JP2003106702A - Absorption refrigerating machine - Google Patents

Abstract

PROBLEM TO BE SOLVED: To upgrade performance by improving a cooling water supply system in an absorption refrigerating machine. SOLUTION: An absorption refrigerating machine includes a circulation cycle provided by operatively connecting a condenser C, an evaporator E, an absorber A, and regenerators Gn to G1 each of which has a different operating temperature by means of a solution piping system and a refrigerant piping system. The absorption refrigerating machine concentrates absorption solution sequentially from the regenerator Gn on the highest temperature side to the regenerator G1 on the lowest temperature side, and uses the refrigerant steam that is generated in the regenerator Gn on the highest temperature side as a heat source of the regenerator Gn-1 on the lower temperature side. In this absorption refrigerating machine, cooling water Wa is made to flow into the absorber A and the condenser C in parallel and the cooling water that cooled the absorber A is combined with the cooling water that is supplied to the condenser C. With this configuration, in the condenser C, the high condensation performance is achieved by assuring the flow rate and the low temperature of the cooling water, and accordingly the working pressure of the regenerators is reduced. By the reduction of the working pressure, the inner pressure of the absorption refrigerating machine is reduced and the reliability on the operation is improved.

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 refrigeration system has a condenser, an evaporator, an absorber and a regenerator as basic constituent elements, and these constituent elements are sequentially and operatively connected by a solution piping system and a refrigerant piping system. Configured.

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 a 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. The heat of vaporization of the refrigerant in the evaporator is usually used as the cold heat source of the refrigeration system.

[0004]

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, there is a problem that the internal pressure (operating pressure) is increased due to the plurality of regenerators.

That is, when the absorption refrigerating apparatus is provided with a plurality of regenerators having different operating temperatures as described above, the operating temperature of each of these regenerators is governed by the operating temperature of the regenerator located at the lowest stage. The lower the operating temperature of the lowermost regenerator is, the more the operating temperature of the uppermost regenerator, that is, the operating pressure can be kept low, which is defined by the operating pressure of the uppermost regenerator. The internal pressure of the absorption refrigeration system as a whole can be kept low.

On the other hand, in the absorption refrigerating apparatus, the lowermost regenerator having the lowest operating temperature is communicated with the condenser, and the refrigerant vapor generated in the lowermost regenerator is directly fed to the condenser. The liquid refrigerant is condensed here and is fed to the evaporator side.

Therefore, it can be said that it is necessary to lower the operating temperature of the lowermost regenerator, in other words, to lower the refrigerant condensing temperature in the condenser, in order to reduce the internal pressure. Then, as a means for lowering the refrigerant condensing temperature of the condenser, it is effective to lower the temperature of the cooling water supplied to the condenser or increase the flow rate thereof to improve the cooling efficiency. Can be said.

However, in the conventional absorption refrigeration system, when cooling the condenser with cooling water, the absorber and the condenser are connected in series by a cooling water pipe, and cooling is supplied to the cooling water pipe. In general, a cooling water circulation structure is adopted in which water is first introduced into an absorber to cool it and then introduced into the condenser to cool it. For this reason, the cooling water introduced into the absorber is one after being heated by the heat exchange in the condenser of the preceding stage, so that the temperature is relatively high,
Therefore, the cooling efficiency in the condenser is low and inferior, and as a result, a sufficient effect cannot be obtained in terms of lowering the internal pressure.

Therefore, the present invention has been made for the purpose of improving the performance of an absorption refrigeration system by improving the cooling water supply system.

[0011]

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 condensers C, evaporators E and absorbers A, and n (n ≧ 2) n (n ≧ 2) different operating temperatures are supplied with the absorption solution containing the refrigerant. The regenerators Gn to G ₁ are operatively connected by the solution piping system and the refrigerant piping system to form a circulation cycle, and the refrigerant vapor generated in the high temperature side regenerator Gn is sequentially transferred to the low temperature side regenerator Gn ₋₁ . This is repeated by introducing to the lower regenerator G ₁ most operating temperatures to absorb the solution heated and concentrated in the low temperature side of the regenerator Gn _-1 heating regenerator low temperature side by using as a source Gn _-1 In the absorption refrigerating apparatus thus configured, the cooling water Wa supplied from the same cooling water supply system is supplied to the absorber A and the condenser C.
And the cooling water after cooling the absorber A is combined with the cooling water supplied to the condenser C.

According to a second invention of the present application, in the absorption refrigerating apparatus according to the first invention, the absorber A and the evaporator E are both low pressure stages Aa and E having different refrigerant evaporation temperatures.
a and the high pressure stages Ab and Eb, or the condenser C
And a regenerator G ₁ having the lowest operating temperature are divided into high pressure stages Ca and G ₁ a and low pressure stages Cb and G ₁ b having different refrigerant condensation temperatures, or the absorber A and the evaporator E. Are both low-pressure stages Aa, Ea and high-pressure stages Ab, which have different refrigerant evaporation temperatures.
While divided into Eb, the condenser C and the regenerator G ₁ having the lowest operating temperature are divided into high pressure Ca and G ₁ a having different refrigerant condensation temperatures and low pressure stages Cb and G ₁ b, respectively. The absorber A and the condenser C are characterized in that the cooling water Wa is made to flow from the high pressure stage Ab, the low pressure stage Cb side toward the low pressure stage Aa, the high pressure stage Ca side. .

