} the lowest operating temperature, The dilute solution La discharged from the absorber A is branched into n pieces after passing through the heated side of the solution heat exchanger H ₁ on the lowest temperature side, and the total amount of each branched amount is supplied to the respective regenerators G _{n to} G ₁ . It flowed, and characterized by being configured so as to flow into the regenerator G _n-2 of the concentrated solution L _n-1 further cold side of the regenerator G _n-1 on the low temperature side.

In the sixth invention of the present application, the above-mentioned first, second, and
In the absorption refrigeration system according to the third, fourth or fifth aspect of the invention, the concentrated solution L _n from the hottest regenerator G _n is branched after passing through the heating side of the solution heat exchanger H _n. some are characterized by being configured so as to flow into the regenerator G _n-2 of the concentrated solution L _n-1 with further cold side of the regenerator G _n-1 of the low temperature side.

In the seventh invention of the present application, the above-mentioned first, second, and
In the absorption type refrigerating apparatus according to the third, fourth or fifth aspect of the invention, the concentrated solution L _n-1 from the regenerator G _n-1 on the low temperature side is fed to the heating side of the solution heat exchanger H _n-1. Branch after passing
It is characterized in that a part thereof flows out from the regenerator G _n on the highest temperature side and joins with the concentrated solution L _n after passing through the heating side of the solution heat exchanger H _n .

In the eighth invention of the present application, the above-mentioned first, second, and
Third, fourth, fifth, sixth or the absorption type refrigerating apparatus according to the seventh aspect of the invention, the residual after heating the regenerator G _n of the external heat source J for heating the regenerator G _n of the highest temperature side It is characterized in that the circulation route of the absorbing solution is heated by the heat Q.

According to a ninth invention of the present application, in the absorption refrigerating apparatus according to the eighth invention, the residual heat Q causes the residual solution Q to flow from the outlet of the absorber A to the absorbent solution inlet of each of the regenerators G _{n to} G _1. To the absorption solution in the path leading to the above, or the absorption solution immediately before the absorption solution inlet of each of the regenerators G _{n to} G ₁ or the absorption solution immediately before the absorption solution inlet of the regenerator G _n on the highest temperature side. It is characterized in that it is configured to.

According to a tenth invention of the present application, in the absorption refrigerating apparatus according to the eighth or ninth invention, the residual heat pipe 50 for the residual heat Q is replaced by two or more residual heat branch pipes 51, 5.
It is characterized in that the absorption solution is heated in each of the residual heat branch pipes 51 and 52.

In the eleventh invention of the present application, the above eighth and ninth aspects are provided.
Alternatively, the absorption refrigerating apparatus according to the tenth invention is characterized in that the absorption solution is heated in multiple stages by the residual heat Q.

According to a twelfth invention of the present application, in the absorption refrigerating apparatus according to the eighth, ninth, tenth or eleventh invention, the dilute solution pipe 23 or 2 from the absorber A is used.
Branch pipe 48 bypassing the solution heat exchanger H _N (N = 1 to n) provided in the diluted solution pipe 23 or 21B in 1B.
Is provided, and the absorption solution is heated by the residual heat Q in the branch pipe 48.

In the thirteenth invention of the present application, the above-mentioned first, second, third, fourth, fifth, sixth, seventh, eighth, ninth, first
In the absorption type refrigerating apparatus according to the 0th, 11th or 12th aspect of the invention, the vapor drain D generated in the regenerators G _{n-1 to} G ₁
It is characterized by being configured to heat the absorption solution by r _n-1 ~Dr _1.

According to a fourteenth invention of the present application, in the absorption refrigerating apparatus according to the thirteenth invention, each of the regenerators G
It is characterized in _{that n-1} ~G each steam drain Dr _n-1 ~Dr ₁ produced in ₁ is configured to heat the absorption solution joins.

[0024] In the fifteenth invention of the present application, the absorption type refrigerating apparatus according to the invention of the thirteenth or fourteenth, by the steam drain Dr _n-1 ~Dr _1, said absorber each regenerator from the exit of the A the absorbent solution of G _n-1 ~G ₁ of absorbent solution inlet leading path or the absorption solution immediately before the absorption solution inlet of each regenerator G _n-1 ~G _1, by being configured to heat It has a feature.

In the sixteenth invention of the present application, in the absorption refrigerating apparatus according to the thirteenth, fourteenth or fifteenth invention, the vapor drains Dr _{n-1 to} Dr ₁ are branched into two or more, and It is characterized in that the absorption solution is heated in each of the branch paths 34 and 36.

[0026] In the seventeenth invention of the present application, the thirteenth, the fourteenth, the absorption refrigerating apparatus according to the invention of the fifteenth or sixteenth, multi heating the absorption solution by the steam drain Dr _n-1 ~Dr 1 It is characterized in that it is configured to be performed in stages.

In the eighteenth invention of the present application, in the absorption refrigerating apparatus according to the thirteenth, fourteenth, fifteenth, sixteenth or seventeenth invention, the dilute solution pipe 23 from the absorber A is used.
Alternatively, 21B is provided with a branch pipe 48 that bypasses the solution heat exchanger H _N (N = 1 to n) provided in the dilute solution pipe 23 or 21B, and the absorption solution is introduced into the vapor drain Dr _{n in the} branch pipe 48. It is characterized by being configured to heat by _{-1 ~Dr 1.}

In the nineteenth invention of the present application, the above-mentioned first, second, third, fourth, fifth, sixth, seventh, eighth, ninth, first
0th, 11th, 12th, 13th, 14th, 15th, 1st
In the absorption type refrigeration system according to the sixth, seventeenth or eighteenth invention, the absorber A and the evaporator E are divided into a plurality of stages having different refrigerant evaporation temperatures, or the regenerator G _{1 at the} lowest temperature side.
And the condenser C is divided into a plurality of stages having different refrigerant condensing temperatures, or the absorber A and the evaporator E are divided into a plurality of stages having different refrigerant evaporation temperatures, and the regenerator G ₁ on the lowest temperature side and the condensing It is characterized in that the vessel C is divided into a plurality of stages having different refrigerant condensing temperatures.

In the twentieth invention of the present application, the first, second, third, fourth, fifth, sixth, seventh, eighth, ninth, first
0th, 11th, 12th, 13th, 14th, 15th, 1st
In the absorption refrigeration system according to the sixth, seventeenth, eighteenth or nineteenth aspect of the invention, cooling water Wa that circulates the absorber A and the condenser C to cool them together is provided from the side of the condenser C. It is characterized in that it is configured to flow toward the absorber A side.

In the twenty-first invention of the present application, the first, second, third, fourth, fifth, sixth, seventh, eighth, ninth, first
0th, 11th, 12th, 13th, 14th, 15th, 1st
The absorption refrigerating apparatus according to the sixth, seventeenth, eighteenth, nineteenth or twentieth aspect of the invention is characterized in that the number n of installed regenerators and solution heat exchangers is n = 3.

[0031]

According to the present invention, the following effects can be obtained by adopting such a configuration.

(1) According to the absorption refrigerating apparatus of the first invention of the present application, the dilute solution La discharged from the absorber A is branched, and one of the branched solutions has the highest total or partial branch amount. Flow into the regenerator G _n on the side of the other side, and the other flows into the regenerator G _n-2 of the low temperature side after all or part of the branch amount flows into the regenerator G _n-1 of the low temperature side. Therefore, in the regenerator G _n-1 on the low temperature side, the unconcentrated dilute solution La flows into the regenerator G _{n-1 as} it is, so that, for example, the absorption solution heated and concentrated in the regenerator G _n on the highest temperature side flows in. The concentration of the absorbing solution will be lower and the boiling temperature will be lower accordingly. Since the refrigerant vapor temperature in the highest temperature side regenerator G _n , which is the heating source, can be set low by the decrease in the boiling temperature of the absorbing solution in the low temperature side regenerator G _n-1 , the refrigerant vapor temperature can be set. The operating pressure of the regenerator G _n on the highest temperature side, which is proportional to, can also be set low, and as a result, it is possible to provide an absorption refrigerating device having a low operating pressure and good operability.

Further, it was branches the dilute solution La, for example, dilute solutions the total amount of La is directly compared with the case where flow into the above-mentioned highest temperature side regenerator G _n, outermost even the high-temperature side regenerator G _n The amount of inflow to is reduced. As a result, in the regenerator G _n on the highest temperature side, the amount of sensible heat is reduced by the amount of the absorbing solution heated and boiled here,
Correspondingly outermost that necessary for heating the hot side of the regenerator G _n calorimetry (i.e., the heat input to the regenerator G _n) since it also reduced, the coefficient of performance (COP) is improved by the absorption refrigerating apparatus as a whole system High efficiency can be achieved. Further, in the solution heat exchanger H _n just before the regenerator G _n on the highest temperature side, the heat transfer area can be reduced by the amount of the absorbed solution flowing into the solution heat exchanger H _n , and the size can be reduced. Therefore, it can contribute to downsizing of the absorption refrigeration system.

(2) According to the absorption refrigerating apparatus of the second invention of the present application, the following peculiar effect is obtained in addition to the effect described in (1) above. That is, in the absorption refrigerating apparatus of the present invention, the dilute solution La discharged from the absorber A is branched after passing through the heated side of the solution heat exchanger H ₁ on the lowest temperature side, and _one of them is branched on the highest temperature side. the regenerator G _n to allowed to flow through the solution heat exchanger H _n of the immediately preceding and the other solution heat exchanger immediately before the regenerator G _n-1 of the low-temperature side H _n-1
Since the structure so as to flow into through the above and highest temperature side of the regenerator G _n in dilute solution La flowing through the solution heat exchanger H _n immediately before, the low-temperature side of the regenerator G _{n Since} the dilute solution La flowing into the _-1 through the solution heat exchanger H _n-1 immediately before the _-1 flows in the preheated state in the solution heat exchanger H ₁ on the lowest temperature side, the above-mentioned highest temperature required amount of heat of absorption solution at the side of the regenerator G _n and the low temperature side of the regenerator G _n-1 Metropolitan reduced, can be expected to improve the thermal efficiency of the entire system.

(3) According to the absorption refrigerating apparatus of the third invention of the present application, in addition to the effect described in the above (1), the following unique effect is obtained. That is, in the absorption refrigeration system of the present invention, the dilute solution La discharged from the absorber A is branched just before the solution heat exchanger H ₁ on the lowest temperature side,
One of them flows into the regenerator G _n on the highest temperature side via the solution heat exchanger H _n immediately before, and the other _one passes through the heated side of the solution heat exchanger H ₁ on the lowest temperature side and then the low temperature. Since it is configured to flow into the regenerator G _n-1 on the side via the solution heat exchanger H _n-1 immediately before it, for example, the total amount of the dilute solution La is the solution heat exchanger H _n on the low temperature side. _-1 compared with the case of passing through the heated side of the solution heat exchanger H _{1 at} the lowest temperature side and the heated side of the solution heat exchanger H _{1 at} the lowest temperature side, the flow rate of each of the solution heat exchangers H _n-1 and H ₁ decreases. Therefore, the solution heat exchangers H _n-1 and H ₁ can be made compact, and the absorption refrigeration system can be made compact.

(4) According to the absorption refrigerating apparatus of the fourth invention of the present application, in addition to the effect described in the above (2) or (3), the following unique effect can be obtained. That is, in the absorption refrigeration system of the present invention, the dilute solution La on the other side is further branched just before the solution heat exchanger H _{n- 1} and the one re-branching solution La ₁ is the solution heat exchange. After flowing into the low temperature side regenerator G _n-1 via the reactor H _n-1 ,
Since the re-branching solution La ₂ merges with the other re-branching solution La ₂ and flows into the regenerator G _n-2 on the low temperature side, the re-branching solution is fed to the solution heat exchanger H _n-1 on the low temperature side. Only La ₁ flows in, for example, without re-branching, the entire amount of the other dilute solution La branched after passing through the heated side of the solution heat exchanger H ₁ on the lowest temperature side is directly passed to the solution heat exchanger. H
The flow rate in the solution heat exchanger H _n-1 is reduced as compared with the case where the solution heat exchanger H _n-1 is flown, and as a result, the solution heat exchanger H _n-1 can be made compact. .

(5) Absorption formula according to the fifth invention of the present application
According to the refrigeration system, the diluted solution La discharged from the absorber A is
Solution heat exchanger H on the lowest temperature side₁N after passing through the heated side of
Divide into individual pieces, and the total amount of each branch amount is for each regenerator Gn ~
G₁Flowing into the regenerator G on the low temperature side_n-1Concentrated solution L from_n-1
Is the regenerator G on the lower temperature side_n-2Configured to flow into
Therefore, the low temperature side regenerator G_n-1~ G₁At
Since the concentrated diluted solution La flows in as it is,
Regenerator G on the high temperature side_nAbsorption solution heat-concentrated in
The concentration of the absorption solution is lower than that when
As a result, the boiling temperature becomes lower. This low temperature side regeneration
Bowl G_n-1~ G₁The amount of decrease in the boiling temperature of the absorption solution of
Regenerator G on the highest temperature side that serves as a heating source_nRefrigerant vapor in
Since the temperature can be set low, the refrigerant vapor
Regenerator G on the highest temperature side proportional to temperature _nThe operating pressure of
Can be set low, resulting in a low operating pressure.
It is possible to provide an absorption type refrigerating device with good movability.
Becomes

Further, since the dilute solution La is branched into n pieces, for example, compared with the case where the entire amount of the dilute solution La directly flows into the regenerator G _n at the highest temperature side, the regeneration at the highest temperature side is performed. The inflow into the vessel G _n will be reduced. As a result, in the regenerator G _n of the highest temperature side, wherein the amount of absorption solution to be heated to boiling less amount corresponding its sensible heat is reduced, also the more outermost required for heating the hot side of the regenerator G _n Since the amount of heat (that is, the amount of heat input to the regenerator G _n ) is also reduced, the coefficient of performance (COP) of the entire system is improved and the efficiency of the absorption refrigeration system is improved. further,
In the solution heat exchanger H _n just before the regenerator G _n on the highest temperature side, the heat transfer area can be made smaller by the amount of the absorbed solution flowing into the solution heat exchanger H _n , and can be made compact. As a result, it can contribute to downsizing of the absorption refrigeration system.

(6) According to the absorption type refrigeration system of the sixth invention of the present application, the above (1), (2), (3),
In addition to the effects described in (4) or (5), the following unique effects can be obtained. That is, in the absorption refrigerating apparatus of the present invention, the concentrated solution L _n from the regenerator G _n on the highest temperature side branches after passing through the heating side of the solution heat exchanger H _n , and a part of the solution on the low temperature side. since the construction of such flows further into the regenerator G _n-2 on the low temperature side with concentrated solution L _n-1 from the regenerator G _n-1, and eventually, the highest temperature side regenerator G _n Concentrated solution L _n from the regenerator G _n-2 on the lower temperature side
_Since a part of the concentrated solution L _n is caused to flow into the regenerator G _n-2 before the confluence with the _n-2 , the pressure adjustment at the confluence of the concentrated solutions L _n and L _n-1 becomes easy, and the solution Can be smoothly joined.

(7) According to the absorption refrigeration system of the seventh invention of the present application, the above (1), (2), (3),
In addition to the effects described in (4) or (5), the following unique effects can be obtained. That is, in the absorption refrigeration apparatus of the present invention, the concentrated solution L _n-1 from the low temperature side regenerator G _n-1 is branched after passing through the heating side of the solution heat exchanger H _n-1. A part of the regenerator on the low temperature side is configured to flow out from the regenerator G _n on the highest temperature side and join the concentrated solution L _n after passing through the heating side of the solution heat exchanger H _n . The concentrated solution L _n-1 from G _n-1 is branched, and a part of the concentrated solution L _n-1 flows out from the regenerator G _n on the highest temperature side and passes through the heating side of the solution heat exchanger H _n , and then the concentrated solution L _n. By merging with the regenerator G _n-2 , the amount of concentrated solution flowing into the regenerator G _n-2 on the lower temperature side is further reduced.
_The amount of heat required for regeneration at _n-2 (in other words, evaporation of the refrigerant vapor) will be small. Therefore, the regenerator G _n-2
The thermal efficiency in will be improved.

(8) According to the absorption refrigerating apparatus of the eighth invention of the present application, the above (1), (2), (3),
In addition to the effects described in (4), (5), (6) or (7), the following unique effects can be obtained. That is, the absorption type refrigerating apparatus of the present invention, to heat the circulation path of the highest temperature side of the regenerator the absorbent solution in the residual heat Q after heating the regenerator G _n of the external heat source J for heating the G _n Therefore, the heat input of the external heat source J can be suppressed by preheating the absorbing solution by effectively using the residual heat Q.
Furthermore, further improvement in COP of the entire system can be expected.

(9) According to the absorption refrigeration system of the ninth invention of the present application, in addition to the effect described in the above (8), the following unique effect is obtained. That is, in the absorption refrigeration system of the present invention, the residual heat Q causes the absorber A
From the outlet of the regenerators G _{n to} G _{1 to} the absorption solution inlet of the regenerators G _{n to} G ₁ or the absorption solution immediately before the absorption solution inlet of the regenerators G _{n to} G ₁ or the highest temperature side Regenerator G
_Since the absorption solution immediately before the absorption solution inlet of _n is heated, the absorption solution in the path from the outlet of the absorber A to the absorption solution inlet of each of the regenerators G _{n to} G ₁ is heated. In the case of such a configuration, since the degree of freedom in selecting the heating position is large, the piping design of the residual heat is easy, and the absorbing solution immediately before the absorbing solution inlet of each of the regenerators G _{n to} G ₁ is heated. In such a case, the preheated absorption solution flows into each of the regenerators G _{n to} G ₁ in a state where the heat radiation thereof is small (in other words, in a state where a higher temperature is maintained), so that the preheating effect is high and the thermal efficiency is high. Further improvement can be expected, and when the absorption solution immediately before the absorption solution inlet of the regenerator G _n on the highest temperature side is heated, the heat input amount of the external heat source J can be reduced by the amount of preheat. Can be expected to further improve COP A.

(10) According to the absorption type refrigerating apparatus of the tenth invention of the present application, in addition to the effects described in the above (8) or (9), the following unique effects can be obtained. That is,
In the absorption refrigeration system of the present invention, the residual heat pipe 50 for the residual heat Q is branched into two or more residual heat branch pipes 51 and 52, and the absorption solution is heated in each of the residual heat branch pipes 51 and 52. Since it is configured to be performed, the heat with the high residual heat Q can be distributed to the absorbing solution, and the preheating effect on the absorbing solution is promoted.

(11) According to the absorption refrigeration system of the eleventh invention of the present application, the above (8), (9) or (1)
In addition to the effect described in 0), the following unique effect is obtained. That is, in the absorption refrigerating apparatus of the present invention, the residual heat Q is used to heat the absorbing solution in multiple stages, that is, in series in the flow direction of the residual heat Q, so that heat is mutually exchanged. The temperature difference between the absorbing solution and the residual heat Q is equalized as much as possible at each heating position, the heat recovery efficiency of the entire system is improved, and further improvement of the thermal efficiency of the absorption refrigeration system can be expected. .

(12) According to the absorption type refrigeration system of the twelfth invention of the present application, the above (8), (9) and (10) are provided.
Alternatively, in addition to the effect described in (11), the following unique effect can be obtained. That is, in the absorption refrigeration system of the present invention,
The diluted solution pipe 23 from the absorber A is connected to the diluted solution pipe 23.
The branch pipe 48 bypassing the solution heat exchanger H _N (N = 1 to n) provided in the above is provided, and the absorption solution is heated by the residual heat Q in the branch pipe 48. Since the amount of the absorbing solution heated by the residual heat Q is small, the absorbing solution can be efficiently preheated.

(13) According to the absorption type refrigeration system of the thirteenth invention of the present application, the above (1), (2), (3),
(4), (5), (6), (7), (8), (9),
In addition to the effects described in (10), (11) or (12), the following unique effects can be obtained. That is, the absorption type refrigerating apparatus according to the present invention, since the arrangement to heat the absorption solution by steam drain Dr _n-1 ~Dr ₁ produced in the above regenerator G _n-1 ~G _1, the steam Drain Dr _n-1 ~ Dr ₁
It is possible to effectively utilize the heat held by the above to preheat the absorbing solution and reduce the heat load on each of the regenerators G _{n-1 to} G ₁ to further promote the thermal efficiency of the entire system.

(14) According to the absorption type refrigerating apparatus of the fourteenth invention of the present application, in addition to the effect described in the above (13), the following unique effect can be obtained. That is, in the absorption refrigerating apparatus of the present invention, the vapor drains Dr _{n-1 to} Dr ₁ generated in the regenerators G _{n-1 to} G ₁ are combined to heat the absorption solution. So, the combined steam drain D
r _{n-1 to} Dr ₁ have a larger amount of heat, and the large amount of heat can efficiently preheat the absorbing solution.

(15) According to the absorption refrigeration system of the fifteenth invention of the present application, in addition to the effect described in the above (13) or (14), the following unique effect is obtained. That is, in the absorption refrigeration system of the present invention, the vapor drain D
by r _n-1 ~Dr _1, the absorption solution path to absorbent solution inlet outlet from each regenerator G _n-1 ~G ₁ of the absorber A, or each regenerator G _n-1 ~G _Since the absorbent solution immediately before the inlet of the absorbent solution ₁ is heated, the absorbent solution in the path from the outlet of the absorber A to the absorbent solution inlets of the regenerators G _{n-1 to} G ₁ In the case of a configuration in which the heating is performed, the steam drain piping design is easy because the degree of freedom in selecting the heating position is large, and the absorption solution immediately before the absorption solution inlet of each of the regenerators G _{n-1 to} G ₁ is In the case of heating the regenerator G, the preheated absorption solution emits less heat (in other words, maintains a higher temperature).
further improvement in preheating effect is high thermal efficiency since it flows into the _n-1 ~G ₁ can be expected.

(16) According to the absorption type refrigeration system of the sixteenth invention of the present application, in addition to the effect described in the above (13), (14) or (15), the following unique effect is obtained. To be That is, in the absorption type refrigerating apparatus of the present invention, the vapor drains Dr _{n-1 to} Dr ₁ are branched into two or more parts, and the absorption solution is heated in each of the branch paths 34 and 36. Therefore, the above steam drain D
The heating of the absorbing solution by r _{n-1 to} Dr ₁ can be distributed with high heat, and the preheating effect on the absorbing solution is promoted.

(17) According to the absorption type refrigeration system of the seventeenth invention of the present application, the above (13), (14), (1)
In addition to the effect described in 5) or (16), the following unique effect is obtained. That is, in the absorption refrigerating apparatus of the present invention, since the arrangement to perform the heating of the absorption solution by the steam drain Dr _n-1 ~Dr ₁ in multiple stages, the absorption solution and steam drain of each other is a heat exchange The temperature difference from Dr _{n-1 to} Dr ₁ is equalized as much as possible at each heating position, the heat recovery efficiency of the entire system is improved, and the thermal efficiency of the absorption refrigeration system can be expected to be further improved. .

(18) According to the eighteenth invention of the present application,
(13), (14), (15), (16) or (1)
In addition to the effects described in 7), the following unique effects can be obtained. That is, in the absorption refrigerating apparatus of the present invention, the dilute solution pipe 23 from the absorber A is branched pipe 48 that bypasses the solution heat exchanger H _N (N = 1 to n) provided in the dilute solution pipe 23. the provided, since the absorption solution in the branch pipe 48 are configured to be heated by the steam drain Dr _n-1 ~Dr _1, absorption is heated by the heat possessed vapor drain Dr _n-1 ~Dr ₁ Since the amount of the solution is small, the absorption solution can be efficiently preheated.

(19) According to the absorption type refrigeration system of the nineteenth invention of the present application, the above (1), (2), (3),
(4), (5), (6), (7), (8), (9),
(10), (11), (12), (13), (14),
In addition to the effects described in (15), (16), (17) or (18), the following unique effects can be obtained. That is, in the absorption refrigeration system of the present invention, the absorber A and the evaporator E are divided into a plurality of stages having different refrigerant evaporation temperatures, or the regenerator G ₁ and the condenser C on the lowest temperature side are arranged at the refrigerant condensation temperature. Different from each other, or the absorber A and the evaporator E are divided into multiple stages having different refrigerant evaporation temperatures, and the regenerator G ₁ and the condenser C on the lowest temperature side have different refrigerant condensation temperatures. Since it is divided into stages, the entire cycle is shifted to the low concentration side, the operating pressure of the system decreases,
It is possible to provide an absorption type refrigeration system having good operability.

(20) According to the absorption type refrigeration system of the twentieth invention of the present application, the above (1), (2), (3),
(4), (5), (6), (7), (8), (9),
(10), (11), (12), (13), (14),
(15), (16), (17), (18) or (19)
In addition to the effects described in (1), the following unique effects can be obtained. That is, in the absorption refrigeration system of the present invention, the cooling water Wa that circulates the absorber A and the condenser C and cools them together is caused to flow from the condenser C side toward the absorber A side. Therefore, the cooling water Wa having a lower temperature is supplied to the condenser C as compared with the case where the cooling water Wa is flown from the absorber A side to the condenser C side. The cooling capacity in the condenser C is improved, and the operating pressure of the regenerator G ₁ on the lowest temperature side connected to the condenser C is reduced, and as a result, the operating pressure of the regenerator G ₁ on the lowest temperature side is reduced. The maximum operating pressure of the entire cycle that is dominated by
The operating pressure of the regenerator G _n on the highest temperature side is reduced, and an absorption type refrigerating device having more excellent operability can be provided.

(21) According to the absorption type refrigeration system of the eighteenth invention of the present application, the above (1), (2), (3),
(4), (5), (6), (7), (8), (9),
(10), (11), (12), (13), (14),
In addition to the effects described in (15), (16), (17), (18), (19) or (20), the following unique effects can be obtained. That is, in the absorption refrigerating apparatus of the present invention, the number n of installed regenerators and solution heat exchangers is n = 3, but the number of regenerators is increased to increase the number of concentration stages of the absorption solution to improve thermal efficiency. And the advantage of improving the performance of the absorption refrigeration system by increasing the number of solution heat exchangers and increasing the heat recovery rate, and the manufacturing cost by increasing the number of these regenerators and solution heat exchangers. In comparison with the demerit of increase of the above, by setting the number of regenerators and solution heat exchangers to 3 as in the present invention, it is possible to achieve both the performance side and the cost side of the absorption refrigeration system. It is extremely useful in practice.

[0055]

BEST MODE FOR CARRYING OUT THE INVENTION Preferred embodiments of the present invention will be specifically described below.

I: First Embodiment FIG. 1 shows an operation cycle of the absorption refrigerating apparatus Z _{1 according} to the first embodiment of the present invention. This absorption type refrigeration system Z ₁ is an absorption type refrigeration system which uses water as a refrigerant and lithium bromide as an absorption liquid, and includes one condenser C, one absorber A, one evaporator E, and three each. Solution heat exchangers H ₃ , H ₂ ,
H ₁ and the regenerators G ₃ , G ₂ and G ₁ are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E comprises a heat exchange part 7 for passing the liquid We to be cooled and a refrigerant sprayer 13 for spraying the refrigerant Re on the heat exchange part 7 in the container 1.

In the above-mentioned absorber A, the container 2 is filled with a concentrated solution Lg.
And a heat exchange section 8 for removing absorption heat generated in the absorber A. The condenser C is configured by including the heat exchange section 11 in the container 6.

Each of the regenerators G ₃ , G ₂ , and G ₁ is for heating and concentrating the absorption solution containing the refrigerant to obtain a concentrated solution having a high concentration in sequence. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium-temperature regenerator G ₂ that operates at a medium temperature and is configured to have an external heat source J (for example, combustion gas or steam) inside the container 3 (the “low-temperature side regenerator G _n in the claims”). _-1 "
Applicable) to is configured with a solution heating unit 9 in the container 4, corresponding to the even most low temperature regenerator G ₁ ( "lowest temperature side of the regenerator G _1" in the claims which operates at a low temperature )
Is provided with a solution heating unit 10 in the container 5.

Each of the solution heat exchangers H ₁ , H ₂ , and H ₃ has a low-temperature concentrated solution L ₁ produced by each of the regenerators G ₁ , G ₂ , and G ₃ .
This is for recovering the heat of each of the medium-temperature concentrated solution L ₂ and the high-temperature concentrated solution L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types For example, it may be configured by a plate heat exchanger.

Each of these devices is operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the container 6 of the condenser C and the container 1 of the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30. It is supplied to the evaporator E side. Further, the liquid refrigerant Rc supplied to the evaporator E is the refrigerant pump RP.
Is pumped up to the refrigerant sprayer 13 through the liquid refrigerant pipe 29, and is sprayed as the refrigerant Re from the refrigerant sprayer 13 to the heat exchange section 7 side.

The cooling water Wa flowing from the cooling liquid inlet pipe 41 into the heat exchanging portion 8 is introduced to the inlet side of the heat exchanging portion 11 through the cooling water pipe 42 connected to the outlet side of the heat exchanging portion 8. It is guided and flows out from the cooling water outlet pipe 43. After absorbing heat of absorption in the heat exchange section 8, the refrigerant vapor R ₁ transferred from the low temperature regenerator G ₁ in the heat exchange section 11 is cooled and condensed. Let

From the cooled liquid inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We that flows in to and flows out from the liquid to be cooled outlet pipe 46 is cooled by the heat of vaporization of the refrigerant Re. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

A dilute solution pipe 21 equipped with a solution pump LP is connected to the bottom of the container 2 of the absorber A.
After passing through the heated side of the low temperature solution heat exchanger H ₁ , the dilute solution pipe 21 is branched into two paths, a first branch pipe 22 and a second branch pipe 23. The first branch pipe 22 is connected to the high temperature regenerator G ₃ through the heated side of the high temperature solution heat exchanger H ₃ . The second branch pipe 23 is connected to the medium temperature regenerator G ₂ through the heated side of the medium temperature solution heat exchanger H ₂ . Therefore, the dilute solution La flowing out of the absorber A branches after passing through the heated side of the low temperature solution heat exchanger H ₁ , and _one of them branches through the high temperature solution heat exchanger H ₃ to the high temperature regenerator. It flows into G ₃ , and the other flows into the intermediate temperature regenerator G ₂ via the intermediate temperature solution heat exchanger H ₂ .

The medium temperature solution pipe 26, which is connected to the medium temperature regenerator G ₂ and guides the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G ₂ , passes through the heating side of the medium temperature solution heat exchanger H _2. It is connected to the low temperature regenerator G ₁ .

High temperature regenerator G₃Connected to the high temperature re
Organ G₃High temperature concentrated solution L flowing out from₃The above high temperature melting
Liquid heat exchanger H₃High temperature solution pipe 27 passing through the heating side of
Low temperature regenerator G₁Connected to the low temperature regenerator G₁Spilled from
Low temperature concentrated solution L₁The low temperature solution pipe 25 that guides
To become the concentrated solution pipe 24, and the low temperature solution heat exchanger H ₁
To the solution sprayer 12 through the heating side of the.

The air chamber side of the high temperature regenerator G ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The solution heating section 10 of the low temperature regenerator G ₁
The outlet side of the condenser is connected to the condenser C via a refrigerant drain pipe 35.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is joined to the refrigerant drain pipe 35.

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The absorption refrigeration system Z ₁ constitutes a circulation cycle of the refrigerant and the absorption solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₁ will be specifically described with reference to FIGS. 1 and 2.

The diluted solution La (concentration ξa) fed from the absorber A by the solution pump LP passes through the heated side of the low temperature solution heat exchanger H ₁ and is branched.
One of them flows into the high-temperature regenerator G ₃ through the heated side of the high-temperature solution heat exchanger H ₃ and is subjected to the heating and concentrating action by the external heat source J in the high-temperature regenerator G _{3 so} that the concentration ξ ₃
Of high temperature concentrated solution L ₃ and flows out, and passes through the heating side of the high temperature solution heat exchanger H ₃ . At this time, in the high temperature solution heat exchanger H ₃ , heat exchange is performed between the diluted solution La on the heated side and the high temperature concentrated solution L ₃ on the heating side (heat recovery), and the diluted solution La is preheated. In this state, it flows into the high temperature regenerator G ₃ side.

[0076] On the other hand, the branched other dilute solution La is passed through the heated side of the medium-temperature solution heat exchanger H _2, flows into the intermediate temperature regenerator G _2, the high temperature in the middle temperature regenerator G ₂ Refrigerant vapor R ₃ flowing into the solution heating unit 9 from the container G ₃ side
The solution is heated and concentrated by the solution, becomes a medium-temperature concentrated solution L ₂ having a concentration of ξ ₂ , flows out, and flows into the low-temperature regenerator G ₁ through the heating side of the medium-temperature solution heat exchanger H ₂ . At this time, in the medium temperature solution heat exchanger H ₂ , heat exchange is performed between the dilute solution La on the heated side and the medium temperature concentrated solution L ₂ on the heating side (heat recovery),
The diluted solution La flows into the medium temperature regenerator G ₂ side in a preheated state.

Further, the medium temperature concentrated solution L ₂ flowing into the low temperature regenerator G ₁ is a refrigerant vapor R ₂ flowing into the solution heating section 10 from the medium temperature regenerator G ₂ side in the low temperature regenerator G ₁ .
It is heated and concentrated by and is discharged as a low temperature concentrated solution L ₁ having a concentration ξ ₁ .

The low temperature concentrated solution L ₁ having the concentration ξ ₁ flowing out from the low temperature regenerator G ₁ joins with the high temperature concentrated solution L ₃ having the concentration ξ ₃ flowing out from the high temperature regenerator G ₃ side to form the concentration ξ 1. _It becomes a concentrated solution Lg of _m , passes through the heating side of the low temperature solution heat exchanger H ₁ and flows into the absorber A side, where it is sprayed by the solution sprayer 12. At this time, in the low temperature solution heat exchanger H ₁ , heat is exchanged between the diluted solution La on the heated side and the concentrated solution Lg having the concentration ξ _m on the heating side (heat recovery), and the diluted solution La is In the preheated state, they branch into the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ , respectively.

The above is the absorption refrigerating apparatus Z _{1 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

Absorption refrigeration equipment according to the first embodiment
Setting Z₁In, the diluted solution La discharged from the absorber A is
The high temperature regenerator is branched and
G₃To the middle temperature regenerator.
G₂Flow into the low temperature regenerator G₁Flowed into
The medium temperature regenerator G is constructed as described above.₂To
In this case, the unconcentrated dilute solution La may flow in as it is.
And, for example, the high temperature regenerator G₃Absorbed by heating at
Compared with the case where a solution (concentrated solution) is flowed in,
The lower the concentration, the lower the boiling temperature. This
Medium temperature regenerator G ₂Of the boiling temperature of the absorbing solution in water
Only, the high temperature regenerator G that serves as its heating source₃Cold in
Since the temperature of the medium vapor can be set low,
The high temperature regenerator G proportional to the temperature of the medium vapor₃The operating pressure of
Can be set lower, which results in lower operating pressure.
It is possible to provide an absorption type refrigerating device with good movability.
Becomes

Further, since the dilute solution La from the absorber A is branched and a part of the dilute solution La is caused to flow into the high temperature regenerator G ₃ , for example, the entire amount of the dilute solution La is directly kept in the high temperature regenerator G. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system Z ₁ is improved.

[0082] Further, the absorber part thereof is branched dilute solution La from A by which so as to flow into the high-temperature regenerator G _3, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution L flowing in here is supplied.
As the amount of a decreases, the heat transfer area can be reduced to make the device compact, which in turn contributes to making the absorption refrigeration system Z ₁ compact.

Further, the absorption refrigerating apparatus Z _{1 of} this embodiment
In this case, since the diluted solution La discharged from the absorber A is branched after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ is passed through the high temperature solution heat exchanger H ₃ immediately before it. And the dilute solution La flowing into the medium temperature regenerator G ₂ via the medium temperature solution heat exchanger H ₂ immediately before it.
Means that both flow into the low temperature solution heat exchanger H ₁ in a preheated state, and as a result, the required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ decreases. It can be expected that the thermal efficiency of the entire system will be improved.

Further, the absorption type refrigerating apparatus Z of this embodiment.
_{In 1} , the system is configured with _three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ ; By increasing the number of concentration stages of the absorption solution to increase the thermal efficiency, and increasing the number of solution heat exchangers to increase the heat recovery rate, the merit of improving the performance of the absorption refrigeration system and the regenerator In comparison with the disadvantage that the manufacturing cost increases due to the increase in the number of solution heat exchangers, the absorption refrigeration system Z ₁
It is considered to be optimal for achieving both performance and cost, and is extremely useful in practice.

II: Second Embodiment FIG. 3 shows an operation cycle of an absorption refrigeration system Z _{2 according to} a second embodiment of the present invention. This absorption type refrigeration system Z ₂ is an absorption type refrigeration system which uses water as a refrigerant and lithium bromide as an absorption liquid, and includes one condenser C, an absorber A, an evaporator E, and three each. Solution heat exchangers H ₃ , H ₂ ,
H ₁ and the regenerators G ₃ , G ₂ and G ₁ are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E is provided with a heat exchange part 7 for passing the liquid We to be cooled and a refrigerant sprayer 13 for spraying the refrigerant Re on the heat exchange part 7 in the container 1.

In the above-mentioned absorber A, the container 2 is filled with the concentrated solution Lg.
And a heat exchange section 8 for removing absorption heat generated in the absorber A. The condenser C is configured by including the heat exchange section 11 in the container 6.

Each of the regenerators G ₃ , G ₂ , and G ₁ is for heating and concentrating the absorbing solution containing the refrigerant to obtain a concentrated solution having a high concentration in sequence. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium-temperature regenerator G ₂ that operates at a medium temperature and is configured to have an external heat source J (for example, combustion gas or steam) inside the container 3 (the “low-temperature side regenerator G _n in the claims”). _-1 "
Applicable) to is configured with a solution heating unit 9 in the container 4, corresponding to the even most low temperature regenerator G ₁ ( "lowest temperature side of the regenerator G _1" in the claims which operates at a low temperature )
Is provided with a solution heating unit 10 in the container 5.

Each of the heat exchangers H ₁ , H ₂ , and H ₃ has a low-temperature concentrated solution L ₁ , a medium-temperature concentrated solution L ₂ , and a high-temperature concentrated solution produced by the regenerators G ₁ , G ₂ , and G _3. It is for recovering the heat of each L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types,
For example, it is composed of a plate heat exchanger.

Each of these devices is operatively connected by a solution piping system and a refrigerant piping system as follows.

That is, the container 6 of the condenser C and the container 1 of the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30. It is supplied to the evaporator E side. Further, the liquid refrigerant Rc supplied to the evaporator E is the refrigerant pump RP.
Is pumped up to the refrigerant sprayer 13 through the liquid refrigerant pipe 29, and is sprayed as the refrigerant Re from the refrigerant sprayer 13 to the heat exchange section 7 side.

The cooling water Wa flowing from the cooling liquid inlet pipe 41 into the heat exchanging portion 8 is introduced to the inlet side of the heat exchanging portion 11 via the cooling water pipe 42 connected to the outlet side of the heat exchanging portion 8. It is guided and flows out from the cooling water outlet pipe 43. After absorbing heat of absorption in the heat exchange section 8, the refrigerant vapor R ₁ transferred from the low temperature regenerator G ₁ in the heat exchange section 11 is cooled and condensed. Let

From the cooled liquid inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We that flows in to and flows out from the liquid to be cooled outlet pipe 46 is cooled by the heat of vaporization of the refrigerant Re. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

A dilute solution pipe 21 equipped with a solution pump LP is connected to the bottom of the container 2 of the absorber A.
After passing through the heated side of the low temperature solution heat exchanger H ₁ , the dilute solution pipe 21 is branched into two paths, a first branch pipe 22 and a second branch pipe 23. The first branch pipe 22 is connected to the high temperature regenerator G ₃ through the heated side of the high temperature solution heat exchanger H ₃ .

Further, the second branch pipe 23 is a medium temperature solution.
Heat exchanger H₂Through the heated side of the medium temperature regenerator G₂Contact
And the medium temperature solution heat exchanger H₂Just before
Further, it is branched to the branch pipe 28. And this
The branch pipe 28 of the medium temperature regenerator G₂Out of the above
Hot solution heat exchanger H₂Through the heating side of the low temperature regenerator G ₁
The medium temperature solution heat exchanger H of the medium temperature solution pipe 26 connected to
₂It is connected to the downstream side position.

Therefore, the dilute solution flowing out of the absorber A is
La is the low temperature solution heat exchanger H₁After passing through the heated side of
To the high temperature solution heat exchanger H.₃Through
High temperature regenerator G above₃While flowing into the other
Solution heat exchanger H₂Branch immediately before
Branching solution La₁Is the above medium temperature solution heat exchanger H₂The heated side of
Through the above medium temperature regenerator G₂Into the other re-branching solution
La₂Is the above medium temperature regenerator G ₂Out of the medium temperature heat exchange
Bowl H₂Medium temperature concentrated solution L after passing through the heating side of₂Merge with the above
Low temperature regenerator G₁Will flow into.

High temperature regenerator G₃Connected to the high temperature re
Organ G₃High temperature concentrated solution L flowing out from₃The above high temperature melting
Liquid heat exchanger H₃High temperature solution pipe 27 passing through the heating side of
Low temperature regenerator G₁Connected to the low temperature regenerator G₁Spilled from
Low temperature concentrated solution L₁The low temperature solution pipe 25 that guides
To become the concentrated solution pipe 24, and the low temperature solution heat exchanger H ₁
To the solution sprayer 12 through the heating side of the.

The air chamber side of the high temperature regenerator G ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The solution heating section 10 of the low temperature regenerator G ₁
The outlet side of the condenser is connected to the condenser C via a refrigerant drain pipe 35.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is joined to the refrigerant drain pipe 35.

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The absorption refrigeration system Z ₂ constitutes a circulation cycle of the refrigerant and the absorption solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₂ will be specifically described with reference to FIGS. 3 and 4.

The dilute solution La (concentration ξa) fed from the absorber A by the solution pump LP passes through the heated side of the low temperature solution heat exchanger H ₁ and is branched.
One of them flows into the high-temperature regenerator G ₃ through the heated side of the high-temperature solution heat exchanger H ₃ and is subjected to the heating and concentrating action by the external heat source J in the high-temperature regenerator G _{3 so} that the concentration ξ ₃
Of high temperature concentrated solution L ₃ and flows out, and passes through the heating side of the high temperature solution heat exchanger H ₃ . At this time, in the high temperature solution heat exchanger H ₃ , heat exchange is performed between the diluted solution La on the heated side and the high temperature concentrated solution L ₃ on the heating side (heat recovery), and the diluted solution La is preheated. In this state, it flows into the high temperature regenerator G ₃ side.

On the other hand, the other branched dilute solution La is re-distributed.
One of the re-branching solutions La ₁Is the above medium temperature solution
Heat exchanger H₂After passing through the heated side of the₂To
Inflow, the medium temperature regenerator G₂In the above high temperature regenerator G₃~ side
Refrigerant vapor R flowing from the above into the solution heating unit 9₃By
Heat concentrated, concentration ξ₂Medium temperature concentrated solution L₂Became outflow
The above medium temperature solution heat exchanger H₂Flows out through the heated side of
It And this medium temperature solution heat exchanger H₂Medium temperature after passing through
Concentrated solution L₂Is the other re-branching solution La₂Join up with
Low temperature regenerator G₁Flow into. At this time, the medium temperature solution heat
Exchanger H₂In the re-branching solution La on the heated side₁And heating
Medium temperature concentrated solution L₂Heat is exchanged between
), The dilute solution La is preheated, and the medium temperature regenerator is used.
G₂Flows into the side. Furthermore, the low temperature regenerator G₁Flowing into
Concentrated solution (medium temperature concentrated solution L₂And re-branching dilute solution La₂Mixed with
Combined solution) is the low temperature regenerator G₁At the above medium temperature regenerator
G₂Refrigerant vapor R flowing into the solution heating unit 10 from the side₂To
Therefore, it is heated and concentrated, and the concentration ξ₁Low temperature concentrated solution L₁Become
leak.

The low temperature concentrated solution L ₁ having a concentration ξ ₁ flowing out from the low temperature regenerator G ₁ joins with the high temperature concentrated solution L ₃ having a concentration ξ ₃ flowing out from the high temperature regenerator G ₃ side to form a concentration ξ 1. _It becomes a concentrated solution Lg of _m , passes through the heating side of the low temperature solution heat exchanger H ₁ and flows into the absorber A side, where it is sprayed by the solution sprayer 12. At this time, in the low temperature solution heat exchanger H ₁ , heat exchange is performed between the diluted solution La on the heated side and the concentrated solution Lg having the concentration ξ _m on the heating side.

The above is the absorption refrigerating apparatus Z _{2 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

In the absorption refrigeration system Z _{2 according} to the second embodiment, the diluted solution La branched after passing through the low temperature solution heat exchanger H ₁ is further converted into the medium temperature solution heat exchanger H.
Re-branching immediately before ₂ , and one of the re-branching solutions L
a ₁ After allowed to flow into the intermediate temperature regenerator G ₂ through the medium-temperature solution heat exchanger H _2, and it is combined with other re-branch solution La ₂ was configured to flow into the low temperature regenerator G ₁ There is.

[0110] Therefore, in the medium-temperature solution heat exchanger H ₂ side, the middle temperature solution heat exchanger H ₂ re branch solution La ₁
Since only the inflow is made, for example, as compared with the case where the whole amount of the dilute solution La branched after passing through the low temperature solution heat exchanger H ₁ is directly flown into the medium temperature solution heat exchanger H ₂ without being re-branched, becomes the flow rate decreases in the intermediate temperature solution heat exchanger H _2, can be made compact of the medium-temperature solution heat exchanger H ₂ corresponds to the flow rate reduction.

On the other hand, in the medium temperature regenerator G ₂ , since the unconcentrated re-branching solution La ₁ flows in as it is, for example, the absorption solution (concentrated solution) which is heated and concentrated in the high temperature regenerator G _3. The concentration of the absorbing solution is lower and the boiling temperature thereof is lower as compared with the case of flowing in.
Decrement the boiling temperature of the absorbent solution at the intermediate temperature regenerator G ₂ alone, since it can be set low refrigerant vapor temperature in the high temperature generator G ₃ to be the heat source, the high temperature is proportional to the refrigerant vapor temperature The operating pressure of the regenerator G ₃ can also be set low, and as a result, it is possible to provide an absorption type refrigeration system having a low operating pressure and good operability.

Further, since the dilute solution La from the absorber A is branched so that a part of the dilute solution La flows into the high temperature regenerator G ₃ , for example, the entire amount of the dilute solution La remains unchanged. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system Z ₂ is improved.

[0113] Further, the absorber part thereof is branched dilute solution La from A by which so as to flow into the high-temperature regenerator G _3, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution L flowing in here is supplied.
As the amount of a decreases, the heat transfer area can be reduced to make the device compact, which in turn contributes to making the absorption refrigerating device Z ₂ compact.

The absorption refrigerating apparatus Z _{2 of} this embodiment is also used.
In this case, since the diluted solution La discharged from the absorber A is branched after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ is passed through the high temperature solution heat exchanger H ₃ immediately before it. And the re-branched solution La ₁ that re-branches into the medium temperature regenerator G ₂ immediately before the medium temperature solution heat exchanger H ₂ and flows in via the medium temperature solution heat exchanger H ₂ . Both of them flow into the low temperature solution heat exchanger H ₁ in a preheated state, and as a result, the required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ is reduced, and the entire system is reduced. It can be expected to improve the thermal efficiency.

The absorption refrigerating apparatus Z _{2 of} this embodiment is also used.
Then, the system is configured by _three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ , but such a configuration requires a large number of regenerators. To increase the efficiency of the absorption solution by increasing the number of concentration stages of the absorption solution, and to increase the number of solution heat exchangers to increase the heat recovery rate, and the merit of improving the performance of the absorption refrigeration system, and the regenerator and When weighed against the disadvantage of increasing the manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. is there.

III: Third Embodiment FIG. 5 shows an operation cycle of an absorption refrigeration system Z _{3 according to} a third embodiment of the present invention. The absorption type refrigerating apparatus Z ₃ is an absorption type refrigerating apparatus which uses water as a refrigerant and lithium bromide as an absorbing liquid, and includes one condenser C, an absorber A, an evaporator E, and three pieces each. Solution heat exchangers H ₃ , H ₂ ,
H ₁ and the regenerators G ₃ , G ₂ and G ₁ are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E comprises a container 1 having a heat exchange section 7 for passing the liquid We to be cooled and a refrigerant sprayer 13 for spraying the refrigerant Re on the heat exchange section 7.

The absorber A has a container 2 in which the concentrated solution Lg
And a heat exchange section 8 for removing absorption heat generated in the absorber A. The condenser C is configured by including the heat exchange section 11 in the container 6.

Each of the regenerators G ₃ , G ₂ and G ₁ is for heating and concentrating the absorbing solution containing the refrigerant to obtain a concentrated solution having a high concentration in sequence. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium-temperature regenerator G ₂ that operates at a medium temperature and is configured to have an external heat source J (for example, combustion gas or steam) inside the container 3 (the “low-temperature side regenerator G _n in the claims”). _-1 "
Applicable) to is configured with a solution heating unit 9 in the container 4, corresponding to the even most low temperature regenerator G ₁ ( "lowest temperature side of the regenerator G _1" in the claims which operates at a low temperature )
Is provided with a solution heating unit 10 in the container 5.

Each of the heat exchangers H ₁ , H ₂ , and H ₃ has a low-temperature concentrated solution L ₁ , a medium-temperature concentrated solution L ₂ , and a high-temperature concentrated solution produced by the regenerators G ₁ , G ₂ , and G _3. It is for recovering the heat of each of L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types,
For example, a plate heat exchanger may be used.

Each of these devices is operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the container 6 of the condenser C and the container 1 of the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30. It is supplied to the evaporator E side. Further, the liquid refrigerant Rc supplied to the evaporator E is the refrigerant pump RP.
Is pumped up to the refrigerant sprayer 13 through the liquid refrigerant pipe 29, and is sprayed as the refrigerant Re from the refrigerant sprayer 13 to the heat exchange section 7 side.

The cooling water Wa flowing from the cooling liquid inlet pipe 41 into the heat exchanging portion 8 is introduced to the inlet side of the heat exchanging portion 11 via the cooling water pipe 42 connected to the outlet side of the heat exchanging portion 8. It is guided and flows out from the cooling water outlet pipe 43. After absorbing heat of absorption in the heat exchange section 8, the refrigerant vapor R ₁ transferred from the low temperature regenerator G ₁ in the heat exchange section 11 is cooled and condensed. Let

From the liquid to be cooled inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We that flows in to and flows out from the liquid to be cooled outlet pipe 46 is cooled by the heat of vaporization of the refrigerant Re. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

A dilute solution pipe 21 having a solution pump LP is connected to the bottom of the container 2 of the absorber A.
The dilute solution pipe 21 is branched into two paths of a first branch pipe 22 and a second branch pipe 23 immediately before the low temperature solution heat exchanger H ₁ . Then, the first branch pipe 22
Is connected to the high temperature regenerator G ₃ through the heated side of the high temperature solution heat exchanger H ₃ . The second branch pipe 23 is connected to the medium temperature regenerator G ₂ through the heated side of the low temperature solution heat exchanger H _{1 and} the heated side of the medium temperature solution heat exchanger H ₂ in order. There is. Therefore, the absorber A
The diluted solution La flowing out from the low temperature solution heat exchanger H _{1 is}
Immediately before, one of which branches above the high temperature solution heat exchanger H ₃
It flows into the high-temperature regenerator G ₃ via the other will be flowing into the intermediate temperature regenerator G ₂ through the low-temperature solution heat exchanger H ₁ and the medium-temperature solution heat exchanger H ₂ and respectively.

The medium temperature solution pipe 26, which is connected to the medium temperature regenerator G ₂ and guides the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G ₂ , passes through the heating side of the medium temperature solution heat exchanger H _2. It is connected to the low temperature regenerator G ₁ .

[0127] connected to the bottom of the high-temperature regenerator G ₃ leads to a high temperature concentrated solution L ₃ exiting from the high temperature generator G _3, hot solution pipe through the heating side of the high-temperature solution heat exchanger H ₃ 27
If, leads to low temperature concentrated solution L ₁ which flows out is connected to the low temperature regenerator G ₁ from the cold regenerator G _1, the low-temperature solution pipe 25 through the heating side of the low-temperature solution heat exchanger H _1, merging Then, the concentrated solution pipe 24 is formed and is connected to the solution sprayer 12.

The air chamber side of the high temperature regenerator G ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The solution heating section 10 of the low temperature regenerator G ₁
The outlet side of the condenser is connected to the condenser C via a refrigerant drain pipe 35.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is joined to the refrigerant drain pipe 35.

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The absorption refrigerating apparatus Z ₃ constitutes a circulation cycle of the refrigerant and the absorption solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₃ will be specifically described with reference to FIGS. 5 and 6.

From the absorber A to the solution pump LP.
The diluted solution La (concentration ξa) sent by
Liquid heat exchanger H₁Branch just before
Liquid heat exchanger H₃High temperature regenerator G through the heated side of₃To
Inflow, the high temperature regenerator G₃In the above external heat source J
The concentration ξ₃High temperature concentrated solution L₃Becomes
Flow out, the high temperature solution heat exchanger H₃On the heated side of.
At this time, the high temperature solution heat exchanger H₃At the heated side
Diluted solution La and high temperature concentrated solution L on the heating side₃Heat exchange with
Is performed (heat recovery), and the diluted solution La is preheated.
High temperature regenerator G above ₃Flows into the side.

On the other hand, the other branched dilute solution La first passes through the heated side of the low temperature solution heat exchanger H ₁ , and
Further, after passing through the heated side of the medium temperature solution heat exchanger H ₂ , it flows into the medium temperature regenerator G ₂ . Then, it is heated and concentrated in the medium-temperature regenerator G ₂ from the high temperature generator G ₃ side by the refrigerant vapor R ₃ flowing into the solution heating unit 9,
The medium-temperature concentrated solution L ₂ having a concentration of ξ ₂ flows out, passes through the heating side of the medium-temperature solution heat exchanger H ₂ , and flows into the low-temperature regenerator G ₁ . At this time, in the medium temperature solution heat exchanger H ₂ , heat is exchanged between the dilute solution La on the heated side and the medium temperature concentrated solution L ₂ on the heating side (heat recovery), and the dilute solution La is preheated. In this state, it flows into the high temperature regenerator G ₃ side.

Further, the medium temperature concentrated solution L ₂ flowing into the low temperature regenerator G ₁ is a refrigerant vapor R ₂ flowing into the solution heating section 10 from the medium temperature regenerator G ₂ side in the low temperature regenerator G ₁ .
It is heated and concentrated by and is discharged as a low temperature concentrated solution L ₁ having a concentration ξ ₁ . Then, the low-temperature concentrated solution L ₁ concentrations xi] ₁ flowing from the low temperature regenerator G ₁ is the low-temperature solution heat exchanger H ₁
Of the high temperature regenerator G ₃ side and then merges with the high temperature concentrated solution L ₃ of concentration ξ ₃ to form a concentrated solution Lg of concentration ξ _m , which flows into the absorber A side. Then, the solution is sprayed by the solution sprayer 12.

At this time, in the low temperature solution heat exchanger H ₁ , heat is exchanged between the dilute solution La on the heated side and the concentrated solution Lg having the concentration ξ ₁ on the heating side.

The above is the absorption refrigerating apparatus Z _{3 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

Absorption-type refrigeration equipment according to the third embodiment
Setting Z₃In, the diluted solution La discharged from the absorber A is
The high temperature regenerator is branched and
G₃To the middle temperature regenerator.
G₂Flow into the low temperature regenerator G₁Flowed into
The medium temperature regenerator G is constructed as described above.₂To
In this case, the unconcentrated dilute solution La may flow in as it is.
And, for example, the high temperature regenerator G₃Absorbed by heating at
Compared with the case where a solution (concentrated solution) is flowed in,
The lower the concentration, the lower the boiling temperature. This
Medium temperature regenerator G ₂Of the boiling temperature of the absorbing solution in water
Only, the high temperature regenerator G that serves as its heating source₃Cold in
Since the temperature of the medium vapor can be set low,
The high temperature regenerator G proportional to the temperature of the medium vapor₃The operating pressure of
Can be set lower, which results in lower operating pressure.
It is possible to provide an absorption type refrigerating device with good movability.
Becomes

Further, since the dilute solution La from the absorber A is branched and a part of the dilute solution La is caused to flow into the high temperature regenerator G ₃ , for example, the entire amount of the dilute solution La is kept as it is. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system Z ₂ is improved.

Further, the absorption type refrigeration system Z of this embodiment.
_{In 3} , the dilute solution La discharged from the absorber A is branched just before the low temperature solution heat exchanger H ₁ , and _one of them is passed to the high temperature regenerator G ₃ via the high temperature solution heat exchanger H ₃ immediately before it. Since the other _one passes through the low temperature solution heat exchanger H ₁ and then flows into the intermediate temperature regenerator G ₂ via the intermediate temperature solution heat exchanger H ₂ immediately before it, for example, it is rare. as compared with the case where the total amount of the solution La passes through the low-temperature solution heat exchanger H _1, and decreases the flow rate of the low temperature solution heat exchanger H ₁ is correspondingly low temperature solution heat exchanger compactness of an H ₁ is promoted Therefore, it is expected that the absorption type refrigeration system Z ₃ can be made compact.

[0143] Further, the absorber part thereof is branched dilute solution La from A by which so as to flow into the high-temperature regenerator G _3, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution La flowing into this is supplied.
As a result, the heat transfer area can be reduced by the amount corresponding to the decrease in the amount, and the size can be made compact, which in turn can contribute to the size reduction of the absorption refrigeration system Z ₃ .

Furthermore, the absorption type refrigerating apparatus Z of this embodiment.
_{In 3} , the system is composed of three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ ; By increasing the number of concentration stages of the absorption solution to increase the thermal efficiency, and increasing the number of solution heat exchangers to increase the heat recovery rate, the merit of improving the performance of the absorption refrigeration system and the regenerator And, when weighed against the disadvantage of increased manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. Is.

IV: Fourth Embodiment FIG. 7 shows an operation cycle of an absorption refrigeration system Z _{4 according to} a fourth embodiment of the present invention. The absorption type refrigerating apparatus Z ₄ is an absorption type refrigerating apparatus which uses water as a refrigerant and lithium bromide as an absorbing liquid, and includes one condenser C, an absorber A, an evaporator E, and three each. Solution heat exchangers H ₃ , H ₂ ,
H ₁ and the regenerators G ₃ , G ₂ and G ₁ are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E has a heat exchange part 7 for passing the liquid We to be cooled and a refrigerant sprayer 13 for spraying the refrigerant Re on the heat exchange part 7 in the container 1.

The above-mentioned absorber A has a container 2 having a concentrated solution Lg
And a heat exchange section 8 for removing absorption heat generated in the absorber A. The condenser C is configured by including the heat exchange section 11 in the container 6.

Each of the regenerators G ₃ , G ₂ and G ₁ is for heating and concentrating the absorption solution containing the refrigerant to obtain a concentrated solution having a high concentration in sequence. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium-temperature regenerator G ₂ that operates at a medium temperature and is configured to have an external heat source J (for example, combustion gas or steam) inside the container 3 (the “low-temperature side regenerator G _n in the claims”). _-1 "
Applicable) to is configured with a solution heating unit 9 in the container 4, corresponding to the even most low temperature regenerator G ₁ ( "lowest temperature side of the regenerator G _1" in the claims which operates at a low temperature )
Is provided with a solution heating unit 10 in the container 5.

Each of the heat exchangers H ₁ , H ₂ , and H ₃ has a low-temperature concentrated solution L ₁ , a medium-temperature concentrated solution L ₂ , and a high-temperature concentrated solution produced by the above-mentioned regenerators G ₁ , G ₂ , and G _3. It is for recovering the heat of each of L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types,
For example, a plate heat exchanger may be used.

Each of these devices is operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the container 6 of the condenser C and the container 1 of the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30. It is supplied to the evaporator E side. Further, the liquid refrigerant Rc supplied to the evaporator E is the refrigerant pump RP.
Is pumped up to the refrigerant sprayer 13 through the liquid refrigerant pipe 29, and is sprayed as the refrigerant Re from the refrigerant sprayer 13 to the heat exchange section 7 side.

The cooling water Wa flowing from the cooling liquid inlet pipe 41 into the heat exchanging portion 8 is introduced to the inlet side of the heat exchanging portion 11 via the cooling water pipe 42 connected to the outlet side of the heat exchanging portion 8. It is guided and flows out from the cooling water outlet pipe 43. After absorbing heat of absorption in the heat exchange section 8, the refrigerant vapor R ₁ transferred from the low temperature regenerator G ₁ in the heat exchange section 11 is cooled and condensed. Let

From the liquid to be cooled inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We that flows in to and flows out from the liquid to be cooled outlet pipe 46 is cooled by the heat of vaporization of the refrigerant Re. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

A dilute solution pipe 21 having a solution pump LP is connected to the bottom of the container 2 of the absorber A.
The dilute solution pipe 21 is branched into two paths of a first branch pipe 22 and a second branch pipe 23 immediately before the low temperature solution heat exchanger H ₁ . Then, the first branch pipe 22
Is connected to the high temperature regenerator G ₃ through the heated side of the high temperature solution heat exchanger H ₃ .

On the other hand, the second branch pipe 23 is connected to the heated side of the low temperature solution heat exchanger H ₁ and the medium temperature solution heat exchanger H _{2 by} heating.
It is connected to the medium temperature regenerator G ₂ through the heated side of the medium and is further branched to a branch pipe 28 immediately before the medium temperature solution heat exchanger H ₂ . Then, the branch pipe 28 comes out of the medium temperature regenerator G ₂ and passes through the heating side of the medium temperature solution heat exchanger H ₂ and is connected to the low temperature regenerator G ₁ by the medium temperature solution heat of the medium temperature solution pipe 26. It is connected to a position downstream of the exchanger H ₂ .

Therefore, the dilute solution La flowing out from the absorber A branches just before the low temperature solution heat exchanger H ₁ , and _one of them branches through the high temperature solution heat exchanger H ₃ to the high temperature regenerator G. One of the re-branching solutions La ₁ flows into the medium temperature ₃ while the other passes through the heated side of the low temperature solution heat exchanger H _{1 and} is then re-branched immediately before the medium temperature solution heat exchanger H _2. The medium-temperature regenerator G ₂ flows into the medium-temperature regenerator G ₂ through the heated side of the solution heat exchanger H ₂ , and the other branching solution La ₂ flows out of the medium-temperature regenerator G ₂ and the heating side of the medium-temperature solution heat exchanger H ₂ . After being passed through, the medium temperature solution L ₂ joins and flows into the low temperature regenerator G ₁ .

[0157] connected to the bottom of the high-temperature regenerator G ₃ leads to a high temperature concentrated solution L ₃ exiting from the high temperature generator G _3, hot solution pipe through the heating side of the high-temperature solution heat exchanger H ₃ 27
If, leads to low temperature concentrated solution L ₁ which flows out is connected to the low temperature regenerator G ₁ from the cold regenerator G _1, the low-temperature solution pipe 25 through the heating side of the low-temperature solution heat exchanger H _1, merging Then, the concentrated solution pipe 24 is formed and is connected to the solution sprayer 12.

The air chamber side of the high temperature regenerator G ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The solution heating section 10 of the low temperature regenerator G ₁
The outlet side of the condenser is connected to the condenser C via a refrigerant drain pipe 35.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is joined to the refrigerant drain pipe 35.

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The absorption refrigeration system Z ₄ constitutes a circulation cycle of the refrigerant and the absorption solution by adopting the above-mentioned equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₄ will be specifically described with reference to FIGS. 7 and 8.

The dilute solution La (concentration ξa) fed from the absorber A by the solution pump LP passes through the heated side of the low temperature solution heat exchanger H ₁ and is branched.
One of them flows into the high-temperature regenerator G ₃ through the heated side of the high-temperature solution heat exchanger H ₃ and is subjected to the heating and concentrating action by the external heat source J in the high-temperature regenerator G _{3 so} that the concentration ξ ₃
Of high temperature concentrated solution L ₃ and flows out, and passes through the heating side of the high temperature solution heat exchanger H ₃ . At this time, in the high temperature solution heat exchanger H ₃ , heat exchange is performed between the diluted solution La on the heated side and the high temperature concentrated solution L ₃ on the heating side (heat recovery), and the diluted solution La is preheated. In this state, it flows into the high temperature regenerator G ₃ side.

On the other hand, the other branched dilute solution La, after passing through the heated side of the low temperature solution heat exchanger H ₁ , is re-branched just before the medium temperature solution heat exchanger H ₂ , and one of the re-branching is performed. The solution La ₁ passes through the heated side of the medium-temperature solution heat exchanger H ₂ and then flows into the medium-temperature regenerator G _2, and in the medium-temperature regenerator G ₂ , from the high-temperature regenerator G ₃ side to the solution heating section. 9 is heated and concentrated by the refrigerant vapor R ₃ flowing into the medium 9, and flows out as a medium-temperature concentrated solution L ₂ having a concentration of ξ _{2 and} the medium-temperature solution heat exchanger H ₂
Flows out through the heated side of. Then, the medium-temperature concentrated solution L _{2 that} has passed through the medium-temperature solution heat exchanger H ₂ merges with the other re-branching solution La ₂ and flows into the low-temperature regenerator G ₁ . At this time, in the medium temperature solution heat exchanger H ₂ , heat is exchanged between the re-branching solution La ₁ on the heated side and the medium temperature concentrated solution L ₂ on the heating side (heat recovery), and the dilute solution La It flows into the medium temperature regenerator G ₂ side in a preheated state.

Further, the concentrated solution flowing into the low temperature regenerator G ₁ (mixed solution of the medium temperature concentrated solution L ₂ and the re-branching solution La ₂ )
Is heated and concentrated in the low temperature regenerator G ₁ by the refrigerant vapor R ₂ flowing into the solution heating unit 10 from the medium temperature regenerator G ₂ side, and flows out as a low temperature concentrated solution L ₁ having a concentration ξ ₁ .

This low temperature regenerator G₁Outflow from
Concentration ξ₁Low temperature concentrated solution L₁Is the low temperature solution heat exchanger H₁
After passing through the heating side of the high temperature regenerator G₃Leaked from the side
Concentration ξ ₃High temperature concentrated solution L₃Confluence with the concentration ξ_mWith a concentrated solution of
And flows into the absorber A side, where the solution sprayer is
Sprayed by 12. At this time, the low temperature solution heat exchange
Bowl H₁In, the diluted solution La on the heated side and the concentration on the heating side
ξ₁Low temperature concentrated solution L₁A heat exchange is carried out between and.

The above is the absorption refrigerating apparatus Z _{4 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

In the absorption type refrigerating apparatus Z _{4 according} to the fourth embodiment, the diluted solution La branched after passing through the low temperature solution heat exchanger H ₁ is further converted into the medium temperature solution heat exchanger H.
Re-branching immediately before ₂ , and one of the re-branching solutions L
a ₁ After allowed to flow into the intermediate temperature regenerator G ₂ through the medium-temperature solution heat exchanger H _2, and it is combined with other re-branch solution La ₂ was configured to flow into the low temperature regenerator G ₁ There is.

[0171] Therefore, in the medium-temperature solution heat exchanger H ₂ side, the middle temperature solution heat exchanger H ₂ re branch solution La ₁
Since only the inflow is made, for example, as compared with the case where the whole amount of the dilute solution La branched after passing through the low temperature solution heat exchanger H ₁ is directly flown into the medium temperature solution heat exchanger H ₂ without being re-branched, becomes the flow rate decreases in the intermediate temperature solution heat exchanger H _2, can be made compact of the medium-temperature solution heat exchanger H ₂ corresponds to the flow rate reduction.

On the other hand, in the medium temperature regenerator G ₂ , since the unconcentrated re-branching solution La ₁ flows in as it is, for example, the absorbing solution (concentrated solution) which is heated and concentrated in the high temperature regenerator G _3. The concentration of the absorbing solution is lower and the boiling temperature thereof is lower as compared with the case of flowing in.
Decrement the boiling temperature of the absorbent solution at the intermediate temperature regenerator G ₂ alone, since it can be set low refrigerant vapor temperature in the high temperature generator G ₃ to be the heat source, the high temperature is proportional to the refrigerant vapor temperature The operating pressure of the regenerator G ₃ can also be set low, and as a result, it is possible to provide an absorption type refrigeration system having a low operating pressure and good operability.

Further, since the dilute solution La from the absorber A is branched so that a part of the dilute solution La flows into the high temperature regenerator G ₃ , for example, the entire amount of the dilute solution La remains unchanged. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ ) is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system Z ₄ is improved.

[0174] Further, the absorber part thereof is branched dilute solution La from A by which so as to flow into the high-temperature regenerator G _3, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution L flowing in here is supplied.
As the amount of a decreases, the heat transfer area can be reduced to make the device compact, which in turn contributes to making the absorption refrigeration system Z ₄ compact.

Further, the absorption type refrigeration system Z of this embodiment._Four
Then, the diluted solution La discharged from the absorber A is added to the low temperature solution.
Heat exchanger H₁Branch just before, one of the above
High temperature regenerator G₃Immediately before that, the high temperature solution heat exchanger H₃Through
And the other is the low temperature solution heat exchanger H.₁Pass through
After that, the above medium temperature regenerator G₂Immediately before that, the medium temperature solution heat exchanger
H ₂Since it is configured to flow in via
If the total amount of the dilute solution La is the low temperature solution heat exchanger H,₁Pass through
The low temperature solution heat exchanger H is₁Flow rate is reduced
Little, that much the low temperature solution heat exchanger H₁Downsizing
Is promoted, and by extension the absorption type refrigeration system Z_FourCompact
Can be expected.

Further, the absorption type refrigerating apparatus Z _{4 of} this embodiment
Then, the system is configured by _three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ , but such a configuration requires a large number of regenerators. To increase the efficiency of the absorption solution by increasing the number of concentration stages of the absorption solution, and to increase the number of solution heat exchangers to increase the heat recovery rate, and the merit of improving the performance of the absorption refrigeration system, and the regenerator and When weighed against the disadvantage of increasing the manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. is there.

V: Fifth Embodiment FIG. 9 shows an operation cycle of an absorption refrigerating apparatus Z _{5 according to} a fifth embodiment of the present invention. The absorption type refrigerating apparatus Z ₅ has the same basic configuration as the absorption type refrigerating apparatus Z ₁ according to the first embodiment, and is different from this in the absorption type refrigerating apparatus of the first embodiment. Refrigerator Z ₁
In the above, the cooling water Wa for cooling the absorber A and the condenser C was made to flow from the absorber A side to the condenser C side, whereas the absorption type of this embodiment is used. In the refrigerating device Z ₅ , the cooling water Wa is made to flow from the condenser C side toward the absorber A side. Therefore, the cooling water inlet pipe 41 in the first embodiment serves as the cooling water outlet pipe, and the cooling water outlet pipe 43 serves as the cooling water inlet pipe.

By using such a cooling water circulation system, for example, the cooling water W having a lower temperature in the condenser C than in the case where the cooling water Wa flows from the absorber A side to the condenser C side.
Since a is supplied, the cooling capacity of the condenser C is improved, and the operating pressure of the low temperature regenerator G ₁ connected to the condenser C is reduced accordingly. As a result, the maximum pressure of the operating pressure of the entire cycle governed by the operating pressure of the low temperature regenerator G ₁ , that is, the operating pressure of the high temperature regenerator G ₃ is reduced, and the absorption refrigerating device having more excellent operability is reduced. Can be provided.

The structure of the absorption refrigerating apparatus Z ₅ and the functions and effects other than those described above are the same as those of the absorption refrigerating apparatus Z ₁ of the first embodiment described above. The description is omitted by using the description.

The structure of this embodiment (that is, the cooling water W
The structure in which the flow direction of a is changed from the condenser to the absorber) is
~ It is also applicable to the fourth embodiment.

VI: Sixth Embodiment FIG. 10 shows an operation cycle of an absorption refrigeration system Z _{6 according to} a sixth embodiment of the present invention. The absorption refrigerating apparatus Z ₆ has the same basic configuration as the absorption refrigerating apparatus Z ₁ according to the _first embodiment, and is different from this in the absorber A and the evaporator E. Is a two-stage configuration having different refrigerant evaporation temperatures, and both the low temperature regenerator G ₁ and the condenser C are two-stage configurations having different refrigerant condensation temperatures. The absorber A, the evaporator E, the low-temperature regenerator G ₁ and the condenser C may be configured in two or more stages.

With such a structure, the entire cycle of the absorption refrigerating apparatus Z ₆ is shifted to the low concentration side, and the operating pressure of the system is reduced accordingly, so that the absorption refrigerating apparatus having good operability can be provided. .

The structure of the absorption refrigerating apparatus Z ₆ and the operational effects other than those described above are the same as those of the absorption refrigerating apparatus Z ₁ of the first embodiment described above, and therefore, they correspond to the first embodiment. The description is omitted by using the description.

The structure of this embodiment (that is, the structure in which the absorber A, the evaporator E, the low temperature regenerator G ₁ and the condenser C have a multi-stage structure of two or more stages) is the second to the fifth. It is also applicable to the embodiment.

VII: Seventh Embodiment FIG. 11 shows an operation cycle of an absorption type refrigeration system Z _{7 according to} a seventh embodiment of the present invention. This absorption refrigeration apparatus Z ₇ is an absorption refrigeration apparatus that uses water as a refrigerant and lithium bromide as an absorption liquid, and includes one condenser C, one absorber A, one evaporator E, and three each. Solution heat exchanger H ₃ ,
H ₂ and H ₁ and regenerators G ₃ , G ₂ and G ₁ are used as a basic configuration, and in addition to this, two drain heat exchangers D ₁ and D ₂ and one exhaust heat exchanger K are provided. These devices are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E comprises a heat exchange section 7 for passing the liquid We to be cooled and a refrigerant distributor (not shown) for distributing a refrigerant on the heat exchange section 7.

The absorber A comprises a solution sprayer (not shown) for spraying a concentrated solution, and a heat exchange section 8 for removing the absorption heat generated in the absorber A.

The condenser C comprises a heat exchange section 11.

Each of the regenerators G ₃ , G ₂ , and G ₁ is for heating and concentrating the absorption solution containing the refrigerant to obtain a concentrated solution having a high concentration in sequence. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium temperature regenerator G ₂ (“low temperature side regenerator” in the claims) that is configured with a solution heating unit 14 through which an external heat source J (for example, combustion gas or steam) passes. G corresponds to _n-1 ") is configured with a solution heating unit 9, and most low-temperature regenerator G ₁ operating at a low temperature (corresponding to" the lowest temperature side of the regenerator G ₁ "in the claims Is provided with a solution heating unit 10.

Each of the heat exchangers H ₁ , H ₂ , and H ₃ has a low-temperature concentrated solution L ₁ , a medium-temperature concentrated solution L ₂ , and a high-temperature concentrated solution produced by the regenerators G ₁ , G ₂ , and G _3. It is for recovering the heat of each of L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types,
For example, a plate heat exchanger may be used.

The respective drain heat exchangers D ₁ and D ₂ are vapor drains D produced by the low temperature regenerator G ₁ and the medium temperature regenerator G _2.
It recovers the heat of r ₁ and Dr ₂ to the dilute solution La side and is generally a shell-and-tube type heat exchanger, but is composed of another type such as a plate type heat exchanger. Is also good.

Each of these devices is operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the condenser C and the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30 to the evaporator E side. Supplied. The liquid refrigerant Rc supplied to the evaporator E is sprayed from the refrigerant distributor to the heat exchange section 7 side.

From the liquid to be cooled inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We flowing in to and flowing out from the liquid to be cooled outlet pipe 46 is cooled by the heat of evaporation of the refrigerant. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

At the bottom of the absorber A, a solution pump LP
The dilute solution pipe 21 including is connected. After passing through the heated side of the low temperature solution heat exchanger H ₁ , the dilute solution pipe 21 is branched into two paths, a first branch pipe 22 and a second branch pipe 23. Then, the first branch pipe 22
Passes through the heated side of the high temperature solution heat exchanger H ₃ and further through the heated side of the exhaust heat exchanger K, and the high temperature regenerator G
Connected to ₃ . Further, the second branch pipe 23,
It is connected to the medium temperature regenerator G ₂ through the heated side of the medium temperature solution heat exchanger H ₂ . Therefore, the dilute solution La flowing out of the absorber A branches after passing through the heated side of the low temperature solution heat exchanger H ₁ , and _one of them branches through the high temperature solution heat exchanger H ₃ to the high temperature regenerator. It flows into G ₃ , and the other flows into the intermediate temperature regenerator G ₂ via the intermediate temperature solution heat exchanger H ₂ .

Further, the dilute solution pipe 21 bypasses the low temperature solution heat exchanger H ₁ and passes through the heated side of the first drain heat exchanger D ₁ to pass the low temperature solution heat exchanger H _1. An absorption solution branch pipe 47 for connecting the front and the rear of the is provided.
The second branch pipe 23 bypasses the medium temperature solution heat exchanger H ₂ and passes through the heated side of the second drain heat exchanger D ₂ before and after the medium temperature solution heat exchanger H ₂ . An absorption solution branch pipe 48 for connecting the above is provided.

The medium temperature solution pipe 26, which is connected to the medium temperature regenerator G ₂ and guides the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G ₂ , passes through the heating side of the medium temperature solution heat exchanger H _2. It is connected to the low temperature regenerator G ₁ .

High temperature regenerator G₃Connected to the high temperature re
Organ G₃High temperature concentrated solution L flowing out from₃The above high temperature melting
Liquid heat exchanger H₃High temperature solution pipe 27 passing through the heating side of
Low temperature regenerator G₁Connected to the low temperature regenerator G₁Spilled from
Low temperature concentrated solution L₁The low temperature solution pipe 25 that guides
To become the concentrated solution pipe 24, and the low temperature solution heat exchanger H ₁
Is connected to the absorber A through the heating side of.

The solution heating section 14 of the 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. Also, the high temperature regenerator G
The air chamber side of ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is connected to the condenser C through the heating side of the second drain heat exchanger D _2. ing.

The solution heating section 10 of the low temperature regenerator G ₁
The refrigerant drain pipe 35 connected to the outlet side of the
It is connected to the condenser C through the heating side of the drain heat exchanger D ₁ .

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The heat exchange section 8 of the absorber A and the heat exchange section 11 of the condenser C are connected via a cooling water pipe 42, and the cooling water W flowing in from the cooling water inlet pipe 41 side.
a performs a cooling action on the condenser C side,
Further, the absorber A side has a cooling effect and is discharged from the cooling water outlet pipe 43.

The absorption refrigeration system Z ₇ constitutes a circulation cycle of the refrigerant and the absorption solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₇ will be specifically described.

The dilute solution La fed from the absorber A by the solution pump LP is the low temperature solution heat exchanger H.
Branched in ₁ immediately preceding, cold strong solution L ₁ and the high-temperature regenerator from the low temperature regenerator G ₁ portion thereof passing through the heating side by passing through the heated side of the low temperature solution heat exchanger H ₁ It is concentrated solution Lg preheating by heat exchange made by merging the high-temperature concentrated solution L ₃ from G _3. Also, another portion is preheated by steam drain Dr ₁ exchanges heat from the low temperature generator G ₁ through the heated side by passing through the first heated side of the drain heat exchanger D ₁ . The diluted solutions La thus branched and individually preheated are merged again, and then branched again to the first branch pipe 22 side and the second branch pipe 23 side.

The dilute solution La branched to the side of the first branch pipe 22 exchanges heat with the high temperature concentrated solution L ₃ passing through the heated side of the high temperature solution heat exchanger H ₃ by passing through the heated side. The external heat source J is preheated by the exhaust heat exchanger K and is passed through the heated side of the exhaust heat exchanger K to pass through the heated side.
After being preheated by exchanging heat with the residual heat Q of the above, it flows into the high temperature regenerator G ₃ . Then, the dilute solution La flowing into the high temperature regenerator G ₃ is subjected to the heating and concentrating action of the external heat source J to become a high temperature concentrated solution L ₃ and flows out, so that the heating side of the high temperature solution heat exchanger H ₃ is discharged. Pass through.

On the other hand, the dilute solution La branched to the side of the second branch pipe 23 is further branched immediately before the medium temperature solution heat exchanger H _{2 and} a part of the diluted solution La is heated by the medium temperature solution heat exchanger H ₂ . The intermediate temperature regenerator G ₂ which passes through the heating side
It is preheated by exchanging heat with the medium-temperature concentrated solution L ₂ from. Also,
Another portion is preheated by steam drain Dr ₂ exchanges heat from the intermediate temperature regenerator G ₂ through the heating side by passing through the second heated side of the drain heat exchanger D _2.

The dilute solutions La branched and individually preheated in this way are merged again, and then the medium temperature regenerator G is used.
₂ into the medium temperature regenerator G _{2 and the} high temperature regenerator G
The low temperature regenerator G is heated and concentrated by the refrigerant vapor R ₃ flowing into the solution heating section 9 from the ₃ side, flows out as a medium temperature concentrated solution L ₂ , passes through the heating side of the medium temperature solution heat exchanger H _2. Inflow to ₁ .

Further, the medium-temperature concentrated solution L ₂ flowing into the low temperature regenerator G ₁ is a refrigerant vapor R ₂ flowing into the solution heating section 10 from the medium temperature regenerator G ₂ side in the low temperature regenerator G ₁ .
Is concentrated by heating to form a low temperature concentrated solution L ₁ and flows out.

[0212] Then, the joined the low temperature regenerator G ₁ cold concentrated solution L ₁ which flows from the high-temperature concentrated solution L ₃ flowing out from the high temperature generator G ₃ side, heating of the low-temperature solution heat exchanger H ₁ And flows into the absorber A side.

The above is the absorption refrigerating apparatus Z _{7 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

Absorption-type refrigeration equipment according to the seventh embodiment
Setting Z₇In, the diluted solution La discharged from the absorber A is
The high temperature regenerator is branched and
G₃To the middle temperature regenerator.
G₂Flow into the low temperature regenerator G₁Flowed into
The medium temperature regenerator G is constructed as described above.₂To
In this case, the unconcentrated dilute solution La may flow in as it is.
And, for example, the high temperature regenerator G₃Absorbed by heating at
Compared with the case where a solution (concentrated solution) is flowed in,
The lower the concentration, the lower the boiling temperature. This
Medium temperature regenerator G ₂Of the boiling temperature of the absorbing solution in water
Only, the high temperature regenerator G that serves as its heating source₃Cold in
Since the temperature of the medium vapor can be set low,
The high temperature regenerator G proportional to the temperature of the medium vapor₃The operating pressure of
Can be set lower, which results in lower operating pressure.
It is possible to provide an absorption type refrigerating device with good movability.
Becomes

Further, since the dilute solution La from the absorber A is branched and a part of the dilute solution La is caused to flow into the high temperature regenerator G ₃ , for example, the entire amount of the dilute solution La is directly kept in the high temperature regenerator G 3. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ ) is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system is improved.

[0216] Further, the absorber part thereof is branched dilute solution La from A by which so as to flow into the high-temperature regenerator G _3, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution L flowing in here is supplied.
As the amount of a decreases, the heat transfer area can be reduced to make the device compact, which in turn contributes to making the absorption refrigeration system compact.

Further, the absorption refrigerating apparatus Z _{7 of} this embodiment is also provided.
In this case, since the diluted solution La discharged from the absorber A is branched after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ is passed through the high temperature solution heat exchanger H ₃ immediately before it. And the dilute solution La flowing into the medium temperature regenerator G ₂ via the medium temperature solution heat exchanger H ₂ immediately before it.
Both flow into the low temperature solution heat exchanger H ₁ in a preheated state, and as a result, the required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ decreases, It is expected that the thermal efficiency of the entire system will improve.

Also, the absorption refrigerating apparatus Z _{7 of} this embodiment is used.
Then, the dilute solution L is generated by the residual heat Q after heating the high temperature regenerator G ₃ of the external heat source J for heating the high temperature regenerator G _3.
Since a is heated, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and further COP of the entire system can be expected to be further improved.

Furthermore, the absorption refrigerating apparatus Z of this embodiment.
In _7, since the structure to heat the dilute solution La by the low temperature regenerator G ₁ and the intermediate temperature regenerator steam drain Dr ₁ resulted in G _2, Dr _2, the steam drain Dr _1, Dr ₂
The heat retained by the can be effectively used for preheating the diluted solution La, and the thermal efficiency of the entire system can be further promoted.

Further, the absorption refrigerating apparatus Z _{7 of} this embodiment is also used.
Then, in the absorbing solution branch pipe 47 branched from the dilute solution pipe 21, the first drain heat exchanger D ₁ and in the absorbing solution branch pipe 48 branched from the second branch pipe 23, the second drain heat exchanger is exchanged. Since the dilute solution La is heated in the vessel D ₂ by the vapor drains Dr ₁ and Dr ₂ , respectively, the vapor drains Dr ₁ and
Since the amount of the absorbing solution heated by the retained heat of Dr ₂ is small, the absorbing solution can be efficiently preheated.

Further, the absorption type refrigeration system Z of this embodiment.
_{In 7} , the system is composed of three regenerators G ₁ , G ₂ and G ₃ and three solution heat exchangers H ₁ , H ₂ and H ₃ ; By increasing the number of concentration stages of the absorption solution to increase the thermal efficiency, and increasing the number of solution heat exchangers to increase the heat recovery rate, the merit of improving the performance of the absorption refrigeration system and the regenerator And, when weighed against the disadvantage of increased manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. Is.

VIII: Eighth Embodiment FIG. 12 shows an operation cycle of the absorption refrigeration system Z _{8 according} to the eighth embodiment of the present invention. The absorption type refrigerating apparatus Z ₈ is an absorption type refrigerating apparatus which uses water as a refrigerant and lithium bromide as an absorbing liquid, and includes one condenser C, an absorber A, an evaporator E, and three each. Solution heat exchanger H ₃ ,
H ₂ and H ₁ and regenerators G ₃ , G ₂ and G ₁ are used as a basic configuration, and in addition to this, two drain heat exchangers D ₁ and D ₂ and one exhaust heat exchanger K are provided. These devices are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E comprises a heat exchange section 7 for passing the liquid We to be cooled and a refrigerant distributor (not shown) for distributing a refrigerant on the heat exchange section 7.

The absorber A comprises a solution sprayer (not shown) for spraying a concentrated solution, and a heat exchange section 8 for removing absorption heat generated in the absorber A.

The condenser C comprises a heat exchange section 11.

Each of the regenerators G ₃ , G ₂ , and G ₁ is for heating and concentrating the absorption solution containing the refrigerant to successively obtain concentrated solutions of high concentration. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium temperature regenerator G ₂ (“low temperature side regenerator” in the claims) that is configured with a solution heating unit 14 through which an external heat source J (for example, combustion gas or steam) passes. G corresponds to _n-1 ") is configured with a solution heating unit 9, and most low-temperature regenerator G ₁ operating at a low temperature (corresponding to" the lowest temperature side of the regenerator G ₁ "in the claims Is provided with a solution heating unit 10.

Each of the heat exchangers H ₁ , H ₂ , and H ₃ has a low-temperature concentrated solution L ₁ , a medium-temperature concentrated solution L ₂ , and a high-temperature concentrated solution produced by the regenerators G ₁ , G ₂ , and G _3. It is for recovering the heat of each of L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types,
For example, a plate heat exchanger may be used.

The respective drain heat exchangers D ₁ and D ₂ are vapor drains D produced by the low temperature regenerator G ₁ and the medium temperature regenerator G _2.
It recovers the heat of r ₁ and Dr ₂ to the dilute solution La side and is generally a shell-and-tube type heat exchanger, but is composed of another type such as a plate type heat exchanger. Is also good.

Each of these devices is operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the condenser C and the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30 to the evaporator E side. Supplied. The liquid refrigerant Rc supplied to the evaporator E is sprayed from the refrigerant distributor to the heat exchange section 7 side.

From the liquid to be cooled inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We flowing in to and flowing out from the liquid to be cooled outlet pipe 46 is cooled by the heat of evaporation of the refrigerant. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

At the bottom of the absorber A, a solution pump LP
The dilute solution pipe 21 including is connected. After passing through the heated side of the low temperature solution heat exchanger H ₁ , the dilute solution pipe 21 is branched into two paths, a first branch pipe 22 and a second branch pipe 23. Then, the first branch pipe 22
Passes through the heated side of the high temperature solution heat exchanger H ₃ and further through the heated side of the exhaust heat exchanger K, and the high temperature regenerator G
Connected to ₃ . Further, the second branch pipe 23,
It is connected to the medium temperature regenerator G ₂ through the heated side of the medium temperature solution heat exchanger H ₂ . Therefore, the dilute solution La flowing out of the absorber A branches after passing through the heated side of the low temperature solution heat exchanger H ₁ , and _one of them branches through the high temperature solution heat exchanger H ₃ to the high temperature regenerator. It flows into G ₃ , and the other flows into the intermediate temperature regenerator G ₂ via the intermediate temperature solution heat exchanger H ₂ .

[0233] Further, the dilute solution pipe 21, the low-temperature solution heat exchanger H ₁ to the bypass and through the first heated side of the drain heat exchanger D ₁ low temperature solution heat exchanger H ₁ An absorption solution branch pipe 47 for connecting the front and the rear of the is provided.
The second branch pipe 23 bypasses the medium temperature solution heat exchanger H ₂ and passes through the heated side of the second drain heat exchanger D ₂ before and after the medium temperature solution heat exchanger H ₂ . An absorption solution branch pipe 48 for connecting the above is provided.

The medium temperature solution pipe 26, which is connected to the medium temperature regenerator G ₂ and guides the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G ₂ , passes through the heating side of the medium temperature solution heat exchanger H _2. It is connected to the low temperature regenerator G ₁ .

High temperature regenerator G₃Connected to the high temperature re
Organ G₃High temperature concentrated solution L flowing out from₃The above high temperature melting
Liquid heat exchanger H₃High temperature solution pipe 27 passing through the heating side of
Low temperature regenerator G₁Connected to the low temperature regenerator G₁Spilled from
Low temperature concentrated solution L₁The low temperature solution pipe 25 that guides
To become the concentrated solution pipe 24, and the low temperature solution heat exchanger H ₁
Is connected to the absorber A through the heating side of.

The solution heating section 14 of the 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. Also, the high temperature regenerator G
The air chamber side of ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is connected to the heating side of the second drain heat exchanger D ₂ and the first drain heat exchanger D. It is connected to the condenser C through the heating side of ₁ .

The solution heating section 10 of the low temperature regenerator G ₁
The outlet side of the refrigerant drain pipe 35 is connected to the refrigerant drain pipe 35, and the refrigerant drain pipe 35 is connected to the first drain heat exchanger D.
The refrigerant drain pipe 34 is joined in the middle of the _first and second drain heat exchangers D ₂ .

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The heat exchange section 8 of the absorber A and the heat exchange section 11 of the condenser C are connected via a cooling water pipe 42, and the cooling water W flowing in from the cooling water inlet pipe 41 side.
a performs a cooling action on the absorber A side,
Further, the condenser C side has a cooling function and is discharged from the cooling water outlet pipe 43.

The absorption refrigeration system Z ₈ constitutes a circulation cycle of the refrigerant and the absorption solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₈ will be specifically described.

The diluted solution La fed from the absorber A by the solution pump LP is the low temperature solution heat exchanger H.
Branched in ₁ immediately preceding, cold strong solution L ₁ and the high-temperature regenerator from the low temperature regenerator G ₁ portion thereof passing through the heating side by passing through the heated side of the low temperature solution heat exchanger H ₁ It is concentrated solution Lg preheating by heat exchange made by merging the high-temperature concentrated solution L ₃ from G _3. The other part is preheated by passing through the heated side of the first drain heat exchanger D _{1 and} exchanging heat with the steam drains Dr ₁ and Dr ₂ passing through the heating side. The diluted solutions La thus branched and individually preheated are merged again, and then branched again to the first branch pipe 22 side and the second branch pipe 23 side.

The diluted solution La branched to the first branch pipe 22 side exchanges heat with the high temperature concentrated solution L ₃ passing through the heated side of the high temperature solution heat exchanger H ₃ by passing through the heated side. The external heat source J is preheated by the exhaust heat exchanger K and is passed through the heated side of the exhaust heat exchanger K to pass through the heated side.
After being preheated by exchanging heat with the residual heat Q of the above, it flows into the high temperature regenerator G ₃ . Then, the dilute solution La flowing into the high temperature regenerator G ₃ is subjected to the heating and concentrating action of the external heat source J to become a high temperature concentrated solution L ₃ and flows out, so that the heating side of the high temperature solution heat exchanger H ₃ is discharged. Pass through.

On the other hand, the diluted solution La branched to the side of the second branch pipe 23 is further branched immediately before the medium temperature solution heat exchanger H _{2 and} a part of the diluted solution La is heated by the medium temperature solution heat exchanger H ₂ . The intermediate temperature regenerator G ₂ which passes through the heating side
It is preheated by exchanging heat with the medium-temperature concentrated solution L ₂ from. Also,
Another portion is preheated by steam drain Dr ₂ exchanges heat from the intermediate temperature regenerator G ₂ through the heating side by passing through the second heated side of the drain heat exchanger D _2.

The dilute solutions La branched and individually preheated in this way are merged again, and then the intermediate temperature regenerator G is added.
₂ into the medium temperature regenerator G _{2 and the} high temperature regenerator G
The low temperature regenerator G is heated and concentrated by the refrigerant vapor R ₃ flowing into the solution heating section 9 from the ₃ side, flows out as a medium temperature concentrated solution L ₂ , passes through the heating side of the medium temperature solution heat exchanger H _2. Inflow to ₁ .

Further, the medium temperature concentrated solution L ₂ flowing into the low temperature regenerator G ₁ is a refrigerant vapor R ₂ flowing into the solution heating section 10 from the medium temperature regenerator G ₂ side in the low temperature regenerator G ₁ .
Is concentrated by heating to form a low temperature concentrated solution L ₁ and flows out.

[0249] Then, the joined the low temperature regenerator G ₁ cold concentrated solution L ₁ which flows from the high-temperature concentrated solution L ₃ flowing out from the high temperature generator G ₃ side, heating of the low-temperature solution heat exchanger H ₁ And flows into the absorber A side.

The absorption refrigeration system Z _{8 of} this embodiment has been described above.
In the operation cycle, the following unique action and effects are obtained.

Absorption-type refrigeration equipment according to the eighth embodiment
Setting Z₈In, the diluted solution La discharged from the absorber A is
The high temperature regenerator is branched and
G₃To the middle temperature regenerator.
G₂Flow into the low temperature regenerator G₁Flowed into
The medium temperature regenerator G is constructed as described above.₂To
In this case, the unconcentrated dilute solution La may flow in as it is.
And, for example, the high temperature regenerator G₃Absorbed by heating at
Compared with the case where a solution (concentrated solution) is flowed in,
The lower the concentration, the lower the boiling temperature. This
Medium temperature regenerator G ₂Of the boiling temperature of the absorbing solution in water
Only, the high temperature regenerator G that serves as its heating source₃Cold in
Since the temperature of the medium vapor can be set low,
The high temperature regenerator G proportional to the temperature of the medium vapor₃The operating pressure of
Can be set lower, which results in lower operating pressure.
It is possible to provide an absorption type refrigerating device with good movability.
Becomes

Further, since the dilute solution La from the absorber A is branched and a part of the dilute solution La is caused to flow into the high temperature regenerator G ₃ , for example, the entire amount of the dilute solution La is kept as it is. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ ) is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system is improved.

[0253] Further, the absorber part thereof is branched dilute solution La from A by which so as to flow into the high-temperature regenerator G _3, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution L flowing in here is supplied.
As the amount of a decreases, the heat transfer area can be reduced to make the device compact, which in turn contributes to making the absorption refrigeration system compact.

The absorption refrigerating apparatus Z _{8 of} this embodiment is also used.
In this case, since the diluted solution La discharged from the absorber A is branched after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ is passed through the high temperature solution heat exchanger H ₃ immediately before it. And the dilute solution La flowing into the medium temperature regenerator G ₂ via the medium temperature solution heat exchanger H ₂ immediately before it.
Both flow into the low temperature solution heat exchanger H ₁ in a preheated state, and as a result, the required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ decreases, It is expected that the thermal efficiency of the entire system will improve.

The absorption refrigerating apparatus Z _{8 of} this embodiment is also used.
Then, the dilute solution L is generated by the residual heat Q after heating the high temperature regenerator G ₃ of the external heat source J for heating the high temperature regenerator G _3.
Since a is heated, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and further COP of the entire system can be expected to be further improved.

Furthermore, the absorption type refrigeration system Z of this embodiment.
In _8, since the structure to heat the dilute solution La by the low temperature regenerator G ₁ and the intermediate temperature regenerator steam drain Dr ₁ resulted in G _2, Dr _2, the steam drain Dr _1, Dr ₂
The heat retained by the can be effectively used for preheating the diluted solution La, and the thermal efficiency of the entire system can be further promoted.

The absorption refrigerating apparatus Z _{8 of} this embodiment is also used.
In, it is combined with a steam drain Dr ₂ generated in the low temperature regenerator G steam drain Dr ₁ produced in ₁ and the intermediate temperature regenerator G _2, configured and to heat the dilute solution La with the merged steam drain Therefore, the absorption solution can be efficiently preheated with a larger amount of heat.

Furthermore, the absorption type refrigeration system Z of this embodiment.
_{In 8} , in the absorption solution branch pipe 47 branched from the dilute solution pipe 21, the first drain heat exchanger D ₁ and in the absorption solution branch pipe 48 branched from the second branch pipe 23, the second drain heat Since the dilute solution La is heated by the vapor drains Dr ₁ and Dr _{2 in the} exchanger D ₂ , the vapor drain D
Since the amount of the absorbing solution heated by the retained heat of r ₁ and Dr ₂ is small, the absorbing solution can be efficiently preheated.

The absorption refrigerating apparatus Z _{8 of} this embodiment is also used.
Then, the system is configured by _three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ , but such a configuration requires a large number of regenerators. To increase the efficiency of the absorption solution by increasing the number of concentration stages of the absorption solution, and to increase the number of solution heat exchangers to increase the heat recovery rate, and the merit of improving the performance of the absorption refrigeration system, and the regenerator and When weighed against the disadvantage of increasing the manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. is there.

IX: Ninth Embodiment FIG. 13 shows an operation cycle of an absorption refrigeration system Z _{9 according to} a ninth embodiment of the present invention. The absorption type refrigerating apparatus Z ₉ is an absorption type refrigerating apparatus which uses water as a refrigerant and lithium bromide as an absorbing liquid, and includes one condenser C, an absorber A, an evaporator E, and three pieces each. Solution heat exchanger H ₃ ,
H ₂ and H ₁ and regenerators G ₃ , G ₂ and G ₁ are the basic components, and in addition to this, three drain heat exchangers D ₁ , D ₂ and 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 form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E comprises a heat exchange section 7 for passing the liquid We to be cooled and a refrigerant distributor (not shown) for distributing the refrigerant on the heat exchange section 7.

The absorber A comprises a solution sprayer (not shown) for spraying a concentrated solution, and a heat exchange section 8 for removing the absorption heat generated in the absorber A.

The condenser C comprises a heat exchange section 11.

Each of the regenerators G ₃ , G ₂ , and G ₁ is for heating and concentrating the absorbing solution containing the refrigerant to successively obtain concentrated solutions of high concentration. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium temperature regenerator G ₂ (“low temperature side regenerator” in the claims) that is configured with a solution heating unit 14 through which an external heat source J (for example, combustion gas or steam) passes. G corresponds to _n-1 ") is configured with a solution heating unit 9, and most low-temperature regenerator G ₁ operating at a low temperature (corresponding to" the lowest temperature side of the regenerator G ₁ "in the claims Is provided with a solution heating unit 10.

The heat exchangers H ₁ , H ₂ , and H ₃ have low-temperature concentrated solution L ₁ , medium-temperature concentrated solution L ₂ , and high-temperature concentrated solution produced by the regenerators G ₁ , G ₂ , and G ₃ , respectively. It is for recovering the heat of each of L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types,
For example, a plate heat exchanger may be used.

The above drain heat exchangers D ₁ , D ₂ and D ₃ are
The heat of the steam drains Dr ₁ and Dr ₂ generated in the low temperature regenerator G ₁ and the medium temperature regenerator G ₂ is recovered to the dilute solution La side, and is generally a shell-and-tube heat exchanger. However, other types, for example, plate type heat exchangers may be used.

Each of these devices is operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the condenser C and the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc produced in the condenser C is transferred to the evaporator E side through the liquid refrigerant pipe 30. Supplied. The liquid refrigerant Rc supplied to the evaporator E is sprayed from the refrigerant distributor to the heat exchange section 7 side.

From the liquid to be cooled inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We flowing in to and flowing out from the liquid to be cooled outlet pipe 46 is cooled by the heat of evaporation of the refrigerant. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

At the bottom of the absorber A, a solution pump LP
The dilute solution pipe 21 including is connected. After passing through the heated side of the low temperature solution heat exchanger H ₁ , the dilute solution pipe 21 is branched into two paths, a first branch pipe 22 and a second branch pipe 23. Then, the first branch pipe 22
Passes through the heated side of the high temperature solution heat exchanger H ₃ and further through the heated side of the exhaust heat exchanger K, and the high temperature regenerator G
Connected to ₃ . Further, the second branch pipe 23,
It is connected to the medium temperature regenerator G ₂ through the heated side of the medium temperature solution heat exchanger H ₂ . Therefore, the dilute solution La flowing out of the absorber A branches after passing through the heated side of the low temperature solution heat exchanger H ₁ , and _one of them branches through the high temperature solution heat exchanger H ₃ to the high temperature regenerator. It flows into G ₃ , and the other flows into the intermediate temperature regenerator G ₂ via the intermediate temperature solution heat exchanger H ₂ .

Further, in the dilute solution pipe 21, the low temperature solution heat exchanger H ₁ is bypassed and the heated side of the first drain heat exchanger D _{1 and} the heated side of the third drain heat exchanger D ₃ are heated. An absorption solution branch pipe 47 is provided to connect the low temperature solution heat exchanger H _{1 to} the front and rear of the low temperature solution heat exchanger H ₁ . The second branch pipe 23 bypasses the medium temperature solution heat exchanger H ₂ and passes through the heated side of the second drain heat exchanger D ₂ before and after the medium temperature solution heat exchanger H ₂ . An absorption solution branch pipe 48 for connecting the above is provided.

The medium temperature solution pipe 26, which is connected to the medium temperature regenerator G ₂ and guides the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G ₂ , passes through the heating side of the medium temperature solution heat exchanger H _2. It is connected to the low temperature regenerator G ₁ .

High temperature regenerator G₃Connected to the high temperature re
Organ G₃High temperature concentrated solution L flowing out from₃The above high temperature melting
Liquid heat exchanger H₃High temperature solution pipe 27 passing through the heating side of
Low temperature regenerator G₁Connected to the low temperature regenerator G₁Spilled from
Low temperature concentrated solution L₁The low temperature solution pipe 25 that guides
To become the concentrated solution pipe 24, and the low temperature solution heat exchanger H ₁
Connected to the solution spreader of absorber A above through the heating side of
ing.

The solution heating section 14 of the 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. Also, the high temperature regenerator G
The air chamber side of ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G _{2 has} the heating side of the second drain heat exchanger D ₂ and the third drain heat exchanger D ₃ Is sequentially connected to the condenser C through the heating side.

The solution heating section 10 of the low temperature regenerator G ₁
The refrigerant drain pipe 35 connected to the outlet side of the
It is connected to the condenser C through the heating side of the drain heat exchanger D ₁ .

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The heat exchange section 8 of the absorber A and the heat exchange section 11 of the condenser C are connected via a cooling water pipe 42, and the cooling water W flowing in from the cooling water inlet pipe 41 side.
a performs a cooling action on the absorber A side,
Further, the condenser C side has a cooling function and is discharged from the cooling water outlet pipe 43. Note that the cooling water Wa may have a structure in which the flow direction of the cooling water Wa is changed from the condenser to the absorber.

The absorption type refrigerating apparatus Z ₉ constitutes a circulation cycle of the refrigerant and the absorbing solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption type refrigerating apparatus Z ₉ will be specifically described.

The dilute solution La fed from the absorber A by the solution pump LP is the low temperature solution heat exchanger H.
Branched in ₁ immediately preceding, cold solution L ₁ and the high-temperature regenerator G from the low temperature regenerator G ₁ portion thereof passing through the heating side by passing through the heated side of the low temperature solution heat exchanger H ₁ It is preheated by exchanging heat with the concentrated solution Lg formed by joining the high-temperature concentrated solution L ₃ from ₃ together. Also, another portion is preheated by steam drain Dr ₁ exchanges heat from the low temperature generator G ₁ through the heated side by passing through the first heated side of the drain heat exchanger D ₁ At the same time, by further passing through the heated side of the third drain heat exchanger D ₃ , the intermediate temperature regenerator G ₂ passing through the heated side of the third drain heat exchanger D ₃ is passed.
It is preheated by exchanging heat with the steam drain Dr ₂ from. The dilute solutions La thus branched and individually preheated
Are merged again and then branched again to the first branch pipe 22 side and the second branch pipe 23 side.

Then, branch to the first branch pipe 22 side.
The diluted solution La is the high temperature solution heat exchanger H₃On the heated side
Hot solution L passing through the heating side by passing₃Exchange heat with
Is preheated by the exhaust heat exchanger K
Of the external heat source J passing through the heating side by passing through the heating side
After being preheated by exchanging heat with the residual heat Q, the above high temperature regenerator G
₃Flow into. And the above-mentioned high temperature regenerator G₃Rare flowing into
The solution La receives the heating concentration effect by the external heat source J.
K, high temperature concentrated solution L₃And flow out, and heat exchange with the high temperature solution
Exchanger H₃On the heated side of.

On the other hand, the diluted solution La branched to the side of the second branch pipe 23 is further branched immediately before the medium temperature solution heat exchanger H _{2 and} a part of the diluted solution La is heated by the medium temperature solution heat exchanger H ₂ . The intermediate temperature regenerator G ₂ which passes through the heating side
It is preheated by exchanging heat with the medium temperature solution L ₂ from. The other part is preheated by exchanging heat with the steam drain Dr ₂ from the intermediate temperature regenerator G ₂ passing through the heated side of the second drain heat exchanger D ₂ and passing through the heated side. .

The dilute solutions La thus branched and individually preheated are re-merged, and then the intermediate temperature regenerator G is added.
₂ into the medium temperature regenerator G _{2 and the} high temperature regenerator G
The low temperature regenerator G is heated and concentrated by the refrigerant vapor R ₃ flowing into the solution heating section 9 from the ₃ side, flows out as a medium temperature concentrated solution L ₂ , passes through the heating side of the medium temperature solution heat exchanger H _2. Inflow to ₁ .

Further, the medium-temperature concentrated solution L ₂ flowing into the low temperature regenerator G ₁ is a refrigerant vapor R ₂ flowing into the solution heating section 10 from the medium temperature regenerator G ₂ side in the low temperature regenerator G ₁ .
Is concentrated by heating to form a low temperature concentrated solution L ₁ and flows out.

[0287] Then, the joined the low temperature regenerator G ₁ cold concentrated solution L ₁ which flows from the high-temperature concentrated solution L ₃ flowing out from the high temperature generator G ₃ side, heating of the low-temperature solution heat exchanger H ₁ And flows into the absorber A side.

The above is the absorption refrigeration system Z _{9 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

Absorption refrigeration equipment according to the ninth embodiment
Setting Z₉In, the diluted solution La discharged from the absorber A is
The high temperature regenerator is branched and
G₃To the middle temperature regenerator.
G₂Flow into the low temperature regenerator G₁Flowed into
The medium temperature regenerator G is constructed as described above.₂To
In this case, the unconcentrated dilute solution La may flow in as it is.
And, for example, the high temperature regenerator G₃Absorbed by heating at
Compared with the case where a solution (concentrated solution) is flowed in,
The lower the concentration, the lower the boiling temperature. This
Medium temperature regenerator G ₂Of the boiling temperature of the absorbing solution in water
Only, the high temperature regenerator G that serves as its heating source₃Cold in
Since the temperature of the medium vapor can be set low,
The high temperature regenerator G proportional to the temperature of the medium vapor₃The operating pressure of
Can be set lower, which results in lower operating pressure.
It is possible to provide an absorption type refrigerating device with good movability.
Becomes

Further, since the dilute solution La from the absorber A is branched and a part of the dilute solution La is made to flow into the high temperature regenerator G ₃ , for example, the entire amount of the dilute solution La is kept as it is. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ ) is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system is improved.

[0291] Further, the absorber part thereof is branched dilute solution La from A by which so as to flow into the high-temperature regenerator G _3, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution L flowing in here is supplied.
As the amount of a decreases, the heat transfer area can be reduced to make the device compact, which in turn contributes to making the absorption refrigeration system compact.

The absorption refrigerating apparatus Z _{9 of} this embodiment is also used.
In this case, since the diluted solution La discharged from the absorber A is branched after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ is passed through the high temperature solution heat exchanger H ₃ immediately before it. And the dilute solution La flowing into the medium temperature regenerator G ₂ via the medium temperature solution heat exchanger H ₂ immediately before it.
Both flow into the low temperature solution heat exchanger H ₁ in a preheated state, and as a result, the required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ decreases, It is expected that the thermal efficiency of the entire system will improve.

The absorption refrigerating apparatus Z _{9 of} this embodiment is also used.
Then, the dilute solution L is generated by the residual heat Q after heating the high temperature regenerator G ₃ of the external heat source J for heating the high temperature regenerator G _3.
Since a is heated, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and further COP of the entire system can be expected to be further improved.

Further, the absorption type refrigeration system Z of this embodiment.
In _9, since the structure to heat the dilute solution La by the low temperature regenerator G ₁ and the intermediate temperature regenerator steam drain Dr ₁ resulted in G _2, Dr _2, the steam drain Dr _1, Dr ₂
The heat retained by the can be effectively used for preheating the diluted solution La, and the thermal efficiency of the entire system can be further promoted.

The absorption refrigerating apparatus Z _{9 of} this embodiment is also used.
Then, in the absorption solution branch pipe 47 branched from the dilute solution pipe 21, the first and third drain heat exchangers D ₁ and D _{3 are}
And in the absorption solution branch pipe 48 branched from the second branch pipe 23, the second drain heat exchanger D
₂ , the diluted solution La is added to the vapor drains Dr ₁ and Dr, respectively.
Since configured to heat by _2, since the amount of absorption solution is heated by the heat possessed the steam drain Dr _1, Dr ₂ is small, efficiently absorbing solution can preheat.

Further, the absorption type refrigerating apparatus Z of this embodiment.
_{In the ninth aspect} , since the vapor drain Dr ₂ is configured to perform heating of the absorbing solution in multiple stages in the second drain heat exchanger D ₂ and the third drain heat exchanger D ₃ , mutual heat exchange is performed. The temperature difference between the diluted solution La and the steam drain Dr ₂ is equalized as much as possible at each heating position, the heat recovery efficiency of the entire system is improved, and the thermal efficiency of the absorption refrigeration system is further improved. Can be expected.

The absorption refrigerating apparatus Z _{9 of} this embodiment is also used.
Then, the system is configured by _three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ , but such a configuration requires a large number of regenerators. To increase the efficiency of the absorption solution by increasing the number of concentration stages of the absorption solution, and to increase the number of solution heat exchangers to increase the heat recovery rate, and the merit of improving the performance of the absorption refrigeration system, and the regenerator and When weighed against the disadvantage of increasing the manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. is there.

X: Tenth Embodiment FIG. 14 shows an operation cycle of an absorption type refrigeration system Z _{10 according to} a tenth embodiment of the present invention. The absorption type refrigerating apparatus Z ₁₀ is an absorption type refrigerating apparatus which uses water as a refrigerant and lithium bromide as an absorbing liquid and includes one condenser C, an absorber A, an evaporator E, and three pieces each. Solution heat exchanger H ₃ ,
H ₂ and H ₁ and regenerators G ₃ , G ₂ and G ₁ are the basic components, and in addition to this, three drain heat exchangers D ₁ , D ₂ and 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 form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E comprises a heat exchange section 7 for passing the liquid We to be cooled, and a refrigerant distributor (not shown) for distributing a refrigerant on the heat exchange section 7.

The absorber A comprises a solution sprayer (not shown) for spraying a concentrated solution, and a heat exchange section 8 for removing the absorption heat generated in the absorber A.

The condenser C comprises a heat exchange section 11.

Each of the regenerators G ₃ , G ₂ and G ₁ is for the purpose of heating and concentrating the absorption solution containing the refrigerant to obtain a concentrated solution having a high concentration in sequence. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium temperature regenerator G ₂ (“low temperature side regenerator” in the claims) that is configured with a solution heating unit 14 through which an external heat source J (for example, combustion gas or steam) passes. G corresponds to _n-1 ") is configured with a solution heating unit 9, and most low-temperature regenerator G ₁ operating at a low temperature (corresponding to" the lowest temperature side of the regenerator G ₁ "in the claims Is provided with a solution heating unit 10.

The heat exchangers H ₁ , H ₂ and H ₃ have the low temperature concentrated solution L ₁ , the medium temperature concentrated solution L ₂ and the high temperature concentrated solution produced by the regenerators G ₁ , G ₂ and G ₃ , respectively. It is for recovering the heat of each of L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types,
For example, a plate heat exchanger may be used.

The drain heat exchangers D ₁ , D ₂ and D ₃ are
The heat of the steam drains Dr ₁ and Dr ₂ generated in the low temperature regenerator G ₁ and the medium temperature regenerator G ₂ is recovered to the dilute solution La side, and is generally a shell-and-tube heat exchanger. However, other types, for example, plate type heat exchangers may be used.

Each of these devices is operatively connected by a solution piping system and a refrigerant piping system as follows.

That is, the condenser C and the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30 to the evaporator E side. Supplied. The liquid refrigerant Rc supplied to the evaporator E is sprayed from the refrigerant distributor to the heat exchange section 7 side.

From the liquid to be cooled inlet pipe 45 to the heat exchange unit 7
The liquid to be cooled (water) We flowing in to and flowing out from the liquid to be cooled outlet pipe 46 is cooled by the heat of evaporation of the refrigerant. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

At the bottom of the absorber A, a solution pump LP
The dilute solution pipe 21 including is connected. After passing through the heated side of the low temperature solution heat exchanger H ₁ , the dilute solution pipe 21 is branched into two paths, a first branch pipe 22 and a second branch pipe 23. Then, the first branch pipe 22
Passes through the heated side of the high temperature solution heat exchanger H ₃ and further through the heated side of the exhaust heat exchanger K, and the high temperature regenerator G
Connected to ₃ . Further, the second branch pipe 23,
It is connected to the medium temperature regenerator G ₂ through the heated side of the medium temperature solution heat exchanger H ₂ . Therefore, the dilute solution La flowing out of the absorber A branches after passing through the heated side of the low temperature solution heat exchanger H ₁ , and _one of them branches through the high temperature solution heat exchanger H ₃ to the high temperature regenerator. It flows into G ₃ , and the other flows into the intermediate temperature regenerator G ₂ via the intermediate temperature solution heat exchanger H ₂ .

Further, in the dilute solution pipe 21, the low temperature solution heat exchanger H ₁ is bypassed and the heated side of the first drain heat exchanger D _{1 and} the heated side of the third drain heat exchanger D ₃ are heated. An absorption solution branch pipe 47 is provided to connect the low temperature solution heat exchanger H _{1 to} the front and rear of the low temperature solution heat exchanger H ₁ . The second branch pipe 23 bypasses the medium temperature solution heat exchanger H ₂ and passes through the heated side of the second drain heat exchanger D ₂ before and after the medium temperature solution heat exchanger H ₂ . An absorption solution branch pipe 48 for connecting the above is provided.

The medium temperature solution pipe 26, which is connected to the medium temperature regenerator G ₂ and guides the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G ₂ , passes through the heating side of the medium temperature solution heat exchanger H _2. It is connected to the low temperature regenerator G ₁ .

High temperature regenerator G₃Connected to the high temperature re
Organ G₃High temperature concentrated solution L flowing out from₃The above high temperature melting
Liquid heat exchanger H₃High temperature solution pipe 27 passing through the heating side of
Low temperature regenerator G₁Connected to the low temperature regenerator G₁Spilled from
Low temperature concentrated solution L₁The low temperature solution pipe 25 that guides
To become the concentrated solution pipe 24, and the low temperature solution heat exchanger H ₁
Is connected to the absorber A through the heating side of.

The solution heating section 14 of the 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. Also, the high temperature regenerator G
The air chamber side of ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is branched to the refrigerant drain pipe 36 immediately before the second drain heat exchanger D ₂ . The refrigerant drain pipe 34 is connected to the second
The refrigerant drain pipe 36 passes through the heating side of the drain heat exchanger D _{2, and} the refrigerant drain pipe 36 passes through the heating side of the third drain heat exchanger D ₃ , and then these two pipes 34 and 36 merge to form the condenser. It is connected to C.

The solution heating section 10 of the low temperature regenerator G ₁
The refrigerant drain pipe 35 connected to the outlet side of the
It is connected to the condenser C through the heating side of the drain heat exchanger D ₁ .

The refrigerant R ₁ generated in the low temperature regenerator G ₁ is transferred to the condenser C via the refrigerant passage 33.

The heat exchange section 8 of the absorber A and the heat exchange section 11 of the condenser C are connected via a cooling water pipe 42, and the cooling water W flowing in from the cooling water inlet pipe 41 side.
a performs a cooling action on the absorber A side,
Further, the condenser C side has a cooling function and is discharged from the cooling water outlet pipe 43. Note that the cooling water Wa may have a structure in which the flow direction of the cooling water Wa is changed from the condenser to the absorber.

The absorption refrigeration system Z ₁₀ constitutes a circulation cycle of the refrigerant and the absorption solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₁₀ will be specifically described.

The dilute solution La fed from the absorber A by the solution pump LP is the low temperature solution heat exchanger H.
Branched in ₁ immediately preceding, cold solution L ₁ and the high-temperature regenerator G from the low temperature regenerator G ₁ portion thereof passing through the heating side by passing through the heated side of the low temperature solution heat exchanger H ₁ It is preheated by exchanging heat with the concentrated solution Lg formed by joining the high-temperature concentrated solution L ₃ from ₃ together. Further, the other part exchanges heat with the steam drain Dr ₁ from the low temperature regenerator G ₁ passing through the heated side of the first drain heat exchanger D ₁ and passing through the heated side, and By passing through the heated side of the 3-drain heat exchanger D ₃ , heat is exchanged with the steam drain Dr ₂ from the above-mentioned intermediate temperature regenerator G ₂ passing through the heated side and preheated. The dilute solutions La that have been branched and individually preheated in this way are merged again, and then again, again on the first branch pipe 22 side and the second branch pipe 23.
Branched to the side.

Then, branch to the first branch pipe 22 side.
The diluted solution La is the high temperature solution heat exchanger H₃On the heated side
Hot solution L passing through the heating side by passing₃Exchange heat with
Is preheated by the exhaust heat exchanger K
Of the external heat source J passing through the heating side by passing through the heating side
After being preheated by exchanging heat with the residual heat Q, the above high temperature regenerator G
₃Flow into. And the above-mentioned high temperature regenerator G₃Rare flowing into
The solution La receives the heating concentration effect by the external heat source J.
K, high temperature concentrated solution L₃And flow out, and heat exchange with the high temperature solution
Exchanger H₃On the heated side of.

On the other hand, the dilute solution La branched to the side of the second branch pipe 23 is further branched immediately before the medium temperature solution heat exchanger H _{2 and} a part of the diluted solution La is heated by the medium temperature solution heat exchanger H ₂ . The intermediate temperature regenerator G ₂ which passes through the heating side
It is preheated by exchanging heat with the medium temperature solution L ₂ from. The other part is preheated by exchanging heat with the steam drain Dr ₂ from the intermediate temperature regenerator G ₂ passing through the heated side of the second drain heat exchanger D ₂ and passing through the heated side. .

The dilute solutions La thus branched and individually preheated are merged again, and then the intermediate temperature regenerator G is added.
₂ into the medium temperature regenerator G _{2 and the} high temperature regenerator G
The low temperature regenerator G is heated and concentrated by the refrigerant vapor R ₃ flowing into the solution heating section 9 from the ₃ side, flows out as a medium temperature concentrated solution L ₂ , passes through the heating side of the medium temperature solution heat exchanger H _2. Inflow to ₁ .

Further, the medium temperature concentrated solution L ₂ flowing into the low temperature regenerator G ₁ is a refrigerant vapor R ₂ flowing into the solution heating unit 10 from the medium temperature regenerator G ₂ side in the low temperature regenerator G ₁ .
Is concentrated by heating to form a low temperature concentrated solution L ₁ and flows out.

[0325] Then, the joined the low temperature regenerator G ₁ cold concentrated solution L ₁ which flows from the high-temperature concentrated solution L ₃ flowing out from the high temperature generator G ₃ side, heating of the low-temperature solution heat exchanger H ₁ And flows into the absorber A side.

The above is the absorption refrigeration apparatus Z _{10 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

Absorption refrigeration according to the tenth embodiment
Device Z_TenIn, the diluted solution La discharged from the absorber A is
One of them is diverged, and the other one is regenerated at high temperature with the entire amount of branching.
Bowl G ₃To the other side, and the other one recovers the entire amount of branching at the above intermediate temperature.
Bowl G₂Flow into the low temperature regenerator G₁Flowing into
Since it is configured to operate, the above-mentioned medium temperature regenerator G₂To
In this case, the unconcentrated dilute solution La flows in as it is.
Thus, for example, the high temperature regenerator G₃Condensed with heating concentrated in
Absorption solution as compared to the case where a collection solution (concentrated solution) is flowed in
The lower the concentration, the lower the boiling temperature.
This medium temperature regenerator G ₂Of boiling temperature of absorbing solution in water
The high temperature regenerator G that serves as the heat source₃In
Since the refrigerant vapor temperature can be set low,
The high temperature regenerator G proportional to the temperature of the refrigerant vapor₃Operating pressure
Can be set lower, resulting in lower operating pressure
It is possible to provide an absorption type refrigerating device with good operability.
It will be.

Further, the dilute solution La from the absorber A is branched so that a part of the dilute solution La flows into the high temperature regenerator G ₃ , so that, for example, the entire amount of the dilute solution La remains unchanged. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ ) is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system is improved.

[0329] Further, the absorber part thereof is branched dilute solution La from A by which so as to flow into the high-temperature regenerator G _3, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution L flowing in here is supplied.
As the amount of a decreases, the heat transfer area can be reduced to make the device compact, which in turn contributes to making the absorption refrigeration system compact.

Further, the absorption refrigerating apparatus Z _{10 of} this embodiment is also provided.
In this case, since the diluted solution La discharged from the absorber A is branched after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ is passed through the high temperature solution heat exchanger H ₃ immediately before it. And the dilute solution La flowing into the medium temperature regenerator G ₂ via the medium temperature solution heat exchanger H ₂ immediately before it.
Both flow into the low temperature solution heat exchanger H ₁ in a preheated state, and as a result, the required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ decreases, It is expected that the thermal efficiency of the entire system will improve.

Further, the absorption type refrigeration system Z _{10 of} this embodiment.
Then, the dilute solution L is generated by the residual heat Q after heating the high temperature regenerator G ₃ of the external heat source J for heating the high temperature regenerator G _3.
Since a is heated, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and further COP of the entire system can be expected to be further improved.

Furthermore, the absorption type refrigeration system Z of this embodiment.
In _10, since the arrangement to heat the dilute solution La by the low temperature regenerator G ₁ and the intermediate temperature regenerator steam drain Dr ₁ resulted in G _2, Dr _2, the steam drain Dr _1, Dr ₂
The heat retained by the can be effectively used for preheating the diluted solution La, and the thermal efficiency of the entire system can be further promoted.

Further, the absorption refrigerating apparatus Z _{10 of} this embodiment is also provided.
Then, in the absorption solution branch pipe 47 branched from the dilute solution pipe 21, the first and third drain heat exchangers D ₁ and D _{3 are}
And in the absorption solution branch pipe 48 branched from the second branch pipe 23, the second drain heat exchanger D
₂ , the diluted solution La is added to the vapor drains Dr ₁ and Dr, respectively.
Since configured to heat by ₂ can be preheated efficiently absorbing solution since the amount of absorption solution is less heated by the heat possessed the steam drain Dr _1, Dr _2.

Furthermore, the absorption type refrigeration system Z of this embodiment.
_{In 10} , the vapor drain Dr _{2 is connected} to the refrigerant drain pipe 3
4 side and the refrigerant drain pipe 36 side, and the dilute solution La is divided in each of the refrigerant drain pipes 34, 36.
The heating of the dilute solution La by the vapor drain Dr ₂ can be distributed with high heat, and the preheating effect on the dilute solution La is promoted.

Further, the absorption type refrigerating apparatus Z _{10 of} this embodiment.
Then, the system is configured by _three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ , but such a configuration requires a large number of regenerators. To increase the efficiency of the absorption solution by increasing the number of concentration stages of the absorption solution, and to increase the number of solution heat exchangers to increase the heat recovery rate, and the merit of improving the performance of the absorption refrigeration system, and the regenerator and When weighed against the disadvantage of increasing the manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. is there.

XI: Eleventh Embodiment FIG. 15 shows an operation cycle of an absorption type refrigeration system Z _{11 according to} an eleventh embodiment of the present invention. The absorption type refrigerating apparatus Z ₁₁ is an absorption type refrigerating apparatus which uses water as a refrigerant and lithium bromide as an absorbing liquid, and includes one condenser C, an absorber A, an evaporator E, and three pieces each. Solution heat exchanger H ₃ ,
H ₂ and H ₁ and regenerators G ₃ , G ₂ and G ₁ are the basic components, and in addition to this, two drain heat exchangers D ₁ and D ₂ and three exhaust heat exchangers K ₁ , K ₂ and K ₃ 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.

The evaporator E comprises a heat exchange section 7 for passing the liquid We to be cooled and a refrigerant sprayer (not shown) for spraying a refrigerant on the heat exchange section 7.

The absorber A comprises a solution sprayer (not shown) for spraying a concentrated solution, and a heat exchange section 8 for removing the absorption heat generated in the absorber A.

The condenser C comprises a heat exchange section 11.

Each of the regenerators G ₃ , G ₂ and G ₁ is for heating and concentrating the absorption solution containing the refrigerant to obtain a concentrated solution having a high concentration in sequence. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium temperature regenerator G ₂ (“low temperature side regenerator” in the claims) that is configured with a solution heating unit 14 through which an external heat source J (for example, combustion gas or steam) passes. G corresponds to _n-1 ") is configured with a solution heating unit 9, and most low-temperature regenerator G ₁ operating at a low temperature (corresponding to" the lowest temperature side of the regenerator G ₁ "in the claims Is provided with a solution heating unit 10.

The heat exchangers H ₁ , H ₂ and H ₃ are composed of the low temperature concentrated solution L ₁ , the medium temperature concentrated solution L ₂ and the high temperature concentrated solution produced by the regenerators G ₁ , G ₂ and G ₃ , respectively. It is for recovering the heat of each of L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types,
For example, a plate heat exchanger may be used.

The drain heat exchangers D ₁ and D ₂ are steam drains D produced by the low temperature regenerator G ₁ and the medium temperature regenerator G _2.
It recovers the heat of r ₁ and Dr ₂ to the dilute solution La side and is generally a shell-and-tube type heat exchanger, but is composed of another type such as a plate type heat exchanger. Is also good.

The exhaust heat exchangers K ₁ , K ₂ and K ₃ recover the heat of the residual heat Q of the external heat source J after heating the high temperature regenerator G ₃ to the dilute solution La side. Therefore, the shell-and-tube type heat exchanger is generally used, but it may be configured by another type, for example, a plate type heat exchanger.

Each of these devices is operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the condenser C and the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc produced in the condenser C is passed through the liquid refrigerant pipe 30 to the evaporator E side. Supplied. The liquid refrigerant Rc supplied to the evaporator E is sprayed from the refrigerant distributor to the heat exchange section 7 side.

From the liquid to be cooled inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We flowing in to and flowing out from the liquid to be cooled outlet pipe 46 is cooled by the heat of evaporation of the refrigerant. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

At the bottom of the absorber A, a solution pump LP
The dilute solution pipe 21 including is connected. After passing through the heated side of the low temperature solution heat exchanger H ₁ , the dilute solution pipe 21 is branched into two paths, a first branch pipe 22 and a second branch pipe 23. Then, the first branch pipe 22
Is connected to the high temperature regenerator G ₃ through the heated side of the high temperature solution heat exchanger H ₃ and further through the heated side of the high temperature exhaust heat exchanger K ₃ . In addition, the second branch pipe 2
3 is connected to the medium temperature regenerator G ₂ through the heated side of the medium temperature solution heat exchanger H ₂ and further through the heated side of the medium temperature exhaust heat exchanger K ₂ . Therefore, the dilute solution La flowing out from the absorber A can be used as the low temperature solution heat exchanger H.
It branches after passing through the heated side of ₁ , _one of which flows into the high temperature regenerator G ₃ through the high temperature solution heat exchanger H ₃ and the high temperature exhaust heat heat exchanger K ₃ , and the other of which is the medium temperature solution. It will flow into the intermediate temperature regenerator G ₂ via the heat exchanger H ₂ and the intermediate temperature exhaust heat exchanger K ₂ .

Further, in the dilute solution pipe 21, the low temperature solution heat exchanger H ₁ is bypassed and passes through the heated side of the first drain heat exchanger D ₁ to pass the low temperature solution heat exchanger H _1. An absorption solution branch pipe 47 for connecting the front and the rear of the is provided.
The second branch pipe 23 bypasses the medium temperature solution heat exchanger H ₂ and passes through the heated side of the second drain heat exchanger D ₂ before and after the medium temperature solution heat exchanger H ₂ . An absorption solution branch pipe 48 for connecting the above is provided.

The medium temperature solution pipe 26, which is connected to the medium temperature regenerator G ₂ and guides the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G ₂ , passes through the heating side of the medium temperature solution heat exchanger H _2. It is connected to the low temperature regenerator G ₁ .

High temperature regenerator G₃Connected to the high temperature re
Organ G₃High temperature concentrated solution L flowing out from₃The above high temperature melting
Liquid heat exchanger H₃High temperature solution pipe 27 passing through the heating side of
Low temperature regenerator G₁Connected to the low temperature regenerator G₁Spilled from
Low temperature concentrated solution L₁The low temperature solution pipe 25 that guides
To become the concentrated solution pipe 24, and the low temperature solution heat exchanger H ₁
Is connected to the absorber A through the heating side of.

The solution heating section 14 of the high temperature regenerator G ₃
The residual heat pipe 50 is connected to the outlet side of the. Then, the residual heat pipe 50, the high-temperature exhaust heat exchanger K ₃
Immediately before the above, the first residual heat branch pipe 51 and the second residual heat branch pipe 52 are branched, and the first residual heat branch pipe 51 passes through the heating side of the high temperature exhaust heat heat exchanger K ₃ . On the other hand, the second residual heat branch pipe 52 is further provided with a path passing through the heating side of the intermediate temperature exhaust heat heat exchanger K ₂ and a path passing through the heating side of the low temperature exhaust heat heat exchanger K _1. It is branched.

The air chamber side of the high temperature regenerator G ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is connected to the condenser C through the heating side of the second drain heat exchanger D _2. ing.

The solution heating unit 10 of the low temperature regenerator G ₁
The refrigerant drain pipe 35 connected to the outlet side of the
It is connected to the condenser C through the heating side of the drain heat exchanger D ₁ .

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The heat exchange section 8 of the absorber A and the heat exchange section 11 of the condenser C are connected via a cooling water pipe 42, and the cooling water W flowing in from the cooling water inlet pipe 41 side.
a performs a cooling action on the condenser C side,
Further, the absorber A side has a cooling effect and is discharged from the cooling water outlet pipe 43. Note that the cooling water Wa may have a structure in which the flow direction of the cooling water Wa is changed from the condenser to the absorber.

The absorption type refrigerating apparatus Z ₁₁ constitutes a circulation cycle of the refrigerant and the absorption solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₁₁ will be specifically described.

The dilute solution La fed from the absorber A by the solution pump LP is the low temperature solution heat exchanger H.
Branched in ₁ immediately preceding, cold solution L ₁ and the high-temperature regenerator G from the low temperature regenerator G ₁ portion thereof passing through the heating side by passing through the heated side of the low temperature solution heat exchanger H ₁ It is preheated by exchanging heat with the concentrated solution Lg formed by joining the high-temperature concentrated solution L ₃ from ₃ together. Also, another portion is preheated by steam drain Dr ₁ exchanges heat from the low temperature generator G ₁ through the heated side by passing through the first heated side of the drain heat exchanger D ₁ . The diluted solutions La that have been branched and individually preheated in this way are merged again, and then again the first branch pipe 2
The second side and the second branch pipe 23 side are branched.

The dilute solution La branched to the first branch pipe 22 side passes through the heated side of the high temperature solution heat exchanger H _{3 to} exchange heat with the high temperature solution L ₃ passing through the heated side. It is preheated and also the high temperature exhaust heat heat exchanger K
_After passing through the heated side of ₃ and preheated by exchanging heat with the residual heat Q of the external heat source J passing through the heated side, it flows into the high temperature regenerator G ₃ . Then, the dilute solution La flowing into the high temperature regenerator G ₃ is subjected to the heating and concentrating action of the external heat source J to become a high temperature concentrated solution L ₃ and flows out, so that the heating side of the high temperature solution heat exchanger H ₃ is discharged. Pass through.

On the other hand, the diluted solution La branched to the side of the second branch pipe 23 is further branched immediately before the medium temperature solution heat exchanger H _{2 and} a part of the diluted solution La is heated by the medium temperature solution heat exchanger H ₂ . The intermediate temperature regenerator G ₂ which passes through the heating side
It is preheated by exchanging heat with the medium temperature solution L ₂ from. The other part is preheated by exchanging heat with the steam drain Dr ₂ from the intermediate temperature regenerator G ₂ passing through the heated side of the second drain heat exchanger D ₂ and passing through the heated side. .

[0363] In this way, each branch is preheated individually.
The diluted solution La thus collected merges again, and is then discharged at the above-mentioned medium temperature.
Heat heat exchanger K₂By passing the heated side of
After being preheated by exchanging heat with the above-mentioned residual heat Q,
Organ G₂Flowing into the middle temperature regenerator G₂At the above high temperature
Organ G₃Refrigerant vapor R flowing into the solution heating unit 9 from the side₃
It is heated and concentrated by₂Becomes a spill
It This medium temperature regenerator G ₂Medium temperature concentrated solution L flowing out from₂Is
Medium temperature solution heat exchanger H₂After passing through the heating side of
The above low temperature exhaust heat heat exchanger K₁Above the low through the heated side of
Temperature regenerator G₁Flow into.

Further, the medium-temperature concentrated solution L ₂ flowing into the low-temperature regenerator G ₁ is a refrigerant vapor R ₂ flowing into the solution heating section 10 from the medium-temperature regenerator G ₂ side in the low-temperature regenerator G ₁ .
Is concentrated by heating to form a low temperature concentrated solution L ₁ and flows out.

[0365] Then, the joined the low temperature regenerator G ₁ cold concentrated solution L ₁ which flows from the high-temperature concentrated solution L ₃ flowing out from the high temperature generator G ₃ side, heating of the low-temperature solution heat exchanger H ₁ And flows into the absorber A side.

The absorption refrigeration system Z _{11 of} this embodiment has been described above.
In the operation cycle, the following unique action and effects are obtained.

Absorption refrigeration according to the eleventh embodiment
Device Z₁₁In, the diluted solution La discharged from the absorber A is
One of them is diverged, and the other one is regenerated at high temperature with the entire amount of branching.
Bowl G ₃To the other side, and the other one recovers the entire amount of branching at the above intermediate temperature.
Bowl G₂Flow into the low temperature regenerator G₁Flowing into
Since it is configured to operate, the above-mentioned medium temperature regenerator G₂To
In this case, the unconcentrated dilute solution La flows in as it is.
Thus, for example, the high temperature regenerator G₃Condensed with heating concentrated in
Absorption solution as compared to the case where a collection solution (concentrated solution) is flowed in
The lower the concentration, the lower the boiling temperature.
This medium temperature regenerator G ₂Of boiling temperature of absorbing solution in water
The high temperature regenerator G that serves as the heat source₃In
Since the refrigerant vapor temperature can be set low,
The high temperature regenerator G proportional to the temperature of the refrigerant vapor₃Operating pressure
Can be set lower, resulting in lower operating pressure
It is possible to provide an absorption type refrigerating device with good operability.
It will be.

Further, the dilute solution La from the absorber A is branched so that a part of the dilute solution La is made to flow into the high temperature regenerator G ₃ , so that, for example, the entire amount of the dilute solution La remains as it is. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ ) is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system is improved.

[0369] Further, the absorber part thereof is branched dilute solution La from A by which so as to flow into the high-temperature regenerator G _3, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution L flowing in here is supplied.
As the amount of a decreases, the heat transfer area can be reduced to make the device compact, which in turn contributes to making the absorption refrigeration system compact.

Further, the absorption type refrigerating apparatus Z _{11 of} this embodiment.
In this case, since the diluted solution La discharged from the absorber A is branched after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ is passed through the high temperature solution heat exchanger H ₃ immediately before it. And the dilute solution La flowing into the medium temperature regenerator G ₂ via the medium temperature solution heat exchanger H ₂ immediately before it.
Both flow into the low temperature solution heat exchanger H ₁ in a preheated state, and as a result, the required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ decreases, It is expected that the thermal efficiency of the entire system will improve.

Further, the absorption type refrigerating apparatus Z _{11 of} this embodiment.
Then, the dilute solution L is generated by the residual heat Q after heating the high temperature regenerator G ₃ of the external heat source J for heating the high temperature regenerator G _3.
Since a is heated, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and further COP of the entire system can be expected to be further improved.

Furthermore, the absorption type refrigeration system Z of this embodiment.
_{In 11} , the residual heat pipe 50 of the residual heat Q is branched into a first residual heat branch pipe 51 and a second residual heat branch pipe 52, and the diluted solution La is heated in each of the residual heat branch pipes 51 and 52. Therefore, the heat having the high residual heat Q can be distributed to the dilute solution La, and the preheating effect on the absorbing solution is promoted.

Further, the absorption type refrigeration system Z of this embodiment.
In _11, since the arrangement to heat the dilute solution La by the low temperature regenerator G ₁ and the intermediate temperature regenerator steam drain Dr ₁ resulted in G _2, Dr _2, the steam drain Dr _1, Dr ₂
The heat retained by the can be effectively used for preheating the diluted solution La, and the thermal efficiency of the entire system can be further promoted.

Further, the absorption type refrigerating apparatus Z _{11 of} this embodiment.
Then, in the absorbing solution branch pipe 47 branched from the dilute solution pipe 21, the first drain heat exchanger D ₁ and in the absorbing solution branch pipe 48 branched from the second branch pipe 23, the second drain heat exchanger is exchanged. Since the dilute solution La is heated in the vessel D ₂ by the vapor drains Dr ₁ and Dr ₂ , respectively, the vapor drains Dr ₁ and
Since the amount of the absorbing solution heated by the retained heat of Dr ₂ is small, the absorbing solution can be efficiently preheated.

Furthermore, the absorption type refrigeration system Z of this embodiment.
₁₁Then, three regenerators G₁, G₂, G ₃And three solution heat exchange
Exchanger H₁, H₂, H₃The system is made up of
In the configuration, the number of regenerators is increased to increase the number of absorption solution concentration stages.
Increase the heat efficiency and increase the number of solution heat exchangers.
Absorption refrigeration system by increasing the heat recovery rate
Of the regenerator and solution heat
The increase in manufacturing costs due to the increase in the number of exchangers
If you weigh the disadvantages, the absorption refrigeration system
Considered optimal for achieving both performance and cost
And is extremely useful in practice.

XII: Twelfth Embodiment FIG. 16 shows an operation cycle of an absorption refrigeration system Z _{12 according to} a twelfth embodiment of the present invention. The absorption type refrigerating apparatus Z ₁₂ is an absorption type refrigerating apparatus which uses water as a refrigerant and lithium bromide as an absorbing liquid, and includes one condenser C, an absorber A, an evaporator E, and three pieces each. Solution heat exchanger H ₃ ,
H ₂ and H ₁ and regenerators G ₃ , G ₂ and G ₁ are the basic components, and in addition to this, two drain heat exchangers D ₁ and D ₂ and two exhaust heat exchangers K ₂ and K _3, and these devices are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E comprises a heat exchange section 7 for passing the liquid We to be cooled, and a refrigerant distributor (not shown) for distributing the refrigerant on the heat exchange section 7.

The absorber A comprises a solution sprayer (not shown) for spraying a concentrated solution, and a heat exchange section 8 for removing the absorption heat generated in the absorber A.

The condenser C comprises a heat exchange section 11.

Each of the regenerators G ₃ , G ₂ and G ₁ is for heating and concentrating the absorbing solution containing the refrigerant to obtain a concentrated solution having a high concentration in sequence. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium temperature regenerator G ₂ (“low temperature side regenerator” in the claims) that is configured with a solution heating unit 14 through which an external heat source J (for example, combustion gas or steam) passes. G corresponds to _n-1 ") is configured with a solution heating unit 9, and most low-temperature regenerator G ₁ operating at a low temperature (corresponding to" the lowest temperature side of the regenerator G ₁ "in the claims Is provided with a solution heating unit 10.

Each of the heat exchangers H ₁ , H ₂ , and H ₃ has a low-temperature concentrated solution L ₁ , a medium-temperature concentrated solution L ₂ , and a high-temperature concentrated solution produced by the regenerators G ₁ , G ₂ , and G _3. It is for recovering the heat of each of L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types,
For example, a plate heat exchanger may be used.

The drain heat exchangers D ₁ and D ₂ are steam drains D produced by the low temperature regenerator G ₁ and the medium temperature regenerator G _2.
It recovers the heat of r ₁ and Dr ₂ to the dilute solution La side and is generally a shell-and-tube type heat exchanger, but is composed of another type such as a plate type heat exchanger. Is also good.

The exhaust heat exchangers K ₂ and K ₃ recover the heat of the residual heat Q of the external heat source J after heating the high temperature regenerator G ₃ to the dilute solution La side. Generally, it is a shell-and-tube type heat exchanger, but it may be configured by another type, for example, a plate type heat exchanger.

Each of these devices is operatively connected by a solution piping system and a refrigerant piping system as follows.

That is, the condenser C and the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30 to the evaporator E side. Supplied. The liquid refrigerant Rc supplied to the evaporator E is sprayed from the refrigerant distributor to the heat exchange section 7 side.

From the liquid-to-be-cooled inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We flowing in to and flowing out from the liquid to be cooled outlet pipe 46 is cooled by the heat of evaporation of the refrigerant. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

At the bottom of the absorber A, a solution pump LP
The dilute solution pipe 21 including is connected. After passing through the heated side of the low temperature solution heat exchanger H ₁ , the dilute solution pipe 21 is branched into two paths, a first branch pipe 22 and a second branch pipe 23. Then, the first branch pipe 22
Is connected to the high temperature regenerator G ₃ through the heated side of the high temperature solution heat exchanger H ₃ and further through the heated side of the high temperature exhaust heat exchanger K ₃ . In addition, the second branch pipe 2
3 is connected to the medium temperature regenerator G ₂ through the heated side of the medium temperature solution heat exchanger H ₂ . Therefore, the dilute solution La flowing out from the absorber A branches after passing through the heated side of the low temperature solution heat exchanger H ₁ , one of which is the high temperature solution heat exchanger H ₃ and the high temperature exhaust heat heat exchange. It flows into the high temperature regenerator G ₃ via the device K ₃ , and the other flows into the intermediate temperature regenerator G ₂ via the medium temperature solution heat exchanger H ₂ .

Furthermore, in the dilute solution pipe 21, the low temperature solution heat exchanger H ₁ is bypassed and passes through the heated side of the first drain heat exchanger D ₁ to pass the low temperature solution heat exchanger H _1. An absorption solution branch pipe 47 for connecting the front and the rear of the is provided.
Further, in the second branch pipe 23, the medium temperature solution heat exchanger H ₂ is bypassed and the heated side of the second drain heat exchanger D _{2 and} the heated side of the medium temperature exhaust heat exchanger K ₂ are heated. An absorption solution branch pipe 48 is provided to connect the front and rear of the medium temperature solution heat exchanger H ₂ through the pipe.

The medium temperature solution pipe 26, which is connected to the medium temperature regenerator G ₂ and guides the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G ₂ , passes through the heating side of the medium temperature solution heat exchanger H _2. It is connected to the low temperature regenerator G ₁ .

[0390] lead to hot concentrated solution L ₃ to flow out connected to the high-temperature regenerator G ₃ from the high temperature regenerator G _3, the hot solution pipe 27 through the heating side of the high-temperature solution heat exchanger H _3, the low temperature cold concentrated low temperature solution pipe 25 for guiding the solution L ₁ is merged to the concentrated solution pipe 24, and the heating of the low-temperature solution heat exchanger H ₁ flowing out is connected to the regenerator G ₁ and from the cold regenerator G ₁ It is connected to the absorber A through the side.

The solution heating section 14 of the high temperature regenerator G ₃
The residual heat pipe 50 is connected to the outlet side of the. Then, the residual heat pipe 50, the high-temperature exhaust heat exchanger K ₃
Immediately before the above, the first residual heat branch pipe 51 and the second residual heat branch pipe 52 are branched, and the first residual heat branch pipe 51 passes through the heating side of the high temperature exhaust heat heat exchanger K ₃ . On the other hand, the second residual heat branch pipe 52 passes through the heating side of the intermediate temperature exhaust heat heat exchanger K ₂ .

The air chamber side of the high temperature regenerator G ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is connected to the condenser C through the heating side of the second drain heat exchanger D _2. ing.

[0395] The solution heating unit 10 of the low temperature regenerator G ₁
The refrigerant drain pipe 35 connected to the outlet side of the
It is connected to the condenser C through the heating side of the drain heat exchanger D ₁ .

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The heat exchange section 8 of the absorber A and the heat exchange section 11 of the condenser C are connected via a cooling water pipe 42, and the cooling water W flowing from the cooling water inlet pipe 41 side.
a performs a cooling action on the absorber A side,
Further, the condenser C side has a cooling function and is discharged from the cooling water outlet pipe 43. Note that the cooling water Wa may have a structure in which the flow direction of the cooling water Wa is changed from the condenser to the absorber.

The absorption type refrigerating apparatus Z ₁₂ constitutes a circulation cycle of the refrigerant and the absorption solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₁₂ will be specifically described.

The dilute solution La fed from the absorber A by the solution pump LP is the low temperature solution heat exchanger H.
Branched in ₁ immediately preceding, cold solution L ₁ and the high-temperature regenerator G from the low temperature regenerator G ₁ portion thereof passing through the heating side by passing through the heated side of the low temperature solution heat exchanger H ₁ It is preheated by exchanging heat with the concentrated solution Lg formed by joining the high-temperature concentrated solution L ₃ from ₃ together. Also, another portion is preheated by steam drain Dr ₁ exchanges heat from the low temperature generator G ₁ through the heated side by passing through the first heated side of the drain heat exchanger D ₁ . The diluted solutions La that have been branched and individually preheated in this way are merged again, and then again the first branch pipe 2
The second side and the second branch pipe 23 side are branched.

The dilute solution La branched to the first branch pipe 22 side passes through the heated side of the high temperature solution heat exchanger H _{3 to} exchange heat with the high temperature solution L ₃ passing through the heated side. It is preheated and also the high temperature exhaust heat heat exchanger K
_After passing through the heated side of ₃ and preheated by exchanging heat with the residual heat Q of the external heat source J passing through the heated side, it flows into the high temperature regenerator G ₃ . Then, the dilute solution La flowing into the high temperature regenerator G ₃ is subjected to the heating concentration effect by the external heat source J, becomes a concentrated solution and flows out, and passes through the heating side of the high temperature solution heat exchanger H ₃ .

On the other hand, the dilute solution La branched to the side of the second branch pipe 23 is further branched immediately before the medium temperature solution heat exchanger H _{2 and} a part of the diluted solution La is heated by the medium temperature solution heat exchanger H ₂ . The intermediate temperature regenerator G ₂ which passes through the heating side
It is preheated by exchanging heat with the medium temperature solution L ₂ from. A part of the other part exchanges heat with the steam drain Dr ₂ from the intermediate temperature regenerator G ₂ passing through the heated side of the second drain heat exchanger D ₂ and passes through the heated side of the second drain heat exchanger D _2. By passing through the heated side of the exhaust heat exchanger K ₂ , it is preheated by exchanging heat with the residual heat Q passing through the heated side.

[0403] Thus branches to dilute solution La preheated individually merges again flows into the intermediate temperature regenerator G _2, the from the high temperature generator G ₃ side in middle temperature regenerator G ₂ It is heated and concentrated by the refrigerant vapor R ₃ flowing into the solution heating section 9, and flows out as a medium-temperature concentrated solution L ₂ . The medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G ₂ passes through the heating side of the medium temperature solution heat exchanger H ₂ and then flows into the low temperature regenerator G ₁ .

Further, the medium temperature concentrated solution L _{2 which} has flowed into the low temperature regenerator G ₁ is a refrigerant vapor R ₂ which flows into the solution heating section 10 from the medium temperature regenerator G ₂ side in the low temperature regenerator G ₁ .
Is concentrated by heating to form a low temperature concentrated solution L ₁ and flows out.

[0405] Then, the joined the low temperature regenerator G ₁ cold concentrated solution L ₁ which flows from the high-temperature concentrated solution L ₃ flowing out from the high temperature generator G ₃ side, heating of the low-temperature solution heat exchanger H ₁ And flows into the absorber A side.

The above is the absorption refrigeration apparatus Z _{12 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

Absorption-type refrigeration according to the twelfth embodiment
Device Z₁₂In, the diluted solution La discharged from the absorber A is
One of them is diverged, and the other one is regenerated at high temperature with the entire amount of branching.
Bowl G ₃To the other side, and the other one recovers the entire amount of branching at the above intermediate temperature.
Bowl G₂Flow into the low temperature regenerator G₁Flowing into
Since it is configured to operate, the above-mentioned medium temperature regenerator G₂To
In this case, the unconcentrated dilute solution La flows in as it is.
Thus, for example, the high temperature regenerator G₃Condensed with heating concentrated in
Absorption solution as compared to the case where a collection solution (concentrated solution) is flowed in
The lower the concentration, the lower the boiling temperature.
This medium temperature regenerator G ₂Of boiling temperature of absorbing solution in water
The high temperature regenerator G that serves as the heat source₃In
Since the refrigerant vapor temperature can be set low,
The high temperature regenerator G proportional to the temperature of the refrigerant vapor₃Operating pressure
Can be set lower, resulting in lower operating pressure
It is possible to provide an absorption type refrigerating device with good operability.
It will be.

Further, the dilute solution La from the absorber A is branched so that a part of the dilute solution La is made to flow into the high temperature regenerator G ₃ , so that, for example, the entire amount of the dilute solution La remains unchanged. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ ) is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system is improved.

[0409] Further, the absorber part thereof is branched dilute solution La from A by which so as to flow into the high-temperature regenerator G _3, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution L flowing in here is supplied.
As the amount of a decreases, the heat transfer area can be reduced to make the device compact, which in turn contributes to making the absorption refrigeration system compact.

Further, the absorption type refrigerating apparatus Z _{12 of} this embodiment.
In this case, since the diluted solution La discharged from the absorber A is branched after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ is passed through the high temperature solution heat exchanger H ₃ immediately before it. And the dilute solution La flowing into the medium temperature regenerator G ₂ via the medium temperature solution heat exchanger H ₂ immediately before it.
Both flow into the low temperature solution heat exchanger H ₁ in a preheated state, and as a result, the required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ decreases, It is expected that the thermal efficiency of the entire system will improve.

Further, the absorption type refrigerating apparatus Z _{12 of} this embodiment.
Then, the dilute solution L is generated by the residual heat Q after heating the high temperature regenerator G ₃ of the external heat source J for heating the high temperature regenerator G _3.
Since a is heated, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and further COP of the entire system can be expected to be further improved.

Furthermore, the absorption type refrigeration system Z of this embodiment.
In _12, since the arrangement to heat the dilute solution La by the low temperature regenerator G ₁ and the intermediate temperature regenerator steam drain Dr ₁ resulted in G _2, Dr _2, the steam drain Dr _1, Dr ₂
The heat retained by the can be effectively used for preheating the diluted solution La, and the thermal efficiency of the entire system can be further promoted.

Further, the absorption type refrigerating apparatus Z _{12 of} this embodiment.
Then, in the absorbing solution branch pipe 47 branched from the dilute solution pipe 21, the first drain heat exchanger D ₁ and in the absorbing solution branch pipe 48 branched from the second branch pipe 23, the second drain heat exchanger is exchanged. Since the dilute solution La is heated in the vessel D ₂ by the vapor drains Dr ₁ and Dr ₂ , respectively, the vapor drains Dr ₁ and
Since the amount of the absorbing solution heated by the retained heat of Dr ₂ is small, the absorbing solution can be efficiently preheated.

Furthermore, the absorption type refrigeration system Z of this embodiment.
_{At 12} , the residual heat pipe 50 of the residual heat Q is branched into a first residual heat branch pipe 51 and a second residual heat branch pipe 52, and the dilute solution La absorbing solution is respectively applied to the residual heat branch pipes 51 and 52. Since the above heating is performed, the heat with the high residual heat Q can be distributed to the dilute solution La, and the preheating effect on the absorbing solution is promoted.

Further, the absorption type refrigerating apparatus Z _{12 of} this embodiment.
Then, the system is configured by _three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ , but such a configuration requires a large number of regenerators. To increase the efficiency of the absorption solution by increasing the number of concentration stages of the absorption solution, and to increase the number of solution heat exchangers to increase the heat recovery rate, and the merit of improving the performance of the absorption refrigeration system, and the regenerator and When weighed against the disadvantage of increasing the manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. is there.

XIII: Thirteenth Embodiment FIG. 17 shows an operation cycle of the absorption refrigeration system Z _{13 according} to the thirteenth embodiment of the present invention. This absorption type refrigeration system Z ₁₃ is an absorption type refrigeration system which uses water as a refrigerant and lithium bromide as an absorption liquid, and includes one condenser C, an absorber A, an evaporator E, and three each. Solution heat exchanger H ₃ ,
H ₂ and H ₁ and regenerators G ₃ , G ₂ and G ₁ are the basic components, and in addition to this, two drain heat exchangers D ₁ and D ₂ and three exhaust heat exchangers K ₁ , K ₂ and K ₃ 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.

The evaporator E comprises a heat exchange section 7 for passing the liquid We to be cooled and a refrigerant distributor (not shown) for distributing the refrigerant on the heat exchange section 7.

The absorber A comprises a solution sprayer (not shown) for spraying a concentrated solution, and a heat exchange section 8 for removing the absorption heat generated in the absorber A.

The condenser C comprises a heat exchange section 11.

Each of the regenerators G ₃ , G ₂ and G ₁ is for heating and concentrating the absorption solution containing the refrigerant to obtain a concentrated solution having a high concentration in sequence. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium temperature regenerator G ₂ (“low temperature side regenerator” in the claims) that is configured with a solution heating unit 14 through which an external heat source J (for example, combustion gas or steam) passes. G corresponds to _n-1 ") is configured with a solution heating unit 9, and most low-temperature regenerator G ₁ operating at a low temperature (corresponding to" the lowest temperature side of the regenerator G ₁ "in the claims Is provided with a solution heating unit 10.

Each of the heat exchangers H ₁ , H ₂ , and H ₃ has a low-temperature concentrated solution L ₁ , a medium-temperature concentrated solution L ₂ , and a high-temperature concentrated solution produced by the regenerators G ₁ , G ₂ , and G _3. It is for recovering the heat of each of L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types,
For example, a plate heat exchanger may be used.

The respective drain heat exchangers D ₁ and D ₂ are vapor drains D produced by the low temperature regenerator G ₁ and the medium temperature regenerator G _2.
It recovers the heat of r ₁ and Dr ₂ to the dilute solution La side and is generally a shell-and-tube type heat exchanger, but is composed of another type such as a plate type heat exchanger. Is also good.

The exhaust heat exchangers K ₁ , K ₂ and K ₃ recover the heat of the residual heat Q of the external heat source J after heating the high temperature regenerator G ₃ to the dilute solution La side. Therefore, the shell-and-tube type heat exchanger is generally used, but it may be configured by another type, for example, a plate type heat exchanger.

Each of these devices is operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the condenser C and the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is transferred to the evaporator E side via the liquid refrigerant pipe 30. Supplied. The liquid refrigerant Rc supplied to the evaporator E is sprayed from the refrigerant distributor to the heat exchange section 7 side.

From the liquid to be cooled inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We flowing in to and flowing out from the liquid to be cooled outlet pipe 46 is cooled by the heat of evaporation of the refrigerant. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

At the bottom of the absorber A, a solution pump LP
The dilute solution pipe 21 including is connected. After passing through the heated side of the low temperature solution heat exchanger H ₁ , the dilute solution pipe 21 is branched into two paths, a first branch pipe 22 and a second branch pipe 23. Then, the first branch pipe 22
Is connected to the high temperature regenerator G ₃ through the heated side of the high temperature solution heat exchanger H ₃ and further through the heated side of the high temperature exhaust heat exchanger K ₃ . In addition, the second branch pipe 2
3 is connected to the medium temperature regenerator G ₂ through the heated side of the medium temperature solution heat exchanger H ₂ and further through the heated side of the medium temperature exhaust heat exchanger K ₂ . Therefore, the dilute solution La flowing out from the absorber A can be used as the low temperature solution heat exchanger H.
It branches after passing through the heated side of ₁ , _one of which flows into the high temperature regenerator G ₃ through the high temperature solution heat exchanger H ₃ and the high temperature exhaust heat heat exchanger K ₃ , and the other of which is the medium temperature solution. It will flow into the intermediate temperature regenerator G ₂ via the heat exchanger H ₂ and the intermediate temperature exhaust heat exchanger K ₂ .

Furthermore, the dilute solution pipe 21 bypasses the low temperature solution heat exchanger H ₁ and passes through the heated side of the first drain heat exchanger D ₁ to pass through the low temperature solution heat exchanger H ₁ . An absorption solution branch pipe 47 that connects the front and rear is provided. The second branch pipe 23 bypasses the medium temperature solution heat exchanger H ₂ and passes through the heated side of the second drain heat exchanger D ₂ before and after the medium temperature solution heat exchanger H ₂ . An absorption solution branch pipe 48 for connecting the above is provided.

[0429] medium-temperature solution pipe 2 for guiding the medium temperature concentrated solution L ₂ which flows from the intermediate temperature regenerator middle temperature regenerator G ₂ is connected to G ₂
6 is connected to the low temperature regenerator G ₁ through the heating side of the medium temperature solution heat exchanger H ₂ and further through the heated side of the low temperature exhaust heat exchanger K ₁ .

The above high temperature regenerator G₃Connected to the high temperature re
Organ G₃High temperature concentrated solution L flowing out from₃The above high temperature melting
Liquid heat exchanger H₃High temperature solution pipe 27 passing through the heating side of
Low temperature regenerator G₁Connected to the low temperature regenerator G₁Spilled from
Low temperature concentrated solution L₁The low temperature solution pipe 25 that guides
To become the concentrated solution pipe 24, and the low temperature solution heat exchanger H ₁
Is connected to the absorber A through the heating side of.

The solution heating section 14 of the high temperature regenerator G ₃
The residual heat pipe 50 is connected to the outlet side of the. Then, the residual heat pipe 50, the high-temperature exhaust heat exchanger K ₃
Of the intermediate temperature exhaust heat exchanger K _{2 and} the heating side of the low temperature exhaust heat exchanger K ₁ sequentially.

The air chamber side of the high temperature regenerator G ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is connected to the condenser C through the heating side of the second drain heat exchanger D _2. ing.

[0435] The solution heating unit 10 of the low temperature regenerator G ₁
The refrigerant drain pipe 35 connected to the outlet side of the
It is connected to the condenser C through the heating side of the drain heat exchanger D ₁ .

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The heat exchange section 8 of the absorber A and the heat exchange section 11 of the condenser C are connected via a cooling water pipe 42, and the cooling water W flowing in from the cooling water inlet pipe 41 side.
a performs a cooling action on the absorber A side,
Further, the condenser C side has a cooling function and is discharged from the cooling water outlet pipe 43. Note that the cooling water Wa may have a structure in which the flow direction of the cooling water Wa is changed from the condenser to the absorber.

The absorption refrigeration system Z ₁₃ constitutes a circulation cycle of the refrigerant and the absorption solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₁₃ will be specifically described.

The dilute solution La fed from the absorber A by the solution pump LP is the low temperature solution heat exchanger H.
Branched in ₁ immediately preceding, cold solution L ₁ and the high-temperature regenerator G from the low temperature regenerator G ₁ portion thereof passing through the heating side by passing through the heated side of the low temperature solution heat exchanger H ₁ It is preheated by exchanging heat with the concentrated solution Lg formed by joining the high-temperature concentrated solution L ₃ from ₃ together. Also, another portion is preheated by steam drain Dr ₁ exchanges heat from the low temperature generator G ₁ through the heated side by passing through the first heated side of the drain heat exchanger D ₁ . The diluted solutions La that have been branched and individually preheated in this way are merged again, and then again the first branch pipe 2
The second side and the second branch pipe 23 side are branched.

The dilute solution La branched to the first branch pipe 22 side passes through the heated side of the high temperature solution heat exchanger H _{3 to} exchange heat with the high temperature solution L ₃ passing through the heated side. It is preheated and also the high temperature exhaust heat heat exchanger K
_After passing through the heated side of ₃ and preheated by exchanging heat with the residual heat Q of the external heat source J passing through the heated side, it flows into the high temperature regenerator G ₃ . Then, the dilute solution La flowing into the high temperature regenerator G ₃ is subjected to the heating and concentrating action of the external heat source J to become a high temperature concentrated solution L ₃ and flows out, so that the heating side of the high temperature solution heat exchanger H ₃ is discharged. Pass through.

On the other hand, the dilute solution La branched to the side of the second branch pipe 23 is further branched immediately before the medium temperature solution heat exchanger H _{2 and} a part of the diluted solution La is heated by the medium temperature solution heat exchanger H ₂ . The intermediate temperature regenerator G ₂ which passes through the heating side
It is preheated by exchanging heat with the medium temperature solution L ₂ from. The other part is preheated by exchanging heat with the steam drain Dr ₂ from the intermediate temperature regenerator G ₂ passing through the heated side of the second drain heat exchanger D ₂ and passing through the heated side. .

[0443] In this way, the branches are preheated individually.
The diluted solution La thus collected merges again, and is then discharged at the above-mentioned medium temperature.
Heat heat exchanger K₂By passing the heated side of
After being preheated by exchanging heat with the above-mentioned residual heat Q,
Organ G₂Flowing into the middle temperature regenerator G₂At the above high temperature
Organ G₃Refrigerant vapor R flowing into the solution heating unit 9 from the side₃
It is heated and concentrated by₂Becomes a spill
It This medium temperature regenerator G ₂Medium temperature concentrated solution L flowing out from₂Is
Medium temperature solution heat exchanger H₂After passing through the heating side of
The above low temperature exhaust heat heat exchanger K₁Above the low through the heated side of
Temperature regenerator G₁Flow into.

Further, the medium temperature concentrated solution L ₂ flowing into the low temperature regenerator G ₁ is a refrigerant vapor R ₂ flowing into the solution heating section 10 from the medium temperature regenerator G ₂ side in the low temperature regenerator G ₁ .
Is concentrated by heating to form a low temperature concentrated solution L ₁ and flows out.

[0445] Then, the joined the low temperature regenerator G ₁ cold concentrated solution L ₁ which flows from the high-temperature concentrated solution L ₃ flowing out from the high temperature generator G ₃ side, heating of the low-temperature solution heat exchanger H ₁ And flows into the absorber A side.

The absorption refrigeration system Z _{13 of} this embodiment has been described above.
In the operation cycle, the following unique action and effects are obtained.

Absorption refrigeration according to the thirteenth embodiment
Device Z₁₃In, the diluted solution La discharged from the absorber A is
One of them is diverged, and the other one is regenerated at high temperature with the entire amount of branching.
Bowl G ₃To the other side, and the other one recovers the entire amount of branching at the above intermediate temperature.
Bowl G₂Flow into the low temperature regenerator G₁Flowing into
Since it is configured to operate, the above-mentioned medium temperature regenerator G₂To
In this case, the unconcentrated dilute solution La flows in as it is.
Thus, for example, the high temperature regenerator G₃Condensed with heating concentrated in
Absorption solution as compared to the case where a collection solution (concentrated solution) is flowed in
The lower the concentration, the lower the boiling temperature.
This medium temperature regenerator G ₂Of boiling temperature of absorbing solution in water
The high temperature regenerator G that serves as the heat source₃In
Since the refrigerant vapor temperature can be set low,
The high temperature regenerator G proportional to the temperature of the refrigerant vapor₃Operating pressure
Can be set lower, resulting in lower operating pressure
It is possible to provide an absorption type refrigerating device with good operability.
It will be.

Further, since the dilute solution La from the absorber A is branched so that a part of the dilute solution La flows into the high temperature regenerator G ₃ , for example, the entire amount of the dilute solution La remains as it is. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ ) is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system is improved.

[0449] Further, the absorber part thereof is branched dilute solution La from A by which so as to flow into the high-temperature regenerator G _3, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution L flowing in here is supplied.
As the amount of a decreases, the heat transfer area can be reduced to make the device compact, which in turn contributes to making the absorption refrigeration system compact.

Also, the absorption refrigerating apparatus Z _{13 of} this embodiment is used.
In high-temperature concentrated solution L ₃ from the high temperature generator G ₃ are branched after passing through the heating side of the solution heat exchanger H _3, partially with the medium-temperature concentrated solution L ₂ from the intermediate temperature regenerator G ₂ since configured to flow into the low temperature regenerator G _1, but the fact that the hot concentrated solution L ₃ from the high-temperature regenerator G ₃ and concentrated solution L ₁ from the low temperature regenerator G ₁ is merged, By letting a part of the high temperature concentrated solution L ₃ flow into the low temperature regenerator G ₁ ,
The flow rate ratio between the high-temperature concentrated solution L ₃ and the low-temperature concentrated solution L ₁ before merging is reduced, and the pressure difference when the concentrated solutions L ₃ and L ₁ are merged is improved, and the merging of the solutions is smoothly performed. be able to.

Further, the absorption refrigerating apparatus Z _{13 of} this embodiment is also provided.
In this case, since the diluted solution La discharged from the absorber A is branched after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ is passed through the high temperature solution heat exchanger H ₃ immediately before it. And the dilute solution La flowing into the medium temperature regenerator G ₂ via the medium temperature solution heat exchanger H ₂ immediately before it.
Both flow into the low temperature solution heat exchanger H ₁ in a preheated state, and as a result, the required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ decreases, It is expected that the thermal efficiency of the entire system will improve.

Further, the absorption refrigerating apparatus Z _{13 of} this embodiment is also provided.
Then, the dilute solution L is generated by the residual heat Q after heating the high temperature regenerator G ₃ of the external heat source J for heating the high temperature regenerator G _3.
Since a is heated, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and further COP of the entire system can be expected to be further improved.

Furthermore, the absorption type refrigeration system Z of this embodiment.
_{In 13} , the dilute solution La is multi-staged by the residual heat Q,
That is, since the residual heat Q is configured to be heated in series in the flow direction, the dilute solutions L that are heat-exchanged with each other.
The temperature difference between a and the residual heat Q is equalized as much as possible at each heating position, the heat recovery efficiency of the entire system is improved, and further improvement of the thermal efficiency of the absorption refrigeration system can be expected.

Furthermore, the absorption type refrigeration system Z of this embodiment.
In _13, since the arrangement to heat the dilute solution La by the low temperature regenerator G ₁ and the intermediate temperature regenerator steam drain Dr ₁ resulted in G _2, Dr _2, the steam drain Dr _1, Dr ₂
The heat retained by the can be effectively used for preheating the diluted solution La, and the thermal efficiency of the entire system can be further promoted.

Further, the absorption type refrigeration system Z _{13 of} this embodiment.
Then, in the absorbing solution branch pipe 47 branched from the dilute solution pipe 21, the first drain heat exchanger D ₁ and in the absorbing solution branch pipe 48 branched from the second branch pipe 23, the second drain heat exchanger is exchanged. Since the dilute solution La is heated in the vessel D ₂ by the vapor drains Dr ₁ and Dr ₂ , respectively, the vapor drains Dr ₁ and
Since the amount of the absorbing solution heated by the retained heat of Dr ₂ is small, the absorbing solution can be efficiently preheated.

Further, the absorption type refrigerating apparatus Z _{13 of} this embodiment.
Then, the system is configured by _three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ , but such a configuration requires a large number of regenerators. To increase the efficiency of the absorption solution by increasing the number of concentration stages of the absorption solution, and to increase the number of solution heat exchangers to increase the heat recovery rate, and the merit of improving the performance of the absorption refrigeration system, and the regenerator and When weighed against the disadvantage of increasing the manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. is there.

The embodiments described above are those disclosed in the above specification and drawings. The newly added embodiment will be described below.

XIV: Fourteenth Embodiment FIG. 18 shows an operation cycle of the absorption refrigerating apparatus Z _{14 according} to the fourteenth embodiment of the present invention. The absorption type refrigerating apparatus Z ₁₄ is an absorption type refrigerating apparatus which uses water as a refrigerant and lithium bromide as an absorbing liquid, and includes one condenser C, an absorber A, an evaporator E, and three pieces each. Solution heat exchanger H ₃ ,
The H ₂ and H ₁ and the regenerators G ₃ , G ₂ and G ₁ are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E is provided with a heat exchange section 7 for passing the liquid We to be cooled and a refrigerant sprayer 13 for spraying the refrigerant Re on the heat exchange section 7 in the container 1.

In the above-mentioned absorber A, the container 2 is filled with the concentrated solution Lg.
And a heat exchange section 8 for removing absorption heat generated in the absorber A. The condenser C is configured by including the heat exchange section 11 in the container 6.

Each of the regenerators G ₃ , G ₂ , and G ₁ is for heating and concentrating the absorption solution containing the refrigerant to obtain a concentrated solution having a high concentration in sequence. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium-temperature regenerator G ₂ that operates at a medium temperature and is configured to have an external heat source J (for example, combustion gas or steam) inside the container 3 (the “low-temperature side regenerator G _n in the claims”). _-1 "
Applicable) to is configured with a solution heating unit 9 in the container 4, corresponding to the even most low temperature regenerator G ₁ ( "lowest temperature side of the regenerator G _1" in the claims which operates at a low temperature )
Is provided with a solution heating unit 10 in the container 5.

Each of the heat exchangers H ₁ , H ₂ , and H ₃ has a low-temperature concentrated solution L ₁ , a medium-temperature concentrated solution L ₂ , and a high-temperature concentrated solution produced by the regenerators G ₁ , G ₂ , and G _3. It is for recovering the heat of each L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types,
For example, it is composed of a plate heat exchanger.

Each of these devices is operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the container 6 of the condenser C and the container 1 of the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30. It is supplied to the evaporator E side. Further, the liquid refrigerant Rc supplied to the evaporator E is the refrigerant pump RP.
Is pumped up to the refrigerant sprayer 13 through the liquid refrigerant pipe 29, and is sprayed as the refrigerant Re from the refrigerant sprayer 13 to the heat exchange section 7 side.

The cooling water Wa flowing from the cooling liquid inlet pipe 41 into the heat exchanging portion 8 is introduced to the inlet side of the heat exchanging portion 11 via the cooling water pipe 42 connected to the outlet side of the heat exchanging portion 8. It is guided and flows out from the cooling water outlet pipe 43. After absorbing heat of absorption in the heat exchange section 8, the refrigerant vapor R ₁ transferred from the low temperature regenerator G ₁ in the heat exchange section 11 is cooled and condensed. Let

From the liquid to be cooled inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We that flows in to and flows out from the liquid to be cooled outlet pipe 46 is cooled by the heat of vaporization of the refrigerant Re. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

A dilute solution pipe 21 having a solution pump LP is connected to the bottom of the container 2 of the absorber A.
The dilute solution pipe 21 passes through the heated side of the low temperature solution heat exchanger H ₁ and then is supplied with the first branch pipe 21A and the second branch pipe 21.
It is branched into three routes of B and the third branch pipe 21C. Then, the first branch pipe 21A is connected to the high-temperature regenerator G ₃ through the heated side of the high-temperature solution heat exchanger H _3, the second branch pipe 21B is medium temperature solution heat exchanger H ₂
Is connected to the medium temperature regenerator G ₂ through the heated side of, and the third branch pipe 21C is connected to the low temperature regenerator G ₁ .

The medium temperature solution pipe 26 for guiding the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G ₂ is connected to the third branch pipe 21C after passing through the heating side of the medium temperature solution heat exchanger H _2. There is.

Therefore, the dilute solution flowing out of the absorber A is obtained.
La is the low temperature solution heat exchanger H₁After passing through the heated side of
Into three, one of which is the high temperature solution heat exchanger H₃
Through the high temperature regenerator G₃While flowing into the other
Medium temperature solution heat exchanger H₂Through the above medium temperature regenerator G₂Flow
And the other is the above medium temperature regenerator G₂Spilled from, medium temperature
Solution heat exchanger H₂Medium temperature concentrated solution L after passing through the heating side of₂Combined with
Flow the above low temperature regenerator G ₁Will flow into.

[0470] connected to said high-temperature regenerator G ₃ leads to a high temperature concentrated solution L ₃ exiting from the high temperature generator G _3, hot solution pipe 27 through the heating side of the high-temperature solution heat exchanger H _3, said bifurcated at a downstream side position of the high-temperature solution heat exchanger H _3, one branch pipe 27A is connected to the downstream side position of the medium-temperature solution heat exchanger H ₂ in the medium-temperature solution pipe 26, the other branch pipe 27B is cold concentrated guides the solution L ₁ merges with the low temperature solution pipe 25 the concentrated solution pipe 24, and the above low-temperature solution heat exchanger to flow out connected to the low temperature regenerator G ₁ from the cold regenerator G ₁ It is connected to the solution sprayer 12 through the heating side of H ₁ .

The air chamber side of the high temperature regenerator G ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The solution heating section 10 of the low temperature regenerator G ₁
The outlet side of the condenser is connected to the condenser C via a refrigerant drain pipe 35.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is joined to the refrigerant drain pipe 35.

The refrigerant R ₁ generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The absorption type refrigerating apparatus Z ₁₄ constitutes a circulation cycle of the refrigerant and the absorbing solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₁₄ will be specifically described.

The dilute solution La (concentration ξa) fed from the absorber A by the solution pump LP passes through the heated side of the low temperature solution heat exchanger H _{1 and} is then branched into three. one passes through the heated side of the high-temperature solution heat exchanger H ₃ flows into the high-temperature regenerator G _3, the high-temperature regenerator G ₃
In the above, at the time of being subjected to the heating concentration effect by the external heat source J, a high temperature concentrated solution L ₃ having a concentration ξ ₃ flows out, and passes through the heating side of the high temperature solution heat exchanger H ₃ . At this time, in the high temperature solution heat exchanger H ₃ , heat exchange is performed between the diluted solution La on the heated side and the high temperature concentrated solution L ₃ on the heating side (heat recovery), and the diluted solution La is preheated. In this state, it flows into the high temperature regenerator G ₃ side.

[0479] On the other hand, the branched other dilute solution La is passed through the heated side of the medium-temperature solution heat exchanger H _2, flows into the intermediate temperature regenerator G _2, the high temperature in the middle temperature regenerator G ₂ Refrigerant vapor R ₃ flowing into the solution heating unit 9 from the container G ₃ side
Is heated and concentrated by flowing becomes medium temperature concentrated solution L ₂ concentrations xi] _2, exits through the heating side of the medium-temperature solution heat exchanger H _2. The medium-temperature concentrated solution L _{2 that} has passed through the medium-temperature solution heat exchanger H ₂ flows out of the high-temperature regenerator G ₃ and then passes through the heating side of the high-temperature solution heat exchanger H ₃ , and then the high-temperature concentrated solution L ₃ And a dilute solution La flowing through the third branch pipe 21C and flow into the low temperature regenerator G ₁ . At this time, in the medium temperature solution heat exchanger H ₂ , heat is exchanged between the dilute solution La on the heated side and the medium temperature concentrated solution L ₂ on the heating side (heat recovery), and the dilute solution La is preheated. In this state, it flows into the medium temperature regenerator G ₂ side.

Further, the low temperature regenerator G₁Flowing into
Solution (high temperature concentrated solution L₃And medium-temperature concentrated solution L ₂And dilute solution La
Mixed solution) is the low temperature regenerator G₁At the above medium temperature regeneration
Bowl G₂Refrigerant vapor R flowing into the solution heating unit 10 from the side₂
Heated and concentrated by the concentration ξ₁Low temperature concentrated solution L₁Becomes
Outflow.

The low temperature concentrated solution L ₁ having the concentration ξ ₁ flowing out from the low temperature regenerator G ₁ flows out from the high temperature regenerator G ₃ side and is branched at the outlet side of the high temperature solution heat exchanger H ₃ . concentrated solution Lg next concentration xi] ₃ hot concentrated solution L ₃ and merging to a concentration xi] _m, through the heating side of the low-temperature solution heat exchanger H ₁ flows into the absorber a side, wherein the solution spraying It is sprayed by the container 12. At this time, in the low temperature solution heat exchanger H ₁ , heat exchange is performed between the diluted solution La on the heated side and the concentrated solution Lg having the concentration ξ _m on the heating side.

The above is the absorption refrigeration apparatus Z _{14 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

In the absorption type refrigerating apparatus Z _{14 according} to the 14th embodiment, the dilute solution La branched into three after passing through the low temperature solution heat exchanger H ₁ is regenerated by the regenerators G ₃ , G ₂ , respectively. Since it is configured to flow into G ₁ ,
In the medium temperature regenerator G ₂ , the unconcentrated dilute solution L
Since a flows in as it is, the concentration of the absorbing solution becomes lower than that in the case where the absorbing solution (concentrated solution) that has been heated and concentrated in the high temperature regenerator G ₃ flows in, and the boiling temperature becomes lower accordingly. , decrement the boiling temperature of the absorbent solution in the intermediate temperature regenerator G ₂ only, and thus capable of setting a low refrigerant vapor temperature at the high temperature generator G ₃ to be the heat source. As a result, the operating pressure of the high temperature regenerator G ₃ which is proportional to the refrigerant vapor temperature can be set low,
As a result, it is possible to provide an absorption type refrigeration system having a low operating pressure and good operability.

On the high temperature solution heat exchanger H ₃ side and the medium temperature solution heat exchanger H ₂ side, only the dilute solution La branched into three flows in. Compared with the case where the entire amount of the dilute solution La branched after passing through the solution heat exchanger H ₁ is flown into the high temperature solution heat exchanger H ₃ and the medium temperature solution heat exchanger H ₂ , the high temperature solution heat exchanger H ₃ Also, the flow rate in the medium temperature solution heat exchanger H ₂ is reduced, and the high temperature solution heat exchanger H ₃ and the medium temperature solution heat exchanger H ₂ can be made compact in response to the reduction in the flow rate.

Further, by diluting the dilute solution La from the absorber A and allowing a part of the dilute solution La to flow into the high temperature regenerator G ₃ , for example, the entire amount of the dilute solution La remains as it is. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases. As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system Z ₂ is improved.

Further, the absorption type refrigeration system Z of this embodiment₁₄
Then, the high temperature regenerator G₃High temperature concentrated solution L from₃Is high above
Hot solution heat exchanger H₃After passing through the heating side of the
Part is the above-mentioned medium temperature regenerator G₂Medium temperature concentrated solution L from₂With above
Low temperature regenerator G₁Since it is configured to flow into
High temperature regenerator G₃High temperature concentrated solution L from₃And low temperature regenerator G₁Or
Low temperature concentrated solution L₁It will merge with
Organ G₁High temperature concentrated solution L ₃That a part of the
Finally, the concentrated solution L₃, L₁Pressure adjustment when merging
Alignment is easy, and solution merging can be performed smoothly.
It

Further, the absorption type refrigerating apparatus Z _{14 of} this embodiment.
In this case, since the dilute solution La discharged from the absorber A is branched into three after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ and the medium temperature regenerator G ₂ are provided immediately before that. The dilute solution La that flows in via the high temperature solution heat exchanger H ₃ and the medium temperature solution heat exchanger H ₂ both flows in the preheated state in the low temperature solution heat exchanger H ₁ , and as a result, The required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the medium temperature regenerator G ₂ is reduced, and the thermal efficiency of the entire system can be expected to improve.

Further, the absorption refrigeration system Z _{14 of} this embodiment is also provided.
Then, the system is configured by _three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ , but such a configuration requires a large number of regenerators. To increase the efficiency of the absorption solution by increasing the number of concentration stages of the absorption solution, and to increase the number of solution heat exchangers to increase the heat recovery rate, and the merit of improving the performance of the absorption refrigeration system, and the regenerator and When weighed against the disadvantage of increasing the manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. is there.

In the present embodiment, part of the high temperature concentrated solution L ₃ flowing out from the high temperature regenerator G ₃ is replaced with the medium temperature regenerator G 3.
_The medium-temperature concentrated solution L ₂ flowing out from the medium ₂ is joined in the middle of the medium-temperature solution pipe 26, but a part of the high-temperature concentrated solution L ₃ is directly introduced into the low-temperature regenerator G _1. May be.

XV: Fifteenth Embodiment FIG. 19 shows an operation cycle of the absorption refrigeration system Z _{15 according} to the fifteenth embodiment of the present invention. The absorption type refrigerating apparatus Z ₁₅ is an absorption type refrigerating apparatus which uses water as a refrigerant and lithium bromide as an absorbing liquid, and includes one condenser C, an absorber A, an evaporator E, and three each. Solution heat exchanger H ₃ ,
The H ₂ and H ₁ and the regenerators G ₃ , G ₂ and G ₁ are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E comprises a heat exchange part 7 for passing the liquid We to be cooled and a refrigerant sprayer 13 for spraying the refrigerant Re on the heat exchange part 7 in the container 1.

In the above-mentioned absorber A, the concentrated solution Lg is put in the container 2.
And a heat exchange section 8 for removing absorption heat generated in the absorber A. The condenser C is configured by including the heat exchange section 11 in the container 6.

Each of the regenerators G ₃ , G ₂ and G ₁ is for the purpose of heating and concentrating the absorption solution containing the refrigerant to obtain a concentrated solution of high concentration in sequence, and between them, High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium-temperature regenerator G ₂ that operates at a medium temperature and is configured to have an external heat source J (for example, combustion gas or steam) inside the container 3 (the “low-temperature side regenerator G _n in the claims”). _-1 "
Applicable) to is configured with a solution heating unit 9 in the container 4, corresponding to the even most low temperature regenerator G ₁ ( "lowest temperature side of the regenerator G _1" in the claims which operates at a low temperature )
Is provided with a solution heating unit 10 in the container 5.

Each of the heat exchangers H ₁ , H ₂ , and H ₃ has a low-temperature concentrated solution L ₁ , a medium-temperature concentrated solution L ₂ , and a high-temperature concentrated solution produced in the regenerators G ₁ , G ₂ , and G _3. It is for recovering the heat of each L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types,
For example, it is composed of a plate heat exchanger.

These respective devices are operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the container 6 of the condenser C and the container 1 of the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30. It is supplied to the evaporator E side. Further, the liquid refrigerant Rc supplied to the evaporator E is the refrigerant pump RP.
Is pumped up to the refrigerant sprayer 13 through the liquid refrigerant pipe 29, and is sprayed as the refrigerant Re from the refrigerant sprayer 13 to the heat exchange section 7 side.

The cooling water Wa flowing from the cooling liquid inlet pipe 41 into the heat exchanging portion 8 is introduced to the inlet side of the heat exchanging portion 11 via the cooling water pipe 42 connected to the outlet side of the heat exchanging portion 8. It is guided and flows out from the cooling water outlet pipe 43. After absorbing heat of absorption in the heat exchange section 8, the refrigerant vapor R ₁ transferred from the low temperature regenerator G ₁ in the heat exchange section 11 is cooled and condensed. Let

From the liquid to be cooled inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We that flows in to and flows out from the liquid to be cooled outlet pipe 46 is cooled by the heat of vaporization of the refrigerant Re. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

A dilute solution pipe 21 having a solution pump LP is connected to the bottom of the container 2 of the absorber A.
The dilute solution pipe 21 passes through the heated side of the low temperature solution heat exchanger H ₁ and then is supplied with the first branch pipe 21A and the second branch pipe 21.
It is branched into three routes of B and the third branch pipe 21C. Then, the first branch pipe 21A is connected to the high-temperature regenerator G ₃ through the heated side of the high-temperature solution heat exchanger H _3, the second branch pipe 21B is medium temperature solution heat exchanger H ₂
Is connected to the medium temperature regenerator G ₂ through the heated side of, and the third branch pipe 21C is connected to the low temperature regenerator G ₁ .

The medium temperature solution pipe 26 for guiding the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G ₂ is branched into two after passing through the heating side of the medium temperature solution heat exchanger H ₂ and one branch pipe. 26A is connected to the third branch pipe 21C, while the other branch pipe 26B guides the high temperature concentrated solution L ₃ flowing out from the high temperature regenerator G ₃ and after passing through the high temperature solution heat exchanger H ₃ . It is connected to the high temperature solution pipe 27.

Therefore, the dilute solution La flowing out from the absorber A is branched into three after passing through the heated side of the low temperature solution heat exchanger H ₁ , and _one of them is divided into the high temperature solution heat exchanger H ₃
While flowing into the high temperature regenerator G ₃ through the other, the other flows into the middle temperature regenerator G ₂ through the medium temperature solution heat exchanger H ₂ and the other flows out from the middle temperature regenerator G ₂ . After passing through the heating side of the medium temperature solution heat exchanger H ₂ , it joins with a part of the medium temperature concentrated solution L ₂ branched and flows into the low temperature regenerator G ₁ .

High temperature regenerator G₃Connected to the high temperature re
Organ G₃High temperature concentrated solution L flowing out from₃The above high temperature melting
Liquid heat exchanger H₃High temperature solution pipe 27 passing through the heating side of
Low temperature regenerator G₁Connected to the low temperature regenerator G₁Spilled from
Low temperature concentrated solution L₁The low temperature solution pipe 25 that guides
To become the concentrated solution pipe 24, and the low temperature solution heat exchanger H ₁
To the solution sprayer 12 through the heating side of the.

The air chamber side of the high temperature regenerator G ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating unit 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The solution heating section 10 of the low temperature regenerator G ₁
The outlet side of the condenser is connected to the condenser C via a refrigerant drain pipe 35.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is joined to the refrigerant drain pipe 35.

The refrigerant R ₁ generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The absorption type refrigerating apparatus Z ₁₅ constitutes a circulation cycle of the refrigerant and the absorbing solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₁₅ will be specifically described.

The dilute solution La (concentration ξa) fed from the absorber A by the solution pump LP passes through the heated side of the low temperature solution heat exchanger H _{1 and} is then branched into three parts. one passes through the heated side of the high-temperature solution heat exchanger H ₃ flows into the high-temperature regenerator G _3, the high-temperature regenerator G ₃
In the above, at the time of being subjected to the heating concentration effect by the external heat source J, a high temperature concentrated solution L ₃ having a concentration ξ ₃ flows out, and passes through the heating side of the high temperature solution heat exchanger H ₃ . At this time, in the high temperature solution heat exchanger H ₃ , heat exchange is performed between the diluted solution La on the heated side and the high temperature concentrated solution L ₃ on the heating side (heat recovery), and the diluted solution La is preheated. In this state, it flows into the high temperature regenerator G ₃ side.

[0511] On the other hand, the branched other dilute solution La is passed through the heated side of the medium-temperature solution heat exchanger H _2, flows into the intermediate temperature regenerator G _2, the high temperature in the middle temperature regenerator G ₂ Refrigerant vapor R ₃ flowing into the solution heating unit 9 from the container G ₃ side
Is heated and concentrated by flowing becomes medium temperature concentrated solution L ₂ concentrations xi] _2, exits through the heating side of the medium-temperature solution heat exchanger H _2. And, in some this intermediate temperature solution heat exchanger H ₂ medium temperature concentrated solution passed through L _2, hot concentrated and passed through a heating side of the high-temperature solution heat exchanger H ₃ after flowing out from the high temperature generator G ₃ While merging with the solution L ₃ , the rest of the medium-temperature concentrated solution L ₂ is
It merges with the dilute solution La flowing through the third branch pipe 21C and flows into the low temperature regenerator G ₁ . At this time, in the medium temperature solution heat exchanger H ₂ , heat exchange is performed between the dilute solution La on the heated side and the medium temperature concentrated solution L ₂ on the heating side (heat recovery),
The diluted solution La flows into the medium temperature regenerator G ₂ side in a preheated state.

Further, the low temperature regenerator G₁Flowing into
Solution (Medium temperature concentrated solution L₂And a dilute solution La is a mixed solution)
The low temperature regenerator G₁In the above medium temperature regenerator G₂Above from the side
Refrigerant vapor R flowing into the solution heating unit 10₂Heated by
Contracted, concentration ξ₁Low temperature concentrated solution L ₁And then outflow.

Then, the low temperature concentrated solution L ₁ having a concentration ξ ₁ flowing out from the low temperature regenerator G ₁ is the high temperature concentrated solution L ₃ having a concentration ξ ₃ flowing out from the high temperature regenerator G ₃ side and the high temperature solution heat At the outlet side of the exchanger H ₃ , the medium temperature concentrated solution L ₂ merged into a concentrated solution Lg having a concentration of ξ _m , which passes through the heating side of the low temperature solution heat exchanger H _{1 to} the absorber A side. It flows in, where it is sprayed by the solution sprayer 12. At this time, in the low temperature solution heat exchanger H ₁ , heat exchange is performed between the diluted solution La on the heated side and the concentrated solution Lg having the concentration ξ _m on the heating side.

The above is the absorption refrigeration apparatus Z _{15 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

In the absorption type refrigerating apparatus Z _{15 according} to the 15th embodiment, the dilute solution La branched into three after passing through the low temperature solution heat exchanger H ₁ is regenerated by the regenerators G ₃ , G ₂ , respectively. Since it is configured to flow into G ₁ ,
In the medium temperature regenerator G ₂ , the unconcentrated dilute solution L
Since a flows in as it is, the concentration of the absorbing solution becomes lower than that in the case where the absorbing solution (concentrated solution) that has been heated and concentrated in the high temperature regenerator G ₃ flows in, and the boiling temperature becomes lower accordingly. , decrement the boiling temperature of the absorbent solution in the intermediate temperature regenerator G ₂ only, and thus capable of setting a low refrigerant vapor temperature at the high temperature generator G ₃ to be the heat source. As a result, the operating pressure of the high temperature regenerator G ₃ which is proportional to the refrigerant vapor temperature can be set low,
As a result, it is possible to provide an absorption type refrigeration system having a low operating pressure and good operability.

On the high-temperature solution heat exchanger H ₃ side and the medium-temperature solution heat exchanger H ₂ side, only the diluted solution La branched into three flows in. Compared with the case where the entire amount of the dilute solution La branched after passing through the solution heat exchanger H ₁ is flown into the high temperature solution heat exchanger H ₃ and the medium temperature solution heat exchanger H ₂ , the high temperature solution heat exchanger H ₃ Also, the flow rate in the medium temperature solution heat exchanger H ₂ is reduced, and the high temperature solution heat exchanger H ₃ and the medium temperature solution heat exchanger H ₂ can be made compact in response to the reduction in the flow rate.

Furthermore, the dilute solution La from the absorber A is branched so that a part of the dilute solution La is made to flow into the high temperature regenerator G ₃ , so that, for example, the entire amount of the dilute solution La remains as it is. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases. As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system Z ₂ is improved.

Further, the absorption type refrigeration system Z _{15 of} this embodiment
In medium temperature concentrated solution L ₂ from the intermediate temperature regenerator G ₂ is branched after passing through the heating side of the medium-temperature solution heat exchanger H _2, the high-temperature part thereof flows out from the high temperature generator G ₃ Since it is configured so as to join with the high temperature concentrated solution L ₃ that has passed through the heating side of the solution heat exchanger H _3, the amount of concentrated solution flowing into the low temperature regenerator G ₁ is reduced, and the low temperature regenerator G ₁ The amount of heat required for the regeneration (in other words, the evaporation of the refrigerant vapor) is small. Therefore, the thermal efficiency in the low temperature regenerator G ₁ is improved.

Also, the absorption refrigerating apparatus Z _{15 of} this embodiment
In this case, since the dilute solution La discharged from the absorber A is branched into three after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ and the medium temperature regenerator G ₂ are provided immediately before that. The dilute solution La that flows in via the high temperature solution heat exchanger H ₃ and the medium temperature solution heat exchanger H ₂ both flows in the preheated state in the low temperature solution heat exchanger H ₁ , and as a result, The required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the medium temperature regenerator G ₂ is reduced, and the thermal efficiency of the entire system can be expected to improve.

Further, the absorption refrigeration system Z _{15 of} this embodiment is also provided.
Then, the system is configured by _three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ , but such a configuration requires a large number of regenerators. To increase the efficiency of the absorption solution by increasing the number of concentration stages of the absorption solution, and to increase the number of solution heat exchangers to increase the heat recovery rate, and the merit of improving the performance of the absorption refrigeration system, and the regenerator and When weighed against the disadvantage of increasing the manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. is there.

XVI: Sixteenth Embodiment FIG. 20 shows an operation cycle of the absorption refrigeration system Z _{16 according} to the sixteenth embodiment of the present invention. The absorption type refrigerating apparatus Z ₁₆ is an absorption type refrigerating apparatus which uses water as a refrigerant and lithium bromide as an absorbing liquid, and includes one condenser C, an absorber A, an evaporator E, and three pieces each. Solution heat exchanger H ₃ ,
The H ₂ and H ₁ and the regenerators G ₃ , G ₂ and G ₁ are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E comprises a heat exchange part 7 for passing the liquid We to be cooled and a refrigerant sprayer 13 for spraying the refrigerant Re on the heat exchange part 7 in the container 1.

[0523] The absorber A has a container 2 having a concentrated solution Lg.
And a heat exchange section 8 for removing absorption heat generated in the absorber A. The condenser C is configured by including the heat exchange section 11 in the container 6.

Each of the regenerators G ₃ , G ₂ and G ₁ is for heating and concentrating the absorbing solution containing the refrigerant to obtain a concentrated solution having a high concentration in sequence. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium-temperature regenerator G ₂ that operates at a medium temperature and is configured to have an external heat source J (for example, combustion gas or steam) inside the container 3 (the “low-temperature side regenerator G _n in the claims”). _-1 "
Applicable) to is configured with a solution heating unit 9 in the container 4, corresponding to the even most low temperature regenerator G ₁ ( "lowest temperature side of the regenerator G _1" in the claims which operates at a low temperature )
Is provided with a solution heating unit 10 in the container 5.

The solution heat exchangers H ₁ , H ₂ and H ₃ are the low temperature concentrated solution L ₁ produced by the regenerators G ₁ , G ₂ and G ₃ , respectively.
This is for recovering the heat of each of the medium-temperature concentrated solution L ₂ and the high-temperature concentrated solution L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types For example, it may be configured by a plate heat exchanger.

These respective devices are operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the container 6 of the condenser C and the container 1 of the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30. It is supplied to the evaporator E side. Further, the liquid refrigerant Rc supplied to the evaporator E is the refrigerant pump RP.
Is pumped up to the refrigerant sprayer 13 through the liquid refrigerant pipe 29, and is sprayed as the refrigerant Re from the refrigerant sprayer 13 to the heat exchange section 7 side.

The cooling water Wa flowing from the cooling liquid inlet pipe 41 into the heat exchange section 8 is introduced to the inlet side of the heat exchange section 11 via the cooling water pipe 42 connected to the outlet side of the heat exchange section 8. It is guided and flows out from the cooling water outlet pipe 43. After absorbing heat of absorption in the heat exchange section 8, the refrigerant vapor R ₁ transferred from the low temperature regenerator G ₁ in the heat exchange section 11 is cooled and condensed. Let

[0529] From the liquid to be cooled inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We that flows in to and flows out from the liquid to be cooled outlet pipe 46 is cooled by the heat of vaporization of the refrigerant Re. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

A dilute solution pipe 21 equipped with a solution pump LP is connected to the bottom of the container 2 of the absorber A.
The dilute solution pipe 21 passes through the heated side of the low temperature solution heat exchanger H ₁ and then is supplied with the first branch pipe 21A and the second branch pipe 21.
It is branched into two routes of B. The first branch pipe 21A is connected to the high temperature regenerator G ₃ through the heated side of the high temperature solution heat exchanger H ₃ . The second branch pipe 21B is connected to the medium temperature regenerator G ₂ through the heated side of the medium temperature solution heat exchanger H ₂ . Therefore, the dilute solution La flowing out of the absorber A branches after passing through the heated side of the low temperature solution heat exchanger H ₁ , and _one of them branches through the high temperature solution heat exchanger H ₃ to the high temperature regenerator. It flows into G ₃ , and the other flows into the intermediate temperature regenerator G ₂ via the intermediate temperature solution heat exchanger H ₂ .

The medium temperature solution pipe 26, which is connected to the medium temperature regenerator G ₂ and guides the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G ₂ , passes through the heating side of the medium temperature solution heat exchanger H _2. It is connected to the low temperature regenerator G ₁ .

[0532] connected to said high-temperature regenerator G ₃ leads to a high temperature concentrated solution L ₃ exiting from the high temperature generator G _3, hot solution pipe 27 through the heating side of the high-temperature solution heat exchanger H _3, said _On the outlet side of the high temperature solution heat exchanger H ₃ , it is branched into two,
One branch pipe 27A is connected to the low temperature regenerator G _1, the other branch pipe 27B guides the cold concentrated solution L ₁ which flows out is connected to the low temperature regenerator G ₁ from the cold regenerator G ₁ The concentrated solution pipe 24 is joined with the low temperature solution pipe 25 and is connected to the solution sprayer 12 through the heating side of the low temperature solution heat exchanger H ₁ .

The air chamber side of the high temperature regenerator G ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The solution heating section 10 of the low temperature regenerator G ₁
The outlet side of the condenser is connected to the condenser C via a refrigerant drain pipe 35.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is joined to the refrigerant drain pipe 35.

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The absorption refrigeration system Z ₁₆ constitutes a circulation cycle of the refrigerant and the absorption solution by adopting the above-mentioned equipment arrangement and path configuration.

Next, the operation cycle of the absorption type refrigerating apparatus Z ₁₆ will be specifically described.

The dilute solution La (concentration ξa) fed from the absorber A by the solution pump LP passes through the heated side of the low temperature solution heat exchanger H ₁ and is branched.
One of them flows into the high-temperature regenerator G ₃ through the heated side of the high-temperature solution heat exchanger H ₃ and is subjected to the heating and concentrating action by the external heat source J in the high-temperature regenerator G _{3 so} that the concentration ξ ₃
Of high temperature concentrated solution L ₃ and flows out, and passes through the heating side of the high temperature solution heat exchanger H ₃ . At this time, in the high temperature solution heat exchanger H ₃ , heat exchange is performed between the diluted solution La on the heated side and the high temperature concentrated solution L ₃ on the heating side (heat recovery), and the diluted solution La is preheated. In this state, it flows into the high temperature regenerator G ₃ side.

[0541] On the other hand, the branched other dilute solution La is passed through the heated side of the medium-temperature solution heat exchanger H _2, flows into the intermediate temperature regenerator G _2, the high temperature in the middle temperature regenerator G ₂ Refrigerant vapor R ₃ flowing into the solution heating unit 9 from the container G ₃ side
The solution is heated and concentrated by the solution, becomes a medium-temperature concentrated solution L ₂ having a concentration of ξ ₂ , flows out, and flows into the low-temperature regenerator G ₁ through the heating side of the medium-temperature solution heat exchanger H ₂ . At this time, in the medium temperature solution heat exchanger H ₂ , heat exchange is performed between the dilute solution La on the heated side and the medium temperature concentrated solution L ₂ on the heating side (heat recovery),
The diluted solution La flows into the medium temperature regenerator G ₂ side in a preheated state.

Further, the medium-temperature concentrated solution L ₂ flowing into the low-temperature regenerator G ₁ is the refrigerant vapor R ₂ flowing into the solution heating unit 10 from the medium-temperature regenerator G ₂ side in the low-temperature regenerator G ₁ .
It is heated and concentrated by and is discharged as a low temperature concentrated solution L ₁ having a concentration ξ ₁ .

Furthermore, a part of the high temperature concentrated solution L _{3 having} a concentration ξ ₃ flowing out from the high temperature regenerator G ₃ flows into the low temperature regenerator G ₁ , while the rest of the high temperature concentrated solution L ₃ is The low-temperature concentrated solution L ₁ having a concentration ξ ₁ flowing out from the low-temperature regenerator G ₁ joins to form a concentrated solution Lg having a concentration ξ _m , passes through the heating side of the low-temperature solution heat exchanger H ₁ , and the absorber A side. Flowing into
Here, the solution is sprayed by the solution sprayer 12. At this time, in the low temperature solution heat exchanger H ₁ , heat is exchanged between the diluted solution La on the heated side and the concentrated solution Lg having the concentration ξ _m on the heating side (heat recovery), and the diluted solution La is In the preheated state, they branch into the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ , respectively.

The above is the absorption refrigeration apparatus Z _{16 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

Absorption refrigeration according to the sixteenth embodiment
Device Z₁₆In, the diluted solution La discharged from the absorber A is
One of them is diverged, and the other one is regenerated at high temperature with the entire amount of branching.
Bowl G ₃To the other side, and the other one recovers the entire amount of branching at the above intermediate temperature.
Bowl G₂Flow into the low temperature regenerator G₁Flowing into
Since it is configured to operate, the above-mentioned medium temperature regenerator G₂To
In this case, the unconcentrated dilute solution La flows in as it is.
Thus, for example, the high temperature regenerator G₃Condensed with heating concentrated in
Absorption solution as compared to the case where a collection solution (concentrated solution) is flowed in
The lower the concentration, the lower the boiling temperature.
This medium temperature regenerator G ₂Of boiling temperature of absorbing solution in water
The high temperature regenerator G that serves as the heat source₃In
Since the refrigerant vapor temperature can be set low,
The high temperature regenerator G proportional to the temperature of the refrigerant vapor₃Operating pressure
Can be set lower, resulting in lower operating pressure
It is possible to provide an absorption type refrigerating device with good operability.
It will be.

Further, the dilute solution La from the absorber A is branched so that a part of the dilute solution La is caused to flow into the high temperature regenerator G ₃ , so that, for example, the entire amount of the dilute solution La remains as it is. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system Z ₁ is improved.

[0547] Further, a part of it which is adapted to flow into the said high temperature regenerator G ₃ is branched dilute solution La from the absorber A, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution L flowing in here is supplied.
As the amount of a decreases, the heat transfer area can be reduced to make the device compact, which in turn contributes to making the absorption refrigeration system Z ₁ compact.

Further, the absorption type refrigeration system Z of this embodiment₁₆
Then, the high temperature regenerator G₃High temperature concentrated solution L from₃Is high above
Hot solution heat exchanger H₃After passing through the heating side of the
Part is the above-mentioned medium temperature regenerator G₂Medium temperature concentrated solution L from₂With above
Low temperature regenerator G₁Since it is configured to flow into
High temperature regenerator G₃High temperature concentrated solution L from₃And low temperature regenerator G₁Or
Low temperature concentrated solution L₁It will merge with
Organ G₁High temperature concentrated solution L ₃That a part of the
Finally, the concentrated solution L₃, L₁Pressure adjustment when merging
Alignment is easy, and solution merging can be performed smoothly.
It

Further, the absorption refrigeration system Z _{16 of} this embodiment is also provided.
In this case, since the diluted solution La discharged from the absorber A is branched after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ is passed through the high temperature solution heat exchanger H ₃ immediately before it. And the dilute solution La flowing into the medium temperature regenerator G ₂ via the medium temperature solution heat exchanger H ₂ immediately before it.
Means that both flow into the low temperature solution heat exchanger H ₁ in a preheated state, and as a result, the required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ decreases. It can be expected that the thermal efficiency of the entire system will be improved.

Furthermore, the absorption type refrigerating apparatus Z of this embodiment
₁₆Then, three regenerators G₁, G₂, G ₃And three solution heat exchange
Exchanger H₁, H₂, H₃The system is made up of
In the configuration, the number of regenerators is increased to increase the number of absorption solution concentration stages.
Increase the heat efficiency and increase the number of solution heat exchangers.
Absorption refrigeration system by increasing the heat recovery rate
Of the regenerator and solution heat
The increase in manufacturing costs due to the increase in the number of exchangers
If weigh the disadvantages, the absorption refrigeration system Z
₁Optimal for achieving both performance and cost
It is conceivable and extremely useful in practice.

XVII: Seventeenth Embodiment FIG. 21 shows an operation cycle of the absorption refrigerating apparatus Z _{17 according} to the seventeenth embodiment of the present invention. The absorption type refrigerating apparatus Z ₁₇ is an absorption type refrigerating apparatus using water as a refrigerant and lithium bromide as an absorbing liquid, and includes one condenser C, an absorber A, an evaporator E, and three each. Solution heat exchanger H ₃ ,
The H ₂ and H ₁ and the regenerators G ₃ , G ₂ and G ₁ are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E comprises a container 1 having a heat exchange section 7 for passing the liquid We to be cooled and a refrigerant sprayer 13 for spraying the refrigerant Re on the heat exchange section 7.

[0553] The absorber A has a container 2 containing a concentrated solution Lg.
And a heat exchange section 8 for removing absorption heat generated in the absorber A. The condenser C is configured by including the heat exchange section 11 in the container 6.

Each of the regenerators G ₃ , G ₂ and G ₁ is for heating and concentrating the absorption solution containing the refrigerant to obtain a concentrated solution having a high concentration in sequence. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium-temperature regenerator G ₂ that operates at a medium temperature and is configured to have an external heat source J (for example, combustion gas or steam) inside the container 3 (the “low-temperature side regenerator G _n in the claims”). _-1 "
Applicable) to is configured with a solution heating unit 9 in the container 4, corresponding to the even most low temperature regenerator G ₁ ( "lowest temperature side of the regenerator G _1" in the claims which operates at a low temperature )
Is provided with a solution heating unit 10 in the container 5.

The solution heat exchangers H ₁ , H ₂ and H ₃ are the low temperature concentrated solution L ₁ produced by the regenerators G ₁ , G ₂ and G ₃ , respectively.
This is for recovering the heat of each of the medium-temperature concentrated solution L ₂ and the high-temperature concentrated solution L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types For example, it may be configured by a plate heat exchanger.

Each of these devices is operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the container 6 of the condenser C and the container 1 of the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30. It is supplied to the evaporator E side. Further, the liquid refrigerant Rc supplied to the evaporator E is the refrigerant pump RP.
Is pumped up to the refrigerant sprayer 13 through the liquid refrigerant pipe 29, and is sprayed as the refrigerant Re from the refrigerant sprayer 13 to the heat exchange section 7 side.

The cooling water Wa flowing from the cooling liquid inlet pipe 41 into the heat exchanging portion 8 is introduced to the inlet side of the heat exchanging portion 11 via the cooling water pipe 42 connected to the outlet side of the heat exchanging portion 8. It is guided and flows out from the cooling water outlet pipe 43. After absorbing heat of absorption in the heat exchange section 8, the refrigerant vapor R ₁ transferred from the low temperature regenerator G ₁ in the heat exchange section 11 is cooled and condensed. Let

From the liquid to be cooled inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We that flows in to and flows out from the liquid to be cooled outlet pipe 46 is cooled by the heat of vaporization of the refrigerant Re. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

A dilute solution pipe 21 equipped with a solution pump LP is connected to the bottom of the container 2 of the absorber A.
The dilute solution pipe 21 passes through the heated side of the low temperature solution heat exchanger H ₁ and then is supplied with the first branch pipe 21A and the second branch pipe 21.
It is branched into two routes of B. The first branch pipe 21A is connected to the high temperature regenerator G ₃ through the heated side of the high temperature solution heat exchanger H ₃ . The second branch pipe 21B is connected to the medium temperature regenerator G ₂ through the heated side of the medium temperature solution heat exchanger H ₂ . Therefore, the dilute solution La flowing out of the absorber A branches after passing through the heated side of the low temperature solution heat exchanger H ₁ , and _one of them branches through the high temperature solution heat exchanger H ₃ to the high temperature regenerator. It flows into G ₃ , and the other flows into the intermediate temperature regenerator G ₂ via the intermediate temperature solution heat exchanger H ₂ .

The medium temperature solution pipe 26 connected to the medium temperature regenerator G ₂ guides the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G _2, and the medium temperature solution pipe 26 passing through the heating side of the medium temperature solution heat exchanger H ₂ is _On the outlet side of the medium temperature solution heat exchanger H ₂ , it is branched into two,
One branch pipe 26A is connected to the low temperature regenerator G _1, the other branch pipe 26B leads to a high temperature concentrated solution L ₃ exiting from the high temperature generator G ₃ is connected to the high-temperature regenerator G ₃ , the hot solution pipe 27 through the heating side of the high-temperature solution heat exchanger H _3, are connected at the outlet side of the high temperature solution heat exchanger H _3.

[0562] Also, the hot solution pipe 27, low-temperature solution pipe 25 concentrated solution joins the pipe 24 for guiding the cold concentrated solution L ₁ which flows out is connected to the low temperature regenerator G ₁ from the cold regenerator G ₁ And is connected to the solution sprayer 12 through the heating side of the low temperature solution heat exchanger H ₁ .

The air chamber side of the high temperature regenerator G ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The solution heating section 10 of the low temperature regenerator G ₁
The outlet side of the condenser is connected to the condenser C via a refrigerant drain pipe 35.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is joined to the refrigerant drain pipe 35.

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The absorption type refrigerating apparatus Z ₁₇ constitutes a circulation cycle of the refrigerant and the absorbing solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₁₇ will be specifically described.

The dilute solution La (concentration ξa) fed from the absorber A by the solution pump LP passes through the heated side of the low temperature solution heat exchanger H ₁ and is branched.
One of them flows into the high-temperature regenerator G ₃ through the heated side of the high-temperature solution heat exchanger H ₃ and is subjected to the heating and concentrating action by the external heat source J in the high-temperature regenerator G _{3 so} that the concentration ξ ₃
Of high temperature concentrated solution L ₃ and flows out, and passes through the heating side of the high temperature solution heat exchanger H ₃ . At this time, in the high temperature solution heat exchanger H ₃ , heat exchange is performed between the diluted solution La on the heated side and the high temperature concentrated solution L ₃ on the heating side (heat recovery), and the diluted solution La is preheated. In this state, it flows into the high temperature regenerator G ₃ side.

[0571] On the other hand, the branched other dilute solution La is passed through the heated side of the medium-temperature solution heat exchanger H _2, flows into the intermediate temperature regenerator G _2, the high temperature in the middle temperature regenerator G ₂ Refrigerant vapor R ₃ flowing into the solution heating unit 9 from the container G ₃ side
The solution is heated and concentrated by the solution, becomes a medium-temperature concentrated solution L ₂ having a concentration of ξ ₂ , flows out, and flows into the low-temperature regenerator G ₁ through the heating side of the medium-temperature solution heat exchanger H ₂ . At this time, in the medium temperature solution heat exchanger H ₂ , heat exchange is performed between the dilute solution La on the heated side and the medium temperature concentrated solution L ₂ on the heating side (heat recovery),
The diluted solution La flows into the medium temperature regenerator G ₂ side in a preheated state. Further, part of the medium-temperature concentrated solution L ₂ branches at the outlet side of the medium-temperature solution heat exchanger H ₂ and joins with the high-temperature concentrated solution L ₃ .

Further, the medium-temperature concentrated solution L ₂ flowing into the low-temperature regenerator G ₁ is the refrigerant vapor R ₂ flowing into the solution heating unit 10 from the medium-temperature regenerator G ₂ side in the low-temperature regenerator G ₁ .
It is heated and concentrated by and is discharged as a low temperature concentrated solution L ₁ having a concentration ξ ₁ .

Furthermore, the high temperature concentrated solution L ₃ having the concentration ξ ₃ flowing out from the high temperature regenerator G ₃ joins with a part of the medium temperature concentrated solution L ₂ , and then the concentration flowing out from the low temperature regenerator G _1. merges with the low temperature concentrated solution L ₁ of xi] ₁ concentration xi] _m of concentrated solution Lg
And passes through the heating side of the low temperature solution heat exchanger H ₁ and flows into the absorber A side where it is sprayed by the solution sprayer 12. At this time, in the low temperature solution heat exchanger H ₁ , heat is exchanged between the diluted solution La on the heated side and the concentrated solution Lg having the concentration ξ _m on the heating side (heat recovery), and the diluted solution La is In the preheated state, they branch into the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ , respectively.

The absorption refrigeration system Z _{17 of} this embodiment has been described above.
In the operation cycle, the following unique action and effects are obtained.

Absorption-type refrigeration according to the seventeenth embodiment
Device Z₁₇In, the diluted solution La discharged from the absorber A is
One of them is diverged, and the other one is regenerated at high temperature with the entire amount of branching.
Bowl G ₃To the other side, and the other one recovers the entire amount of branching at the above intermediate temperature.
Bowl G₂Flow into the low temperature regenerator G₁Flowing into
Since it is configured to operate, the above-mentioned medium temperature regenerator G₂To
In this case, the unconcentrated dilute solution La flows in as it is.
Thus, for example, the high temperature regenerator G₃Condensed with heating concentrated in
Absorption solution as compared to the case where a collection solution (concentrated solution) is flowed in
The lower the concentration, the lower the boiling temperature.
This medium temperature regenerator G ₂Of boiling temperature of absorbing solution in water
The high temperature regenerator G that serves as the heat source₃In
Since the refrigerant vapor temperature can be set low,
The high temperature regenerator G proportional to the temperature of the refrigerant vapor₃Operating pressure
Can be set lower, resulting in lower operating pressure
It is possible to provide an absorption type refrigerating device with good operability.
It will be.

Further, the dilute solution La from the absorber A is branched so that a part of the dilute solution La is caused to flow into the high temperature regenerator G ₃ , so that, for example, the entire amount of the dilute solution La remains as it is. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system Z ₁ is improved.

[0577] Further, a part of it which is adapted to flow into the said high temperature regenerator G ₃ is branched dilute solution La from the absorber A, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution L flowing in here is supplied.
As the amount of a decreases, the heat transfer area can be reduced to make the device compact, which in turn contributes to making the absorption refrigeration system Z ₁ compact.

Further, the absorption type refrigeration system Z _{17 of} this embodiment is also provided.
In medium temperature concentrated solution L ₂ from the intermediate temperature regenerator G ₂ is branched after passing through the heating side of the medium-temperature solution heat exchanger H _2, the high-temperature part thereof flows out from the high temperature generator G ₃ Since it is configured so as to join with the high temperature concentrated solution L ₃ that has passed through the heating side of the solution heat exchanger H _3, the amount of concentrated solution flowing into the low temperature regenerator G ₁ is reduced, and the low temperature regenerator G ₁ The amount of heat required for the regeneration (in other words, the evaporation of the refrigerant vapor) is small. Therefore, the thermal efficiency in the low temperature regenerator G ₁ is improved.

Further, the absorption type refrigeration system Z of this embodiment₁₇
Then, the high temperature regenerator G₃High temperature concentrated solution L from₃Is high above
Hot solution heat exchanger H₃After passing through the heating side of the
Part is the above-mentioned medium temperature regenerator G₂Medium temperature concentrated solution L from₂With above
Low temperature regenerator G₁Since it is configured to flow into
High temperature regenerator G₃High temperature concentrated solution L from₃And low temperature regenerator G₁Or
Low temperature concentrated solution L₁It will merge with
Organ G₁High temperature concentrated solution L ₃That a part of the
Finally, the concentrated solution L₃, L₁Pressure adjustment when merging
Alignment is easy, and solution merging can be performed smoothly.
It

[0580] Further, the absorption type refrigeration system Z _{17 of} this embodiment.
In this case, since the diluted solution La discharged from the absorber A is branched after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ is passed through the high temperature solution heat exchanger H ₃ immediately before it. And the dilute solution La flowing into the medium temperature regenerator G ₂ via the medium temperature solution heat exchanger H ₂ immediately before it.
Means that both flow into the low temperature solution heat exchanger H ₁ in a preheated state, and as a result, the required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ decreases. It can be expected that the thermal efficiency of the entire system will be improved.

Furthermore, the absorption type refrigeration system Z of this embodiment
₁₇Then, three regenerators G₁, G₂, G ₃And three solution heat exchange
Exchanger H₁, H₂, H₃The system is made up of
In the configuration, the number of regenerators is increased to increase the number of absorption solution concentration stages.
Increase the heat efficiency and increase the number of solution heat exchangers.
Absorption refrigeration system by increasing the heat recovery rate
Of the regenerator and solution heat
The increase in manufacturing costs due to the increase in the number of exchangers
If weigh the disadvantages, the absorption refrigeration system Z
₁Optimal for achieving both performance and cost
It is conceivable and extremely useful in practice.

XVIII: Eighteenth Embodiment FIG. 22 shows an operation cycle of the absorption refrigerating apparatus Z _{18 according} to the eighteenth embodiment of the present invention. The absorption refrigeration system Z ₁₈ has the same basic configuration as the absorption refrigeration system Z ₁₄ according to the fourteenth embodiment,
The difference from this is that in the absorption refrigeration system Z ₁₄ of the _fourteenth embodiment, cooling water Wa that cools the absorber A and the condenser C is supplied from the absorber A side to the condenser C side.
In contrast to the above, the absorption refrigerating apparatus Z _{18 of} this embodiment is configured to flow the cooling water Wa from the condenser C side to the absorber A side. is there. Therefore, the cooling water inlet pipe 41 in the fourteenth embodiment serves as the cooling water outlet pipe, and the cooling water outlet pipe 43 serves as the cooling water inlet pipe.

By using such a cooling water circulation system, for example, the cooling water W having a lower temperature is supplied to the condenser C as compared with the case of flowing the cooling water Wa from the absorber A side to the condenser C side.
Since a is supplied, the cooling capacity of the condenser C is improved, and the operating pressure of the low temperature regenerator G ₁ connected to the condenser C is reduced accordingly. As a result, the maximum pressure of the operating pressure of the entire cycle governed by the operating pressure of the low temperature regenerator G ₁ , that is, the operating pressure of the high temperature regenerator G ₃ is reduced, and the absorption refrigerating device having more excellent operability is reduced. Can be provided.

The structure of the absorption type refrigerating apparatus Z ₁₈ and the effects other than the above are the same as those of the absorption type refrigerating apparatus Z ₁₄ of the fourteenth embodiment.
By applying the corresponding description of the fourth embodiment, the description here will be omitted.

The structure of this embodiment (that is, the cooling water W
The structure in which the flow direction of a is changed from the condenser to the absorber) is
It is also applicable to the fourth to seventeenth embodiments.

XIX: Nineteenth Embodiment FIG. 23 shows an operation cycle of the absorption refrigerating apparatus Z _{19 according} to the nineteenth embodiment of the present invention. The absorption refrigeration system Z ₁₉ has the same basic configuration as the absorption refrigeration system Z ₁₄ according to the fourteenth embodiment,
The difference is that both the absorber A and the evaporator E have a two-stage configuration with different refrigerant evaporation temperatures, and the low-temperature regenerator G ₁ and the condenser C have two-stage configurations with different refrigerant condensation temperatures. That is the point. The absorber A, the evaporator E, the low-temperature regenerator G ₁ and the condenser C may be configured in two or more stages.

With this configuration, the entire cycle of the absorption refrigeration system Z ₁₉ is shifted to the low concentration side, and the operating pressure of the system is reduced accordingly, so that an absorption refrigeration system with good operability can be provided. .

The structure of the absorption refrigeration system Z ₁₉ and the operational effects other than those described above are the same as those of the absorption refrigeration system Z ₁₄ of the fourteenth embodiment described above.
By applying the corresponding description of the fourth embodiment, the description here will be omitted.

The structure of this embodiment (that is, the structure in which the absorber A, the evaporator E, the low-temperature regenerator G ₁ and the condenser C are constituted by two or more stages) has fourteenth to eighteenth aspects. It is also applicable to the embodiment.

XX: Twentieth Embodiment FIG. 24 shows an operation cycle of an absorption type refrigeration system Z _{20 according to} a twentieth embodiment of the present invention. The absorption type refrigerating apparatus Z ₂₀ is an absorption type refrigerating apparatus which uses water as a refrigerant and lithium bromide as an absorbing liquid, and includes one condenser C, an absorber A, an evaporator E and three pieces each. Solution heat exchanger H ₃ ,
H ₂ and H ₁ and regenerators G ₃ , G ₂ and G ₁ are used as a basic configuration, and in addition to this, two drain heat exchangers D ₁ and D ₂ and one exhaust heat exchanger K are provided. These devices are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E comprises a heat exchange section 7 for passing the liquid We to be cooled and a refrigerant distributor (not shown) for distributing the refrigerant on the heat exchange section 7.

The absorber A comprises a solution sprayer (not shown) for spraying a concentrated solution, and a heat exchange section 8 for removing the absorption heat generated in the absorber A.

The condenser C comprises a heat exchange section 11.

Each of the regenerators G ₃ , G ₂ , and G ₁ is for heating and concentrating the absorbing solution containing the refrigerant to obtain a concentrated solution having a high concentration in sequence. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium temperature regenerator G ₂ (“low temperature side regenerator” in the claims) that is configured with a solution heating unit 14 through which an external heat source J (for example, combustion gas or steam) passes. G corresponds to _n-1 ") is configured with a solution heating unit 9, and most low-temperature regenerator G ₁ operating at a low temperature (corresponding to" the lowest temperature side of the regenerator G ₁ "in the claims Is provided with a solution heating unit 10.

Each of the heat exchangers H ₁ , H ₂ , and H ₃ has a low-temperature concentrated solution L ₁ , a medium-temperature concentrated solution L ₂ , and a high-temperature concentrated solution produced by the regenerators G ₁ , G ₂ , and G _3. It is for recovering the heat of each of L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types,
For example, a plate heat exchanger may be used.

Each of the drain heat exchangers D ₁ and D ₂ is a vapor drain D produced by the low temperature regenerator G ₁ and the medium temperature regenerator G _2.
It recovers the heat of r ₁ and Dr ₂ to the dilute solution La side and is generally a shell-and-tube type heat exchanger, but is composed of another type such as a plate type heat exchanger. Is also good.

Each of these devices is operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the condenser C and the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30 to the evaporator E side. Supplied. The liquid refrigerant Rc supplied to the evaporator E is sprayed from the refrigerant distributor to the heat exchange section 7 side.

[0599] From the liquid to be cooled inlet pipe 45 to the heat exchange unit 7
The liquid to be cooled (water) We flowing in to and flowing out from the liquid to be cooled outlet pipe 46 is cooled by the heat of evaporation of the refrigerant. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

A dilute solution pipe 21 having a solution pump LP is connected to the bottom of the container 2 of the absorber A.
The dilute solution pipe 21 passes through the heated side of the low temperature solution heat exchanger H ₁ and then is supplied with the first branch pipe 21A and the second branch pipe 21.
It is branched into three routes of B and the third branch pipe 21C. Then, the first branch pipe 21A is connected to the high-temperature regenerator G ₃ through the heated side of the high-temperature solution heat exchanger H _3, the second branch pipe 21B is medium temperature solution heat exchanger H ₂
Is connected to the medium temperature regenerator G ₂ through the heated side of, and the third branch pipe 21C is connected to the low temperature regenerator G ₁ .

The medium temperature solution pipe 26 for guiding the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G ₂ is connected to the third branch pipe 21C after passing through the heating side of the medium temperature solution heat exchanger H _2. There is.

Therefore, the dilute solution flowing out of the absorber A is
La is the low temperature solution heat exchanger H₁After passing through the heated side of
Into three, one of which is the high temperature solution heat exchanger H₃
Through the high temperature regenerator G₃While flowing into the other
Medium temperature solution heat exchanger H₂Through the above medium temperature regenerator G₂Flow
And the other is the above medium temperature regenerator G₂Spilled from, medium temperature
Solution heat exchanger H₂Medium temperature concentrated solution L after passing through the heating side of₂Combined with
Flow the above low temperature regenerator G ₁Will flow into.

[0603] connected to said high-temperature regenerator G ₃ leads to a high temperature concentrated solution L ₃ exiting from the high temperature generator G _3, hot solution pipe 27 through the heating side of the high-temperature solution heat exchanger H _3, said bifurcated at a downstream side position of the high-temperature solution heat exchanger H _3, one branch pipe 27A is connected to the downstream side position of the medium-temperature solution heat exchanger H ₂ in the medium-temperature solution pipe 26, the other branch pipe 27B is cold concentrated guides the solution L ₁ merges with the low temperature solution pipe 25 the concentrated solution pipe 24, and the above low-temperature solution heat exchanger to flow out connected to the low temperature regenerator G ₁ from the cold regenerator G ₁ It is connected to the absorber A through the heating side of H ₁ .

Further, in the dilute solution pipe 21, the low temperature solution heat exchanger H ₁ is bypassed and passes through the heated side of the first drain heat exchanger D ₁ to pass the low temperature solution heat exchanger H _1. An absorption solution branch pipe 47 for connecting the front and the rear of the is provided.
The second branch pipe 21B bypasses the medium temperature solution heat exchanger H ₂ and passes through the heated side of the second drain heat exchanger D ₂ before and after the medium temperature solution heat exchanger H ₂ . An absorption solution branch pipe 48 for connecting the above is provided.

The solution heating unit 14 of the 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. Also, the high temperature regenerator G
The air chamber side of ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating unit 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is connected to the condenser C through the heating side of the second drain heat exchanger D _2. ing.

The solution heating unit 10 of the low temperature regenerator G ₁
The refrigerant drain pipe 35 connected to the outlet side of the
It is connected to the condenser C through the heating side of the drain heat exchanger D ₁ .

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The heat exchange section 8 of the absorber A and the heat exchange section 11 of the condenser C are connected via a cooling water pipe 42, and the cooling water W flowing in from the cooling water inlet pipe 41 side.
a performs a cooling action on the condenser C side,
Further, the absorber A side has a cooling effect and is discharged from the cooling water outlet pipe 43.

The absorption type refrigerating apparatus Z ₂₀ constitutes a circulation cycle of the refrigerant and the absorbing solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₂₀ will be specifically described.

The dilute solution La fed from the absorber A by the solution pump LP is the low temperature solution heat exchanger H.
Branched in ₁ immediately preceding, cold strong solution L ₁ and the high-temperature regenerator from the low temperature regenerator G ₁ portion thereof passing through the heating side by passing through the heated side of the low temperature solution heat exchanger H ₁ is a high temperature concentrated solution concentrated solution Lg and by heat exchange preheating part and is formed by confluence of L ₃ from G _3. Also, another portion is preheated by steam drain Dr ₁ exchanges heat from the low temperature generator G ₁ through the heated side by passing through the first heated side of the drain heat exchanger D ₁ . The dilute solutions La thus branched and individually preheated are merged again, and then branched again to the first branch pipe 21A side, the second branch pipe 21B side, and the third branch pipe 21C side. .

The dilute solution La branched to the side of the first branch pipe 21A exchanges heat with the high temperature concentrated solution L ₃ passing through the heated side of the high temperature solution heat exchanger H ₃ by passing through the heated side thereof. Preheated, and further, the exhaust heat exchanger K
After being preheated by exchanging heat with the residual heat Q of the external heat source J passing through the heated side by passing through the heated side thereof, it flows into the high temperature regenerator G ₃ . Then, the dilute solution La flowing into the high temperature regenerator G ₃ is subjected to the heating and concentrating action of the external heat source J to become a high temperature concentrated solution L ₃ and flows out, so that the heating side of the high temperature solution heat exchanger H ₃ is discharged. Pass through.

On the other hand, the dilute solution La branched to the side of the second branch pipe 21B is further branched immediately before the medium temperature solution heat exchanger H _{2 and} a part of it is heated by the medium temperature solution heat exchanger H ₂ . The intermediate temperature regenerator G that passes through the heating side
It is preheated by exchanging heat with the medium temperature concentrated solution L ₂ from ₂ . Also,
Another portion is preheated by steam drain Dr ₂ exchanges heat from the intermediate temperature regenerator G ₂ through the heating side by passing through the second heated side of the drain heat exchanger D _2.

The dilute solutions La thus branched and individually preheated are combined again, and then the intermediate temperature regenerator G is used.
₂ into the medium temperature regenerator G _{2 and the} high temperature regenerator G
_The medium is heated and concentrated by the refrigerant vapor R ₃ flowing into the solution heating section 9 from the ₃ side, becomes a medium temperature concentrated solution L ₂ and flows out, and after passing through the heating side of the medium temperature solution heat exchanger H ₂ , a high temperature concentrated solution L 2. It merges with a part of ₃ and flows into the low temperature regenerator G ₁ .

Further, the medium temperature concentrated solution L ₂ flowing into the low temperature regenerator G ₁ is cooled by the refrigerant vapor R ₂ flowing into the solution heating section 10 from the medium temperature regenerator G ₂ side in the low temperature regenerator G ₁ .
Is concentrated by heating to form a low temperature concentrated solution L ₁ and flows out.

[0618] Then, the low-temperature strong solution L ₁ and the portion of the hot concentrated solution L ₃ flowing out from the high temperature generator G ₃ side joins, the low-temperature solution heat exchanger H that flows from the low temperature regenerator G _{1 1}
Flows into the absorber A side through the heating side.

The above is the absorption refrigerating apparatus Z _{20 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

In the absorption type refrigeration system Z _{20 according} to the twentieth embodiment, the dilute solution La branched into three after passing through the low temperature solution heat exchanger H ₁ is regenerated by the regenerators G ₃ , G ₂ , respectively. Since it is configured to flow into G ₁ ,
In the medium temperature regenerator G ₂ , the unconcentrated dilute solution L
Since a flows in as it is, the concentration of the absorbing solution becomes lower than that in the case where the absorbing solution (concentrated solution) that has been heated and concentrated in the high temperature regenerator G ₃ flows in, and the boiling temperature becomes lower accordingly. , decrement the boiling temperature of the absorbent solution in the intermediate temperature regenerator G ₂ only, and thus capable of setting a low refrigerant vapor temperature at the high temperature generator G ₃ to be the heat source. As a result, the operating pressure of the high temperature regenerator G ₃ which is proportional to the refrigerant vapor temperature can be set low,
As a result, it is possible to provide an absorption type refrigeration system having a low operating pressure and good operability.

On the high temperature solution heat exchanger H ₃ side and the medium temperature solution heat exchanger H ₂ side, only the dilute solution La branched into three flows in. Compared with the case where the entire amount of the dilute solution La branched after passing through the solution heat exchanger H ₁ is flown into the high temperature solution heat exchanger H ₃ and the medium temperature solution heat exchanger H ₂ , the high temperature solution heat exchanger H ₃ Also, the flow rate in the medium temperature solution heat exchanger H ₂ is reduced, and the high temperature solution heat exchanger H ₃ and the medium temperature solution heat exchanger H ₂ can be made compact in response to the reduction in the flow rate.

Further, the dilute solution La from the absorber A is branched so that a part of the dilute solution La is made to flow into the high temperature regenerator G ₃ , so that, for example, the entire amount of the dilute solution La remains unchanged. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases. As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system Z ₂ is improved.

Also, the absorption type refrigeration system Z of this embodiment₂₀
Then, the high temperature regenerator G₃High temperature concentrated solution L from₃Is high above
Hot solution heat exchanger H₃After passing through the heating side of the
Part is the above-mentioned medium temperature regenerator G₂Medium temperature concentrated solution L from₂With above
Low temperature regenerator G₁Since it is configured to flow into
High temperature regenerator G₃High temperature concentrated solution L from₃And low temperature regenerator G₁Or
Low temperature concentrated solution L₁It will merge with
Organ G₁High temperature concentrated solution L ₃That a part of the
Finally, the concentrated solution L₃, L₁Pressure adjustment when merging
Alignment is easy, and solution merging can be performed smoothly.
It

Further, the absorption refrigerating apparatus Z _{20 of} this embodiment is also provided.
In this case, since the dilute solution La discharged from the absorber A is branched into three after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ and the medium temperature regenerator G ₂ are provided immediately before that. The dilute solution La that flows in via the high temperature solution heat exchanger H ₃ and the medium temperature solution heat exchanger H ₂ both flows in the preheated state in the low temperature solution heat exchanger H ₁ , and as a result, The required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the medium temperature regenerator G ₂ is reduced, and the thermal efficiency of the entire system can be expected to improve.

Also, the absorption type refrigeration system Z _{20 of} this embodiment
Then, the dilute solution L is generated by the residual heat Q after heating the high temperature regenerator G ₃ of the external heat source J for heating the high temperature regenerator G _3.
Since a is heated, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and further COP of the entire system can be expected to be further improved.

Furthermore, the absorption type refrigeration system Z of this embodiment
In _20, since the arrangement to heat the dilute solution La by the low temperature regenerator G ₁ and the intermediate temperature regenerator steam drain Dr ₁ resulted in G _2, Dr _2, the steam drain Dr _1, Dr ₂
The heat retained by the can be effectively used for preheating the diluted solution La, and the thermal efficiency of the entire system can be further promoted.

Further, the absorption type refrigeration system Z of this embodiment₂₀
Then, the diluted solution La is branched from the diluted solution pipe 21.
In the absorbed solution branch pipe 47, the first drain heat exchange is performed.
Exchanger D₁In addition, after branching from the second branch pipe 23
The second drain heat exchange in the absorbing solution branch pipe 48.
Bowl D₂Then, each of the dilute solutions La is replaced with the above-mentioned vapor drain Dr.₁，
Dr₂Since it is configured to heat by
Steam drain Dr₁, Dr ₂Absorption that is heated by the retained heat of
Since the amount of solution is small, the absorption solution can be efficiently preheated.
It

Further, the absorption type refrigeration system Z _{20 of} this embodiment is also provided.
Then, the system is configured by _three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ , but such a configuration requires a large number of regenerators. To increase the efficiency of the absorption solution by increasing the number of concentration stages of the absorption solution, and to increase the number of solution heat exchangers to increase the heat recovery rate, and the merit of improving the performance of the absorption refrigeration system, and the regenerator and When weighed against the disadvantage of increasing the manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. is there.

In the present embodiment, a part of the high temperature concentrated solution L ₃ flowing out from the high temperature regenerator G ₃ is replaced with the medium temperature regenerator G 3.
_The medium-temperature concentrated solution L ₂ flowing out from the medium ₂ is joined in the middle of the medium-temperature solution pipe 26, but a part of the high-temperature concentrated solution L ₃ is directly introduced into the low-temperature regenerator G _1. May be.

XXI: Twenty-first Embodiment FIG. 25 shows an operation cycle of the absorption refrigerating apparatus Z _{21 according} to the twenty-first embodiment of the present invention. The absorption type refrigerating apparatus Z ₂₁ is an absorption type refrigerating apparatus which uses water as a refrigerant and lithium bromide as an absorbing liquid, and includes one condenser C, an absorber A, an evaporator E, and three pieces each. Solution heat exchanger H ₃ ,
H ₂ and H ₁ and regenerators G ₃ , G ₂ and G ₁ are used as a basic configuration, and in addition to this, two drain heat exchangers D ₁ and D ₂ and one exhaust heat exchanger K are provided. These devices are operatively connected by a solution piping system and a refrigerant piping system to form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E comprises a heat exchange section 7 for passing the liquid We to be cooled and a refrigerant distributor (not shown) for distributing a refrigerant on the heat exchange section 7.

The absorber A comprises a solution sprayer (not shown) for spraying a concentrated solution, and a heat exchange section 8 for removing the absorption heat generated in the absorber A.

The condenser C comprises a heat exchange section 11.

Each of the regenerators G ₃ , G ₂ , and G ₁ is for heating and concentrating the absorption solution containing the refrigerant to successively obtain concentrated solutions of high concentration. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium temperature regenerator G ₂ (“low temperature side regenerator” in the claims) that is configured with a solution heating unit 14 through which an external heat source J (for example, combustion gas or steam) passes. G corresponds to _n-1 ") is configured with a solution heating unit 9, and most low-temperature regenerator G ₁ operating at a low temperature (corresponding to" the lowest temperature side of the regenerator G ₁ "in the claims Is provided with a solution heating unit 10.

Each of the heat exchangers H ₁ , H ₂ , and H ₃ has a low-temperature concentrated solution L ₁ , a medium-temperature concentrated solution L ₂ , and a high-temperature concentrated solution which are produced in the regenerators G ₁ , G ₂ , and G _3. It is for recovering the heat of each of L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types,
For example, a plate heat exchanger may be used.

Each of the drain heat exchangers D ₁ and D ₂ is a vapor drain D produced by the low temperature regenerator G ₁ and the intermediate temperature regenerator G _2.
It recovers the heat of r ₁ and Dr ₂ to the dilute solution La side and is generally a shell-and-tube type heat exchanger, but is composed of another type such as a plate type heat exchanger. Is also good.

Each of these devices is operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the condenser C and the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30 to the evaporator E side. Supplied. The liquid refrigerant Rc supplied to the evaporator E is sprayed from the refrigerant distributor to the heat exchange section 7 side.

From the cooled liquid inlet pipe 45 to the heat exchange section 7
The liquid to be cooled (water) We flowing in to and flowing out from the liquid to be cooled outlet pipe 46 is cooled by the heat of evaporation of the refrigerant. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

A dilute solution pipe 21 having a solution pump LP is connected to the bottom of the container 2 of the absorber A.
The dilute solution pipe 21 passes through the heated side of the low temperature solution heat exchanger H ₁ and then is supplied with the first branch pipe 21A and the second branch pipe 21.
It is branched into three routes of B and the third branch pipe 21C. Then, the first branch pipe 21A is connected to the high-temperature regenerator G ₃ through the heated side of the high-temperature solution heat exchanger H _3, the second branch pipe 21B is medium temperature solution heat exchanger H ₂
Is connected to the medium temperature regenerator G ₂ through the heated side of, and the third branch pipe 21C is connected to the low temperature regenerator G ₁ .

The medium temperature solution pipe 26 for guiding the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G ₂ is branched into two after passing through the heating side of the medium temperature solution heat exchanger H ₂ and one branch pipe. 26A is connected to the third branch pipe 21C, and the other branch pipe 26B is connected to the outlet side of the high temperature solution heat exchanger H _{3 in} the high temperature solution pipe 27.

Therefore, the dilute solution La flowing out of the absorber A is branched into three after passing through the heated side of the low temperature solution heat exchanger H ₁ , and _one of them is divided into the high temperature solution heat exchanger H ₃
While flowing into the high temperature regenerator G ₃ through the other, the other flows into the middle temperature regenerator G ₂ through the medium temperature solution heat exchanger H ₂ and the other flows out from the middle temperature regenerator G ₂ . After passing through the heating side of the medium temperature solution heat exchanger H ₂ , it joins with a part of the medium temperature concentrated solution L ₂ and flows into the low temperature regenerator G ₁ .

[0643] connected to said high-temperature regenerator G ₃ leads to a high temperature concentrated solution L ₃ exiting from the high temperature generator G _3, hot solution pipe 27 through the heating side of the high-temperature solution heat exchanger H ₃ is the The low temperature regenerator G ₁ is joined to the low temperature solution pipe 25 that guides the low temperature concentrated solution L ₁ flowing out from the low temperature regenerator G ₁ to form a concentrated solution pipe 24, which is the heating side of the low temperature solution heat exchanger H ₁ . And is connected to the absorber A through.

Further, in the dilute solution pipe 21, the low temperature solution heat exchanger H ₁ is bypassed and passes through the heated side of the first drain heat exchanger D ₁ and the low temperature solution heat exchanger H ₁ is passed. An absorption solution branch pipe 47 for connecting the front and the rear of the is provided.
The second branch pipe 21B bypasses the medium temperature solution heat exchanger H ₂ and passes through the heated side of the second drain heat exchanger D ₂ before and after the medium temperature solution heat exchanger H ₂ . An absorption solution branch pipe 48 for connecting the above is provided.

The solution heating section 14 of the 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. Also, the high temperature regenerator G
The air chamber side of ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is connected to the condenser C through the heating side of the second drain heat exchanger D _2. ing.

The solution heating section 10 of the low-temperature regenerator G ₁
The refrigerant drain pipe 35 connected to the outlet side of the
It is connected to the condenser C through the heating side of the drain heat exchanger D ₁ .

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The heat exchange section 8 of the absorber A and the heat exchange section 11 of the condenser C are connected via a cooling water pipe 42, and the cooling water W flowing in from the cooling water inlet pipe 41 side.
a performs a cooling action on the condenser C side,
Further, the absorber A side has a cooling effect and is discharged from the cooling water outlet pipe 43.

The absorption type refrigerating apparatus Z ₂₁ constitutes a circulation cycle of the refrigerant and the absorbing solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption type refrigerating apparatus Z ₂₁ will be specifically described.

The dilute solution La fed from the absorber A by the solution pump LP is the low temperature solution heat exchanger H.
Branched in ₁ immediately preceding, cold strong solution L ₁ and the high-temperature regenerator from the low temperature regenerator G ₁ portion thereof passing through the heating side by passing through the heated side of the low temperature solution heat exchanger H ₁ medium temperature from a high temperature concentrated solution L ₃ and the intermediate temperature regenerator G ₂ from G ₃ concentrated solution L ₂
Is preheated by exchanging heat with a concentrated solution Lg formed by merging with a part of. The other part is the first drain heat exchanger D ₁
When it passes through the heated side, it is preheated by exchanging heat with the steam drain Dr ₁ from the low temperature regenerator G ₁ passing through the heated side.
The dilute solution L branched and preheated individually in this way
a is merged again, and then again the first branch pipe 21A.
Side, the second branch pipe 21B side, and the third branch pipe 21C side.

The dilute solution La branched to the first branch pipe 21A side passes through the heated side of the high temperature solution heat exchanger H _{3 to} exchange heat with the high temperature concentrated solution L ₃ passing through the heated side. Preheated, and further, the exhaust heat exchanger K
After being preheated by exchanging heat with the residual heat Q of the external heat source J passing through the heated side by passing through the heated side thereof, it flows into the high temperature regenerator G ₃ . Then, the dilute solution La flowing into the high temperature regenerator G ₃ is subjected to the heating and concentrating action of the external heat source J to become a high temperature concentrated solution L ₃ and flows out, so that the heating side of the high temperature solution heat exchanger H ₃ is discharged. Pass through.

On the other hand, the dilute solution La branched to the side of the second branch pipe 21B is further branched immediately before the medium temperature solution heat exchanger H _{2 and} a part of it is heated by the medium temperature solution heat exchanger H ₂ . The intermediate temperature regenerator G that passes through the heating side
It is preheated by exchanging heat with the medium temperature concentrated solution L ₂ from ₂ . Also,
Another portion is preheated by steam drain Dr ₂ exchanges heat from the intermediate temperature regenerator G ₂ through the heating side by passing through the second heated side of the drain heat exchanger D _2.

The dilute solutions La thus branched and individually preheated are combined again, and then the intermediate temperature regenerator G is used.
₂ into the medium temperature regenerator G _{2 and the} high temperature regenerator G
The solution is heated and concentrated by the refrigerant vapor R ₃ flowing into the solution heating section 9 from the ₃ side, flows out as a medium temperature concentrated solution L ₂ , passes through the heating side of the medium temperature solution heat exchanger H ₂ , and then branches. A part of the diluted solution La flows through the third branch pipe 21C.
Merges with and flows into the low temperature regenerator G ₁ . The other part merges with the high temperature concentrated solution L ₃ flowing through the high temperature solution pipe 27.

Further, the concentrated solution obtained by merging a part of the medium-temperature concentrated solution L ₂ flowing into the low-temperature regenerator G ₁ and the dilute solution La is the medium-temperature regenerator G ₂ side in the low-temperature regenerator G ₁ . Is heated and concentrated by the refrigerant vapor R ₂ flowing into the solution heating unit 10 from the above, and flows out as a low temperature concentrated solution L ₁ .

Then, the low temperature concentrated solution L ₁ flowing out from the low temperature regenerator G _1, a part of the high temperature concentrated solution L ₃ flowing out from the high temperature regenerator G ₃ side and the medium temperature concentrated solution flowing out from the intermediate temperature regenerator G _{2 are} discharged. It merges with a part of the solution L ₂ , and the low temperature solution heat exchanger H ₁
Flows into the absorber A side through the heating side.

The above is the absorption refrigerating apparatus Z _{21 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

In the absorption refrigeration system Z _{21 according} to the 21st embodiment, the diluted solution La branched into three after passing through the low temperature solution heat exchanger H ₁ is regenerated by the regenerators G ₃ , G ₂ , Since it is configured to flow into G ₁ ,
In the medium temperature regenerator G ₂ , the unconcentrated dilute solution L
Since a flows in as it is, the concentration of the absorbing solution becomes lower than that in the case where the absorbing solution (concentrated solution) that has been heated and concentrated in the high temperature regenerator G ₃ flows in, and the boiling temperature becomes lower accordingly. , decrement the boiling temperature of the absorbent solution in the intermediate temperature regenerator G ₂ only, and thus capable of setting a low refrigerant vapor temperature at the high temperature generator G ₃ to be the heat source. As a result, the operating pressure of the high temperature regenerator G ₃ which is proportional to the refrigerant vapor temperature can be set low,
As a result, it is possible to provide an absorption type refrigeration system having a low operating pressure and good operability.

On the high temperature solution heat exchanger H ₃ side and the medium temperature solution heat exchanger H ₂ side, only the dilute solution La branched into three flows in. Compared with the case where the entire amount of the dilute solution La branched after passing through the solution heat exchanger H ₁ is flown into the high temperature solution heat exchanger H ₃ and the medium temperature solution heat exchanger H ₂ , the high temperature solution heat exchanger H ₃ Also, the flow rate in the medium temperature solution heat exchanger H ₂ is reduced, and the high temperature solution heat exchanger H ₃ and the medium temperature solution heat exchanger H ₂ can be made compact in response to the reduction in the flow rate.

Furthermore, the dilute solution La from the absorber A is branched so that a part of the dilute solution La is made to flow into the high temperature regenerator G ₃ , so that, for example, the entire amount of the dilute solution La remains unchanged. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases. As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system Z ₂ is improved.

Also, the absorption type refrigeration system Z _{21 of} this embodiment.
In medium temperature concentrated solution L ₂ from the intermediate temperature regenerator G ₂ is branched after passing through the heating side of the medium-temperature solution heat exchanger H _2, the high-temperature part thereof flows out from the high temperature generator G ₃ Since it is configured so as to join with the high temperature concentrated solution L ₃ that has passed through the heating side of the solution heat exchanger H _3, the amount of concentrated solution flowing into the low temperature regenerator G ₁ is reduced, and the low temperature regenerator G ₁ The amount of heat required for the regeneration (in other words, the evaporation of the refrigerant vapor) is small. Therefore, the thermal efficiency in the low temperature regenerator G ₁ is improved.

Further, the absorption type refrigeration system Z _{21 of} this embodiment is also provided.
In this case, since the dilute solution La discharged from the absorber A is branched into three after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ and the medium temperature regenerator G ₂ are provided immediately before that. The dilute solution La that flows in via the high temperature solution heat exchanger H ₃ and the medium temperature solution heat exchanger H ₂ both flows in the preheated state in the low temperature solution heat exchanger H ₁ , and as a result, The required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the medium temperature regenerator G ₂ is reduced, and the thermal efficiency of the entire system can be expected to improve.

Further, the absorption type refrigeration system Z _{21 of} this embodiment is also provided.
Then, the dilute solution L is generated by the residual heat Q after heating the high temperature regenerator G ₃ of the external heat source J for heating the high temperature regenerator G _3.
Since a is heated, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and further COP of the entire system can be expected to be further improved.

Furthermore, the absorption type refrigeration system Z of this embodiment
In _21, since the arrangement to heat the dilute solution La by the low temperature regenerator G ₁ and the intermediate temperature regenerator steam drain Dr ₁ resulted in G _2, Dr _2, the steam drain Dr _1, Dr ₂
The heat retained by the can be effectively used for preheating the diluted solution La, and the thermal efficiency of the entire system can be further promoted.

Also, the absorption type refrigeration system Z of this embodiment_{twenty one}
Then, the diluted solution La is branched from the diluted solution pipe 21.
In the absorbed solution branch pipe 47, the first drain heat exchange is performed.
Exchanger D₁In addition, after branching from the second branch pipe 23
The second drain heat exchange in the absorbing solution branch pipe 48.
Bowl D₂Then, each of the dilute solutions La is replaced with the above-mentioned vapor drain Dr.₁，
Dr₂Since it is configured to heat by
Steam drain Dr₁, Dr ₂Absorption that is heated by the retained heat of
Since the amount of solution is small, the absorption solution can be efficiently preheated.
It

Further, the absorption type refrigeration system Z _{21 of} this embodiment is also provided.
Then, the system is configured by _three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ , but such a configuration requires a large number of regenerators. To increase the efficiency of the absorption solution by increasing the number of concentration stages of the absorption solution, and to increase the number of solution heat exchangers to increase the heat recovery rate, and the merit of improving the performance of the absorption refrigeration system, and the regenerator and When weighed against the disadvantage of increasing the manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. is there.

XXII: Twenty-second Embodiment FIG. 26 shows the operation cycle of the absorption refrigerating apparatus Z _{22 according} to the 22nd embodiment of the present invention. The absorption type refrigerating apparatus Z ₂₂ is an absorption type refrigerating apparatus which uses water as a refrigerant and lithium bromide as an absorbing liquid, and includes one condenser C, an absorber A, an evaporator E, and three pieces each. Solution heat exchanger H ₃ ,
H ₂ and H ₁ and regenerators G ₃ , G ₂ and G ₁ are used as a basic configuration, and in addition to this, two drain heat exchangers D ₁ and D ₂ and one exhaust heat exchanger K are provided. And a solution piping system and a refrigerant piping system are operatively connected to form a circulation cycle of the refrigerant and the absorbing solution.

[0670] The evaporator E comprises a heat exchange part 7 for passing the liquid We to be cooled and a refrigerant sprayer 13 for spraying the refrigerant Re on the heat exchange part 7 in the container 1.

In the above-mentioned absorber A, the container 2 is filled with the concentrated solution Lg.
And a heat exchange section 8 for removing absorption heat generated in the absorber A. The condenser C is configured by including the heat exchange section 11 in the container 6.

Each of the regenerators G ₃ , G ₂ and G ₁ is for heating and concentrating the absorption solution containing the refrigerant to obtain a concentrated solution having a high concentration one after another. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium-temperature regenerator G ₂ that operates at a medium temperature and is configured to have an external heat source J (for example, combustion gas or steam) inside the container 3 (the “low-temperature side regenerator G _n in the claims”). _-1 "
Applicable) to is configured with a solution heating unit 9 in the container 4, corresponding to the even most low temperature regenerator G ₁ ( "lowest temperature side of the regenerator G _1" in the claims which operates at a low temperature )
Is provided with a solution heating unit 10 in the container 5.

The solution heat exchangers H ₁ , H ₂ and H ₃ are the low temperature concentrated solutions L ₁ and L ₁ produced by the regenerators G ₁ , G ₂ and G ₃ , respectively.
This is for recovering the heat of each of the medium-temperature concentrated solution L ₂ and the high-temperature concentrated solution L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types For example, it may be configured by a plate heat exchanger.

Each of these devices is operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the container 6 of the condenser C and the container 1 of the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30. It is supplied to the evaporator E side. Further, the liquid refrigerant Rc supplied to the evaporator E is the refrigerant pump RP.
By means of the liquid refrigerant pipe 29, a refrigerant distributor (not shown)
And is sprayed as a refrigerant Re from the refrigerant distributor (not shown) to the heat exchange section 7 side.

[0676] From the liquid to be cooled inlet pipe 45 to the heat exchanging portion 7
The liquid to be cooled (water) We that flows in to and flows out from the liquid to be cooled outlet pipe 46 is cooled by the heat of vaporization of the refrigerant Re. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

A dilute solution pipe 21 having a solution pump LP is connected to the bottom of the container 2 of the absorber A.
The dilute solution pipe 21 passes through the heated side of the low temperature solution heat exchanger H ₁ and then is supplied with the first branch pipe 21A and the second branch pipe 21.
It is branched into two routes of B. The first branch pipe 21A is connected to the high temperature regenerator G ₃ through the heated side of the high temperature solution heat exchanger H ₃ . The second branch pipe 21B is connected to the medium temperature regenerator G ₂ through the heated side of the medium temperature solution heat exchanger H ₂ . Therefore, the dilute solution La flowing out of the absorber A branches after passing through the heated side of the low temperature solution heat exchanger H ₁ , and _one of them branches through the high temperature solution heat exchanger H ₃ to the high temperature regenerator. It flows into G ₃ , and the other flows into the intermediate temperature regenerator G ₂ via the intermediate temperature solution heat exchanger H ₂ .

[0678] lead to medium temperature concentrated solution L ₂ which flows out is connected to the intermediate temperature regenerator G ₂ from intermediate temperature regenerator G _2, the medium-temperature solution line 26 through the heating side of the medium-temperature solution heat exchanger H ₂ is the It is connected to the low temperature regenerator G ₁ .

Further, the high temperature solution pipe 27 is branched at the outlet side of the high temperature solution heat exchanger H ₃ , and one branch pipe 27A is connected to the medium temperature regenerator G ₂ to be connected to the medium temperature regenerator G _2. From the medium temperature solution heat exchanger H _{2 in} the medium temperature solution pipe 26 for guiding the medium temperature concentrated solution L ₂ flowing out of the low temperature regenerator G _1.
Connected to the low temperature regenerator G ₁ and flowing into the low temperature concentrated solution L ₁ leading the low temperature concentrated solution L ₁ to join the low temperature concentrated solution pipe 25.
And is connected to the absorber A through the heating side of the low temperature solution heat exchanger H ₁ .

Further, the dilute solution pipe 21 bypasses the low temperature solution heat exchanger H ₁ and passes through the heated side of the first drain heat exchanger D ₁ to pass the low temperature solution heat exchanger H ₁ An absorption solution branch pipe 47 for connecting the front and the rear of the is provided.
The second branch pipe 21B bypasses the medium temperature solution heat exchanger H ₂ and passes through the heated side of the second drain heat exchanger D ₂ before and after the medium temperature solution heat exchanger H ₂ . An absorption solution branch pipe 48 for connecting the above is provided.

The solution heating section 14 of the 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. Also, the high temperature regenerator G
The air chamber side of ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is connected to the condenser C through the heating side of the second drain heat exchanger D _2. ing.

The solution heating section 10 of the low-temperature regenerator G ₁
The refrigerant drain pipe 35 connected to the outlet side of the
It is connected to the condenser C through the heating side of the drain heat exchanger D ₁ .

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The heat exchange section 8 of the absorber A and the heat exchange section 11 of the condenser C are connected via a cooling water pipe 42, and the cooling water W flowing in from the cooling water inlet pipe 41 side.
a performs a cooling action on the condenser C side,
Further, the absorber A side has a cooling effect and is discharged from the cooling water outlet pipe 43.

The absorption type refrigerating apparatus Z ₂₂ constitutes a circulation cycle of the refrigerant and the absorption solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₂₂ will be specifically described.

The dilute solution La fed from the absorber A by the solution pump LP is the low temperature solution heat exchanger H.
Branched in ₁ immediately preceding, cold strong solution L ₁ and the high-temperature regenerator from the low temperature regenerator G ₁ portion thereof passing through the heating side by passing through the heated side of the low temperature solution heat exchanger H ₁ It is concentrated solution Lg preheating by heat exchange made by merging the high-temperature concentrated solution L ₃ from G _3. Also, another portion is preheated by steam drain Dr ₁ exchanges heat from the low temperature generator G ₁ through the heated side by passing through the first heated side of the drain heat exchanger D ₁ . The diluted solutions La thus branched and individually preheated are merged again, and then branched again to the first branch pipe 21A side and the second branch pipe 21B side.

The dilute solution La branched to the side of the first branch pipe 21A exchanges heat with the high temperature concentrated solution L ₃ passing through the heated side of the high temperature solution heat exchanger H ₃ by passing through the heated side thereof. Preheated, and further, the exhaust heat exchanger K
After being preheated by exchanging heat with the residual heat Q of the external heat source J passing through the heated side by passing through the heated side thereof, it flows into the high temperature regenerator G ₃ . Then, the dilute solution La flowing into the high temperature regenerator G ₃ is subjected to the heating and concentrating action of the external heat source J to become a high temperature concentrated solution L ₃ and flows out, so that the heating side of the high temperature solution heat exchanger H ₃ is discharged. After passing through, it branched off, part of it
It joins the medium-temperature concentrated solution L ₂ and the outlet side of the medium-temperature solution heat exchanger of H ₂ from the intermediate temperature generator G _2. The other part joins with the low temperature concentrated solution L ₁ flowing out from the low temperature generator G ₁ .

On the other hand, the dilute solution La branched to the side of the second branch pipe 21B is further branched immediately before the medium temperature solution heat exchanger H _{2 and} a part of it is heated by the medium temperature solution heat exchanger H ₂ . The intermediate temperature regenerator G that passes through the heating side
It is preheated by exchanging heat with the medium temperature concentrated solution L ₂ from ₂ . Also,
Another portion is preheated by steam drain Dr ₂ exchanges heat from the intermediate temperature regenerator G ₂ through the heating side by passing through the second heated side of the drain heat exchanger D _2.

The dilute solutions La thus branched and individually preheated are combined again, and then the intermediate temperature regenerator G is used.
₂ into the medium temperature regenerator G _{2 and the} high temperature regenerator G
The low temperature regenerator G is heated and concentrated by the refrigerant vapor R ₃ flowing into the solution heating section 9 from the ₃ side, flows out as a medium temperature concentrated solution L ₂ , passes through the heating side of the medium temperature solution heat exchanger H _2. Inflow to ₁ .

Further, the concentrated solution obtained by merging the medium-temperature concentrated solution L ₂ and a part of the high-temperature concentrated solution L ₃ which have flowed into the low-temperature regenerator G ₁ is mixed in the low-temperature regenerator G ₁ with the medium-temperature regenerator G ₁ . The solution is heated and concentrated by the refrigerant vapor R ₂ flowing into the solution heating unit 10 from the _2nd side, and flows out as a low temperature concentrated solution L ₁ .

[0694] Then, the low-temperature strong solution L ₁ and the portion of the hot concentrated solution L ₃ flowing out from the high temperature generator G ₃ side joins, the low-temperature solution heat exchanger H that flows from the low temperature regenerator G _{1 1}
Flows into the absorber A side through the heating side.

The above is the absorption refrigerating apparatus Z _{22 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

Absorption refrigeration according to the 22nd embodiment
Device Z_{twenty two}In, the diluted solution La discharged from the absorber A is
One of them is diverged, and the other one is regenerated at high temperature with the entire amount of branching.
Bowl G ₃To the other side, and the other one recovers the entire amount of branching at the above intermediate temperature.
Bowl G₂Flow into the low temperature regenerator G₁Flowing into
Since it is configured to operate, the above-mentioned medium temperature regenerator G₂To
In this case, the unconcentrated dilute solution La flows in as it is.
Thus, for example, the high temperature regenerator G₃Condensed with heating concentrated in
Absorption solution as compared to the case where a collection solution (concentrated solution) is flowed in
The lower the concentration, the lower the boiling temperature.
This medium temperature regenerator G ₂Of boiling temperature of absorbing solution in water
The high temperature regenerator G that serves as the heat source₃In
Since the refrigerant vapor temperature can be set low,
The high temperature regenerator G proportional to the temperature of the refrigerant vapor₃Operating pressure
Can be set lower, resulting in lower operating pressure
It is possible to provide an absorption type refrigerating device with good operability.
It will be.

Also, by diluting the dilute solution La from the absorber A and allowing a part of the dilute solution La to flow into the high temperature regenerator G ₃ , for example, the entire amount of the dilute solution La remains unchanged. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system Z ₁ is improved.

[0698] Further, a part of it which is adapted to flow into the said high temperature regenerator G ₃ is branched dilute solution La from the absorber A, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution L flowing in here is supplied.
As the amount of a decreases, the heat transfer area can be reduced to make the device compact, which in turn contributes to making the absorption refrigeration system Z ₁ compact.

Also, the absorption type refrigeration system Z of this embodiment_{twenty two}
Then, the high temperature regenerator G₃High temperature concentrated solution L from₃Is high above
Hot solution heat exchanger H₃After passing through the heating side of the
Part is the above-mentioned medium temperature regenerator G₂Medium temperature concentrated solution L from₂With above
Low temperature regenerator G₁Since it is configured to flow into
High temperature regenerator G₃High temperature concentrated solution L from₃And low temperature regenerator G₁Or
Low temperature concentrated solution L₁It will merge with
Organ G₁High temperature concentrated solution L ₃That a part of the
Finally, the concentrated solution L₃, L₁Pressure adjustment when merging
Alignment is easy, and solution merging can be performed smoothly.
It

Also, the absorption refrigerating apparatus Z _{22 of} this embodiment is used.
In this case, since the diluted solution La discharged from the absorber A is branched after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ is passed through the high temperature solution heat exchanger H ₃ immediately before it. And the dilute solution La flowing into the medium temperature regenerator G ₂ via the medium temperature solution heat exchanger H ₂ immediately before it.
Means that both flow into the low temperature solution heat exchanger H ₁ in a preheated state, and as a result, the required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ decreases. It can be expected that the thermal efficiency of the entire system will be improved.

Further, the absorption type refrigeration system Z _{22 of} this embodiment is also provided.
Then, the dilute solution L is generated by the residual heat Q after heating the high temperature regenerator G ₃ of the external heat source J for heating the high temperature regenerator G _3.
Since a is heated, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and further COP of the entire system can be expected to be further improved.

Further, the absorption type refrigerating apparatus Z of this embodiment
In _22, since the arrangement to heat the dilute solution La by the low temperature regenerator G ₁ and the intermediate temperature regenerator steam drain Dr ₁ resulted in G _2, Dr _2, the steam drain Dr _1, Dr ₂
The heat retained by the can be effectively used for preheating the diluted solution La, and the thermal efficiency of the entire system can be further promoted.

Further, the absorption type refrigerating apparatus Z of this embodiment_{twenty two}
Then, the diluted solution La is branched from the diluted solution pipe 21.
In the absorbed solution branch pipe 47, the first drain heat exchange is performed.
Exchanger D₁In addition, after branching from the second branch pipe 23
The second drain heat exchange in the absorbing solution branch pipe 48.
Bowl D₂Then, each of the dilute solutions La is replaced with the above-mentioned vapor drain Dr.₁，
Dr₂Since it is configured to heat by
Steam drain Dr₁, Dr ₂Absorption that is heated by the retained heat of
Since the amount of solution is small, the absorption solution can be efficiently preheated.
It

Further, the absorption type refrigeration system Z _{22 of} this embodiment is also provided.
Then, the system is configured by _three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ , but such a configuration requires a large number of regenerators. To increase the efficiency of the absorption solution by increasing the number of concentration stages of the absorption solution, and to increase the number of solution heat exchangers to increase the heat recovery rate, and the merit of improving the performance of the absorption refrigeration system, and the regenerator and When weighed against the disadvantage of increasing the manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. is there.

XXIII: Twenty-third Embodiment FIG. 27 shows an operation cycle of an absorption type refrigerating machine Z23 according to a _twenty- third embodiment of the present invention. The absorption refrigerating apparatus Z ₂₃ is an absorption refrigerating apparatus that uses water as a refrigerant and lithium bromide as an absorbing liquid, and includes one condenser C, one absorber A, one evaporator E, and three each. Solution heat exchanger H ₃ ,
H ₂ and H ₁ and regenerators G ₃ , G ₂ and G ₁ are used as a basic configuration, and in addition to this, two drain heat exchangers D ₁ and D ₂ and one exhaust heat exchanger K are provided. And a solution piping system and a refrigerant piping system are operatively connected to form a circulation cycle of the refrigerant and the absorbing solution.

The evaporator E is provided with a heat exchange part 7 for passing the liquid to be cooled We in the container 1, and a refrigerant sprayer 13 for spraying the refrigerant Re on the heat exchange part 7.

[0707] The absorber A has a container 2 in which the concentrated solution Lg is
And a heat exchange section 8 for removing absorption heat generated in the absorber A. The condenser C is configured by including the heat exchange section 11 in the container 6.

Each of the regenerators G ₃ , G ₂ and G ₁ is for heating and concentrating the absorbing solution containing the refrigerant to successively obtain concentrated solutions of high concentration. High-temperature regenerator G ₃ which has different operating temperatures and operates at the highest temperature (the “highest-temperature-side regenerator G _n ” in the claims)
Is a medium-temperature regenerator G ₂ that operates at a medium temperature and is configured to have an external heat source J (for example, combustion gas or steam) inside the container 3 (the “low-temperature side regenerator G _n in the claims”). _-1 "
Applicable) to is configured with a solution heating unit 9 in the container 4, corresponding to the even most low temperature regenerator G ₁ ( "lowest temperature side of the regenerator G _1" in the claims which operates at a low temperature )
Is provided with a solution heating unit 10 in the container 5.

The solution heat exchangers H ₁ , H ₂ and H ₃ are the low temperature concentrated solution L ₁ produced by the regenerators G ₁ , G ₂ and G ₃ , respectively.
This is for recovering the heat of each of the medium-temperature concentrated solution L ₂ and the high-temperature concentrated solution L ₃ to the dilute solution La side, and is generally a shell-and-tube heat exchanger, but other types For example, it may be configured by a plate heat exchanger.

Each of these devices is operatively connected as follows by a solution piping system and a refrigerant piping system.

That is, the container 6 of the condenser C and the container 1 of the evaporator E are connected by the liquid refrigerant pipe 30, and the liquid refrigerant Rc generated in the condenser C is passed through the liquid refrigerant pipe 30. It is supplied to the evaporator E side. Further, the liquid refrigerant Rc supplied to the evaporator E is the refrigerant pump RP.
By means of the liquid refrigerant pipe 29, a refrigerant distributor (not shown)
And is sprayed as a refrigerant Re from the refrigerant distributor (not shown) to the heat exchange section 7 side.

From the liquid to be cooled inlet pipe 45 to the heat exchanging portion 7
The liquid to be cooled (water) We that flows in to and flows out from the liquid to be cooled outlet pipe 46 is cooled by the heat of vaporization of the refrigerant Re. Further, the vaporized refrigerant Ra generated in the evaporator E by being sprayed to the heat exchange section 7 is directly transferred to the absorber A side.

A dilute solution pipe 21 equipped with a solution pump LP is connected to the bottom of the container 2 of the absorber A.
The dilute solution pipe 21 passes through the heated side of the low temperature solution heat exchanger H ₁ and then is supplied with the first branch pipe 21A and the second branch pipe 21.
It is branched into two routes of B. The first branch pipe 21A is connected to the high temperature regenerator G ₃ through the heated side of the high temperature solution heat exchanger H ₃ . The second branch pipe 21B is connected to the medium temperature regenerator G ₂ through the heated side of the medium temperature solution heat exchanger H ₂ . Therefore, the dilute solution La flowing out of the absorber A branches after passing through the heated side of the low temperature solution heat exchanger H ₁ , and _one of them branches through the high temperature solution heat exchanger H ₃ to the high temperature regenerator. It flows into G ₃ , and the other flows into the intermediate temperature regenerator G ₂ via the intermediate temperature solution heat exchanger H ₂ .

The medium temperature solution pipe 26 connected to the medium temperature regenerator G ₂ guides the medium temperature concentrated solution L ₂ flowing out from the medium temperature regenerator G _2, and the medium temperature solution pipe 26 passing through the heating side of the medium temperature solution heat exchanger H ₂ is The branch line on the outlet side of the medium temperature solution heat exchanger H ₂ is branched, one branch pipe 26A is connected to the low temperature regenerator G ₁ , and the other branch pipe 26B is the high temperature concentrated solution flowing out from the high temperature generator G _3. leads to L _3, and is connected to the outlet side of the high temperature solution heat exchanger H ₃ in hot solution pipe 27 through the heating side of the high-temperature solution heat exchanger H _3.

[0715] Also, the hot solution pipe 27, low-temperature solution pipe 25 concentrated solution joins the pipe 24 for guiding the cold concentrated solution L ₁ which flows out is connected to the low temperature regenerator G ₁ from the cold regenerator G ₁ And is connected to the absorber A through the heating side of the low temperature solution heat exchanger H ₁ .

Further, the dilute solution pipe 21 bypasses the low temperature solution heat exchanger H ₁ and passes through the heated side of the first drain heat exchanger D ₁ and passes through the low temperature solution heat exchanger H ₁ An absorption solution branch pipe 47 for connecting the front and the rear of the is provided.
The second branch pipe 21B bypasses the medium temperature solution heat exchanger H ₂ and passes through the heated side of the second drain heat exchanger D ₂ before and after the medium temperature solution heat exchanger H ₂ . An absorption solution branch pipe 48 for connecting the above is provided.

The solution heating section 14 of the 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. Also, the high temperature regenerator G
The air chamber side of ₃ is connected to the inlet side of the solution heating section 9 of the medium temperature regenerator G ₂ via a high temperature steam pipe 31.

The air chamber side of the medium temperature regenerator G ₂ is connected to the inlet side of the solution heating section 10 of the low temperature regenerator G ₁ via a medium temperature steam pipe 32.

The refrigerant drain pipe 34 connected to the outlet side of the solution heating section 9 of the medium temperature regenerator G ₂ is connected to the condenser C through the heating side of the second drain heat exchanger D _2. ing.

The solution heating section 10 of the low temperature regenerator G ₁
The refrigerant drain pipe 35 connected to the outlet side of the
It is connected to the condenser C through the heating side of the drain heat exchanger D ₁ .

The refrigerant generated in the low temperature regenerator G ₁ is transferred to the condenser C through the refrigerant passage 33.

The heat exchange section 8 of the absorber A and the heat exchange section 11 of the condenser C are connected via a cooling water pipe 42, and the cooling water W flowing in from the cooling water inlet pipe 41 side.
a performs a cooling action on the condenser C side,
Further, the absorber A side has a cooling effect and is discharged from the cooling water outlet pipe 43.

The absorption type refrigerating apparatus Z ₂₃ constitutes a circulation cycle of the refrigerant and the absorbing solution by adopting the above equipment arrangement and path configuration.

Next, the operation cycle of the absorption refrigerating apparatus Z ₂₃ will be specifically described.

The dilute solution La fed from the absorber A by the solution pump LP is the low temperature solution heat exchanger H.
Branched in ₁ immediately preceding, cold strong solution L ₁ and the high-temperature regenerator from the low temperature regenerator G ₁ portion thereof passing through the heating side by passing through the heated side of the low temperature solution heat exchanger H ₁ It is concentrated solution Lg preheating by heat exchange made by merging the high-temperature concentrated solution L ₃ from G _3. Also, another portion is preheated by steam drain Dr ₁ exchanges heat from the low temperature generator G ₁ through the heated side by passing through the first heated side of the drain heat exchanger D ₁ . The diluted solutions La thus branched and individually preheated are merged again, and then branched again to the first branch pipe 21A side and the second branch pipe 21B side.

The dilute solution La branched to the first branch pipe 21A side exchanges heat with the high temperature concentrated solution L ₃ passing through the heated side of the high temperature solution heat exchanger H ₃ by passing through the heated side thereof. Preheated, and further, the exhaust heat exchanger K
After being preheated by exchanging heat with the residual heat Q of the external heat source J passing through the heated side by passing through the heated side thereof, it flows into the high temperature regenerator G ₃ . Then, the dilute solution La flowing into the high temperature regenerator G ₃ is subjected to the heating and concentrating action of the external heat source J to become a high temperature concentrated solution L ₃ and flows out, so that the heating side of the high temperature solution heat exchanger H ₃ is discharged. After passing, it joins with the low temperature concentrated solution L ₁ flowing out from the low temperature generator G ₁ .

On the other hand, the dilute solution La branched to the side of the second branch pipe 21B is further branched immediately before the medium temperature solution heat exchanger H _{2 and} a part of it is heated by the medium temperature solution heat exchanger H ₂ . The intermediate temperature regenerator G that passes through the heating side
It is preheated by exchanging heat with the medium temperature concentrated solution L ₂ from ₂ . Also,
Another portion is preheated by steam drain Dr ₂ exchanges heat from the intermediate temperature regenerator G ₂ through the heating side by passing through the second heated side of the drain heat exchanger D _2. Thus branched and dilute solution La preheated individually, after merging again flows into the intermediate temperature regenerator G _2, middle temperature regenerator G ₂ the solution heated from the high temperature generator G ₃ side in It is heated and concentrated by the refrigerant vapor R ₃ flowing into the portion 9, and flows out as a medium-temperature concentrated solution L ₂ .

The medium-temperature concentrated solution L ₂ branches after passing through the heating side of the medium-temperature solution heat exchanger H ₂ , part of which flows into the low-temperature regenerator G ₁ , and part of which flows into the low-temperature regenerator G _1. It flows out from the high-temperature generator G ₃ joins the hot concentrated solution L ₃ after passing through the high temperature solution heat exchanger H _3.

Further, the low temperature regenerator G₁While flowing into
Hot concentrated solution L₂Part of the low temperature regenerator G₁In the above
Temperature regenerator G₂Refrigerant flowing into the solution heating unit 10 from the side
Steam R ₂Heat concentrated by low temperature concentrated solution L₁Become
leak.

Then, the low temperature concentrated solution L ₁ flowing out from the low temperature regenerator G _1, the high temperature concentrated solution L ₃ flowing out from the high temperature regenerator G ₃ side and the medium temperature solution heat flowing out from the intermediate temperature generator G ₂ are heated. medium temperature branched at the outlet side of the exchanger H ₂ concentrated solution L ₂
, And then flows into the absorber A side through the heating side of the low temperature solution heat exchanger H ₁ .

The above is the absorption refrigeration apparatus Z _{23 of} this embodiment.
In the operation cycle, the following unique action and effects are obtained.

Absorption refrigeration according to the 23rd embodiment
Device Z_{twenty three}In, the diluted solution La discharged from the absorber A is
One of them is diverged, and the other one is regenerated at high temperature with the entire amount of branching.
Bowl G ₃To the other side, and the other one recovers the entire amount of branching at the above intermediate temperature.
Bowl G₂Flow into the low temperature regenerator G₁Flowing into
Since it is configured to operate, the above-mentioned medium temperature regenerator G₂To
In this case, the unconcentrated dilute solution La flows in as it is.
Thus, for example, the high temperature regenerator G₃Condensed with heating concentrated in
Absorption solution as compared to the case where a collection solution (concentrated solution) is flowed in
The lower the concentration, the lower the boiling temperature.
This medium temperature regenerator G ₂Of boiling temperature of absorbing solution in water
The high temperature regenerator G that serves as the heat source₃In
Since the refrigerant vapor temperature can be set low,
The high temperature regenerator G proportional to the temperature of the refrigerant vapor₃Operating pressure
Can be set lower, resulting in lower operating pressure
It is possible to provide an absorption type refrigerating device with good operability.
It will be.

Further, the dilute solution La from the absorber A is branched so that a part of the dilute solution La is made to flow into the high temperature regenerator G ₃ , so that, for example, the entire amount of the dilute solution La remains unchanged. _As compared with the case of flowing into the high temperature regenerator ₃ , the flow rate of the dilute solution La into the high temperature regenerator G ₃ decreases.
As a result, in the high-temperature regenerator G _3, wherein since the amount corresponding the sensible heat amount is small in the absorption solution which is heated to boiling is reduced, a much needed heat of the high temperature regenerator G ₃ calorimetry (i.e., The amount of heat input to the high temperature regenerator G ₃ is also small, the COP of the entire system is improved, and the efficiency of the absorption refrigeration system Z ₁ is improved.

[0734] Further, a part of it which is adapted to flow into the said high temperature regenerator G ₃ is branched dilute solution La from the absorber A, the high temperature solution heat immediately before the high-temperature regenerator G ₃ In the exchanger H ₃ , the dilute solution L flowing in here is supplied.
As the amount of a decreases, the heat transfer area can be reduced to make the device compact, which in turn contributes to making the absorption refrigeration system Z ₁ compact.

Further, the absorption refrigeration system Z _{23 of} this embodiment is also provided.
In medium temperature concentrated solution L ₂ from the intermediate temperature regenerator G ₂ is branched after passing through the heating side of the medium-temperature solution heat exchanger H _2, the high-temperature part thereof flows out from the high temperature generator G ₃ Since it is configured so as to join with the high temperature concentrated solution L ₃ that has passed through the heating side of the solution heat exchanger H _3, the amount of concentrated solution flowing into the low temperature regenerator G ₁ is reduced, and the low temperature regenerator G ₁ The amount of heat required for the regeneration (in other words, the evaporation of the refrigerant vapor) is small. Therefore, the thermal efficiency in the low temperature regenerator G ₁ is improved.

Further, the absorption refrigeration system Z _{23 of} this embodiment is also provided.
In this case, since the diluted solution La discharged from the absorber A is branched after passing through the low temperature solution heat exchanger H ₁ , the high temperature regenerator G ₃ is passed through the high temperature solution heat exchanger H ₃ immediately before it. And the dilute solution La flowing into the medium temperature regenerator G ₂ via the medium temperature solution heat exchanger H ₂ immediately before it.
Means that both flow into the low temperature solution heat exchanger H ₁ in a preheated state, and as a result, the required heating heat amount of the absorbing solution in the high temperature regenerator G ₃ and the intermediate temperature regenerator G ₂ decreases. It can be expected that the thermal efficiency of the entire system will be improved.

Further, the absorption refrigeration system Z _{23 of} this embodiment is also provided.
Then, the dilute solution L is generated by the residual heat Q after heating the high temperature regenerator G ₃ of the external heat source J for heating the high temperature regenerator G _3.
Since a is heated, the amount of heat input to the external heat source J can be suppressed by effectively using the residual heat Q, and further COP of the entire system can be expected to be further improved.

Furthermore, the absorption type refrigerating apparatus Z of this embodiment
In _23, since the arrangement to heat the dilute solution La by the low temperature regenerator G ₁ and the intermediate temperature regenerator steam drain Dr ₁ resulted in G _2, Dr _2, the steam drain Dr _1, Dr ₂
The heat retained by the can be effectively used for preheating the diluted solution La, and the thermal efficiency of the entire system can be further promoted.

Further, the absorption type refrigeration system Z of this embodiment_{twenty three}
Then, the diluted solution La is branched from the diluted solution pipe 21.
In the absorbed solution branch pipe 47, the first drain heat exchange is performed.
Exchanger D₁In addition, after branching from the second branch pipe 23
The second drain heat exchange in the absorbing solution branch pipe 48.
Bowl D₂Then, each of the dilute solutions La is replaced with the above-mentioned vapor drain Dr.₁，
Dr₂Since it is configured to heat by
Steam drain Dr₁, Dr ₂Absorption that is heated by the retained heat of
Since the amount of solution is small, the absorption solution can be efficiently preheated.
It

Also, the absorption refrigerating apparatus Z _{23 of} this embodiment
Then, the system is configured by _three regenerators G ₁ , G ₂ , G ₃ and three solution heat exchangers H ₁ , H ₂ , H ₃ , but such a configuration requires a large number of regenerators. To increase the efficiency of the absorption solution by increasing the number of concentration stages of the absorption solution, and to increase the number of solution heat exchangers to increase the heat recovery rate, and the merit of improving the performance of the absorption refrigeration system, and the regenerator and When weighed against the disadvantage of increasing the manufacturing cost by increasing the number of solution heat exchangers, it is considered to be optimal in achieving both the performance and cost aspects of the absorption refrigeration system, and is extremely useful in practice. is there.

As described in the above embodiments, the numbers of drain heat exchangers and exhaust heat exchangers do not necessarily have to be the same as those in each embodiment, and may be different. Moreover, you may combine each embodiment.

[Brief description of drawings]

FIG. 1 is an operation cycle diagram of an absorption refrigerating apparatus according to a first embodiment of the present invention.

FIG. 2 is a Duhring diagram of the absorption refrigerating apparatus shown in FIG.

FIG. 3 is an operation cycle diagram of an absorption refrigeration system according to a second embodiment of the present invention.

FIG. 4 is a Duhring diagram of the absorption refrigerating apparatus shown in FIG.

FIG. 5 is an operation cycle diagram of an absorption refrigeration system according to a third embodiment of the present invention.

FIG. 6 is a Duhring diagram of the absorption refrigerating apparatus shown in FIG.

FIG. 7 is an operation cycle diagram of an absorption refrigeration system according to a fourth embodiment of the present invention.

FIG. 8 is a Duhring diagram of the absorption refrigerating apparatus shown in FIG. 7.

FIG. 9 is an operation cycle diagram of an absorption refrigeration system according to a fifth embodiment of the present invention.

FIG. 10 is an operation cycle diagram of an absorption refrigeration system according to a sixth embodiment of the present invention.

FIG. 11 is an operation cycle diagram of an absorption refrigeration system according to a seventh embodiment of the present invention.

FIG. 12 is an operation cycle diagram of an absorption refrigeration system according to an eighth embodiment of the present invention.

FIG. 13 is an operation cycle diagram of an absorption refrigeration system according to a ninth embodiment of the present invention.

FIG. 14 is an operation cycle diagram of an absorption refrigeration system according to a tenth embodiment of the present invention.

FIG. 15 is an operation cycle diagram of an absorption refrigeration system according to an eleventh embodiment of the present invention.

FIG. 16 is an operation cycle diagram of an absorption refrigerating apparatus according to a twelfth embodiment of the present invention.

FIG. 17 is an operation cycle diagram of an absorption refrigeration system according to a thirteenth embodiment of the present invention.

FIG. 18 is an operation cycle diagram of an absorption refrigeration system according to a fourteenth embodiment of the present invention.

FIG. 19 is an operation cycle diagram of an absorption type refrigeration system according to a fifteenth embodiment of the present invention.

FIG. 20 is an operation cycle diagram of an absorption refrigeration system according to a sixteenth embodiment of the present invention.

FIG. 21 is an operation cycle diagram of an absorption refrigeration system according to a seventeenth embodiment of the present invention.

FIG. 22 is an operation cycle diagram of an absorption refrigeration system according to an eighteenth embodiment of the present invention.

FIG. 23 is an operation cycle diagram of an absorption type refrigeration system according to a nineteenth embodiment of the present invention.

FIG. 24 is an operation cycle diagram of an absorption refrigerating apparatus according to a twentieth embodiment of the present invention.

FIG. 25 is an operation cycle diagram of an absorption refrigeration system according to a twenty-first embodiment of the present invention.

FIG. 26 is an operation cycle diagram of an absorption type refrigeration system according to a twenty-second embodiment of the present invention.

FIG. 27 is an operation cycle diagram of an absorption type refrigeration system according to a twenty-third embodiment of the present invention.

[Explanation of symbols]

1 to 6 are containers, 7 and 8 are heat exchange parts, 9 and 10 are solution heating parts, 11 is a heat exchange part, 12 is a solution sprayer, 13 is a refrigerant sprayer, 14 is a solution heating part, and 21 is a dilute solution. Plumbing, 21
A is a first branch pipe, 21B is a second branch pipe, 21C is a third branch pipe, 22 is a first branch pipe, 23 is a second branch pipe, 24 is a concentrated solution pipe, 25 is a low temperature solution pipe, and 26 is a medium temperature. Solution piping, 26A and 26B branch piping, 27 high temperature solution piping, 27A and 27B branch piping, 29 liquid refrigerant piping, 30 liquid refrigerant piping, 31 high temperature steam piping, 32 medium temperature steam piping, 33 refrigerant Piping, 34 is a refrigerant drain piping,
35 is a refrigerant drain pipe, 36 is a refrigerant drain pipe, 41 is a cooling water inlet pipe, 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, and 50 is Residual heat pipe, 51 is the first residual heat branch pipe, 5
2 is the second residual heat branch pipe, A is an absorber, C is a condenser, D
_{1 to} D ₃ are drain heat exchangers, Dr ₁ and Dr ₂ are steam drains, E is an evaporator, G _{1 to} G ₃ are regenerators, H _{1 to} H ₃ are solution heat exchangers, J is an external heat source, K And K _{1 to} K ₃ are exhaust heat exchangers, L _{1 to} L ₃ are solutions, La is a dilute solution, Lg is a concentrated solution, and L is a concentrated solution.
P is a solution pump, R _{1 to} R ₃ are refrigerant vapors, Ra is a vaporized refrigerant, Rc is a liquid refrigerant, Re is a refrigerant, RP is a refrigerant pump, and Q.
The residual heat, Z ₁ to Z ₂₃ is an absorption-type cooling unit.

   ─────────────────────────────────────────────────── ─── Continued front page    F term (reference) 3L093 AA01 BB16 BB22 BB23 BB29                       BB37

Claims (21)

[Claims] 1. At least one condenser (C), evaporator (E), absorber (A) and n (n ≧ 3) solution heat exchangers (H _{n to} H ₁ ) and a regenerator. (G _n ~G ₁₎ to be operatively connected with the solution piping system and the refrigerant piping system constitute a circulation cycle, the high-temperature side of the regenerator (G _n) low-temperature side of the regenerator and the refrigerant vapor generated in ( G _n-1 ), which is then sequentially introduced into the low temperature side regenerator (G _n-1 ) to be used as a heating source to heat and concentrate the absorption solution of the low temperature side regenerator (G _{n -1} ). It is an absorption type refrigerating apparatus in which this is repeated up to the regenerator (G ₁ ) having the lowest operating temperature, and the dilute solution (La) discharged from the absorber (A) is branched,
One of them, after all or part of the branch amount flows into the regenerator (G _n ) on the highest temperature side, and the other after all or part of the branch amount flows into the regenerator (G _n-1 ) on the low temperature side. And an absorption type refrigerating apparatus, which is configured to flow into a regenerator (G _n-2 ) on the lower temperature side. 2. The method according to claim 1, The dilute solution (La) from the absorber (A) is the lowest temperature side.
Solution heat exchanger (H₁) Branch after passing the heated side
One of them is the regenerator (G _n)Niso
Solution heat exchanger (H_n) Through, the other
Regenerator on the low temperature side (G_n-1) Solution heat exchange immediately before
Bowl (H_n-1) Is configured to flow in through
And an absorption type refrigeration system. 3. The dilute solution (La) discharged from the absorber (A) according to claim 1, is the solution heat exchanger (H) at the lowest temperature side.
₁ ) branched just before ₁ ), one of which flows into the regenerator (G _n ) on the highest temperature side via the solution heat exchanger (H _n ) immediately before it, and the other one of which is the solution heat exchange on the lowest temperature side After passing through the heated side of the vessel (H ₁ ), it is configured to flow into the low temperature side regenerator (G _n-1 ) via the solution heat exchanger (H _n-1 ) immediately before it. An absorption type refrigerating device. 4. The dilute solution (La) on the other side according to claim 2 or 3, wherein the dilute solution (La) on the other side is the solution heat exchanger (H).
_n-1 ) is further branched, and one of the re-branching solutions (La ₁ ) flows into the low temperature side regenerator (G _n-1 ) via the solution heat exchanger (H _n-1 ). After that, the absorption refrigerating device is configured so as to merge with the other re-branching solution (La ₂ ) and further flow into the regenerator (G _n-2 ) on the low temperature side. 5. At least one condenser (C), steam
Generator (E), absorber (A) and n (n ≧ 3) solution heat
Exchanger (H_n~ H₁) And regenerator (G_n~ G₁) Solution piping system
And the refrigerant piping system are operatively connected to form a circulation cycle.
The high temperature side regenerator (G_n) The refrigerant vapor generated in
Side regenerator (G_n-1) To the low temperature side
Regenerator (G_n-1) Is used as a heating source for
Organ (G_{n -1}The best way is to concentrate the absorption solution of
Regenerator with low dynamic temperature (G₁)
Which is an absorption refrigerating device,
The dilute solution (La) is the solution heat exchanger (H₁)
After passing, it branches into n pieces, and the total amount of each branch is
Organ (G_n) ~ (G₁) Into the low temperature side regenerator (G
_n-1) Concentrated solution (L_n-1) Is a regenerator on the lower temperature side
(G_n-2) Is configured to flow into
Absorption type refrigeration equipment. 6. The method according to claim 1, 2, 3, 4, or 5, Concentrated solution (L) from the regenerator (Gn) on the highest temperature side_n) Is
Solution heat exchanger (H _n) Branch after passing the heating side
However, a part of the regenerator (G_n-1) From concentrated solution
(L_n-1) Together with the regenerator (G_n-2) Flow
Absorption cold, characterized by being configured to enter
Freezing device. 7. The method according to claim 1, 2, 3, 4, or 5,
Concentrated solution from the low temperature side of the regenerator _{(G n-1) (L} n-1) is branched after passing through the heating side of the solution heat exchanger (H _{n- 1),} a part of the most An absorption characterized in that it is constructed so as to merge with the concentrated solution (L _n ) after flowing out from the regenerator (G _n ) on the high temperature side and passing through the heating side of the solution heat exchanger (H _n ). Freezer. 8. The system of claim 1, 2, 3, 5 or 7, after heat regenerator of the external heat source (J) to heat the highest temperature side of the regenerator (G _n) to (G _n) The absorption type refrigerating apparatus is configured to heat the circulation path of the absorbing solution with the residual heat (Q). 9. The absorption solution according to claim 8, wherein the residual heat (Q) causes an absorption solution in a path from an outlet of the absorber (A) to an absorption solution inlet of each of the regenerators (G _{n to} G ₁ ). or configurations each regenerator absorption solution immediately before the absorption solution inlet of the (G _n ~G _1), or highest temperature side of the regenerator absorption solution immediately before the absorption solution inlet of the (G _n), to heat The absorption type refrigerating device, which is characterized in that 10. The residual heat pipe (50) for the residual heat (Q) according to claim 8 or 9, is branched into two or more residual heat branch pipes (51, 52), and each residual heat branch pipe (51). , 52), each of which is configured to heat the absorbing solution. 11. The absorption type refrigerating device according to claim 8, 9 or 10, wherein the absorption solution is heated in multiple stages by the residual heat (Q). 12. The diluted solution pipe (23) or (21B) according to claim 8, 9, 10 or 11, wherein the diluted solution pipe (23) or (21B) from the absorber (A).
A branch pipe (48) that bypasses the solution heat exchanger H _N (N = 1 to n) provided in the branch pipe (48) is provided, and the absorption solution is heated in the branch pipe (48) by the residual heat (Q). The absorption type refrigerating device, which is characterized in that 13. The method according to claim 1, 2, 3, 4, 5, 6, 7,
In 8, 9, 10, 11 or 12, each regenerator (G _n ~G ₁₎ with the resulting steam drain (Dr
_{n-1 ~Dr 1)} absorption type refrigerating apparatus characterized by being configured to heat the absorption solution by. 14. The steam drain (D) produced in each of the regenerators (G _{n-1 to} G ₁ ) according to claim 13.
An absorption type refrigerating apparatus, characterized in that two or more of r _{n-1 to} Dr ₁ ) are combined to heat the absorption solution. 15. The absorption of each regenerator (G _{n-1 to} G ₁ ) from the outlet of the absorber (A) by the vapor drain (Dr _{n-1 to} Dr ₁ ) according to claim 13 or 14. An absorption formula characterized in that it is configured to heat the absorption solution in the path leading to the solution inlet or the absorption solution immediately before the absorption solution inlet of each of the regenerators (G _{n-1 to} G ₁ ). Refrigeration equipment. 16. The absorption solution according to claim 13, 14 or 15, wherein said vapor drain (Dr _{n-1 to} Dr ₁ ) is branched into two or more, and said branch paths (34) and (36) are respectively branched. An absorption type refrigerating apparatus, which is configured to perform heating of. 17. The absorption according to claim 13, 14, 15 or 16, wherein the heating of the absorbing solution by the vapor drain (Dr _{n-1 to} Dr ₁ ) is performed in multiple stages. Freezer. 18. The method according to claim 13, 14, 15, 16 or 1.
7, the diluted solution pipe (23) or (21B) from the absorber (A) is connected to the diluted solution pipe (23) or (21B).
Is provided with a branch pipe (48) that bypasses the solution heat exchanger (H _N (N = 1 to n)) provided in the steam drain (Dr _n-1 ~). D
An absorption refrigeration system, characterized in that it is configured to be heated by r ₁ ). 19. The method according to claim 1, 2, 3, 4, 5, 6, 7,
8, 9, 10, 11, 12, 13, 14, 15, 16,
In 17 or 18, the absorber (A) and the evaporator (E) are divided into a plurality of stages having different refrigerant evaporation temperatures, or the lowest temperature regenerator (G ₁ ) and the condenser (C) are refrigerants. It is divided into a plurality of stages having different condensing temperatures, or the absorber (A) and the evaporator (E) are divided into a plurality of stages having different refrigerant evaporation temperatures, and the regenerator (G ₁ ) on the lowest temperature side and the condensing An absorption refrigerating apparatus, wherein the vessel (C) is divided into a plurality of stages having different refrigerant condensing temperatures. 20. Claims 1, 2, 3, 4, 5, 6, 7,
8, 9, 10, 11, 12, 13, 14, 15, 16,
In 17, 18, or 19, cooling water (Wa) that circulates through the absorber (A) and the condenser (C) and cools them together is supplied from the condenser (C) side to the absorber (A). An absorption type refrigerating apparatus, which is configured to flow toward the side. 21. Claims 1, 2, 3, 4, 5, 6, 7,
8, 9, 10, 11, 12, 13, 14, 15, 16,
17, 18, 19 or 20, the absorption refrigerating apparatus, wherein the number n of installed regenerators and solution heat exchangers is n = 3.