In the third invention of the present application, the above-mentioned first or second
In the absorption refrigerating apparatus according to the invention of claim 1,
And the cooling water Wa that is supplied separately to the condenser C
The diversion rate to the absorber A side above 100% greater than 50%.
It is characterized by setting to a value less than%.

In the fourth invention of the present application, at least one condenser C, evaporator E, absorber A, and n (n ≧ 2) n (n ≧ 2) different operating temperatures are supplied with the absorption solution containing the refrigerant. The regenerators Gn to G ₁ are operatively connected by the solution piping system and the refrigerant piping system to form a circulation cycle, and the refrigerant vapor generated in the high temperature side regenerator Gn is sequentially transferred to the low temperature side regenerator Gn ₋₁ . This is repeated by introducing to the lower regenerator G ₁ most operating temperatures to absorb the solution heated and concentrated in the low temperature side of the regenerator Gn _-1 heating regenerator low temperature side by using as a source Gn _-1 In the absorption refrigerating apparatus thus configured, the cooling water Wa supplied from the same cooling water supply system is caused to flow in parallel to the absorber A and the condenser C, and the cooling water after cooling the condenser C is obtained. Is configured to join with the cooling water supplied to the absorber A. Is characterized by.

According to a fifth aspect of the present invention, in the absorption refrigerating apparatus according to the fourth aspect of the invention, the absorber A and the evaporator E are both low pressure stages Aa and E having different refrigerant evaporation temperatures.
a and the high pressure stages Ab and Eb, or the condenser C
And a regenerator G ₁ having the lowest operating temperature are divided into high pressure stages Ca and G ₁ a and low pressure stages Cb and G ₁ b having different refrigerant condensation temperatures, or the absorber A and the evaporator E. Are both low-pressure stages Aa, Ea and high-pressure stages Ab, which have different refrigerant evaporation temperatures.
In addition to dividing into Eb, the condenser C and the regenerator G ₁ having the lowest operating temperature are divided into high pressure stages Ca and G ₁ a and low pressure stages Cb and G ₁ b having different refrigerant condensation temperatures. In the absorber A and the condenser C, the cooling water Wa is configured to flow from the high pressure stage Ab, the low pressure stage Cb side toward the low pressure stage Aa, the high pressure stage Ca side. There is.

In the sixth invention of the present application, the above-mentioned fourth or fifth invention is provided.
In the absorption refrigerating apparatus according to the invention of claim 1,
And the cooling water Wa that is supplied separately to the condenser C
Of the flow rate to the condenser C side of 100
It is characterized by setting to a value less than%.

In the seventh invention of the present application, the above-mentioned first, second, and
The absorption refrigerating apparatus according to the third, fourth, fifth or sixth invention is characterized in that the number n of the regenerators is 2 or 3.

[0019]

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

According to the absorption type refrigeration system of the first invention of the present application, the cooling water Wa supplied from the same cooling water supply system is caused to flow in parallel to the absorber A and the condenser C, and Since the cooling water after cooling the absorber A is combined with the cooling water supplied to the condenser C, the cooling water Wa is directly supplied to the absorber A and the condenser C, respectively. Is supplied to each of the condensers C, and cooling water after cooling the absorber A is also supplied to the condenser C.

Therefore, looking at the condenser C side,
The total amount of cooling water Wa supplied from the cooling water supply system is
Moreover, since about half of the amount is supplied without passing through the absorber A (that is, while keeping the low water temperature at the time of introduction into the cooling water supply system), for example, as in the conventional case, a condenser is used. Although the entire amount of the cooling water is supplied to the condenser C, the cooling water supplied to the condenser C is higher than the case where the temperature of the water is relatively high due to the heat exchange in the preceding absorber. The amount of cold heat of water is large, the condensing efficiency in the condenser C is improved accordingly, and the operating pressure of the regenerator having the lowest operating temperature communicating with the condenser C is correspondingly reduced.
As a result, the internal pressure of the absorption refrigeration system as a whole is lowered, and the operational reliability of the absorption refrigeration system is improved.

On the other hand, by flowing the cooling water Wa in parallel to the absorber A and the condenser C, the flow rate of the cooling water in the absorber A is smaller than that in the conventional structure, for example. However, in terms of the total performance of the absorption type refrigerating apparatus, the absorption performance of the absorber A is rather lower than the disadvantage of the condenser C. The merit due to the decrease of the internal pressure due to the improvement of the condensing performance is much larger, and as a result, the high performance of the entire absorption refrigeration system is secured regardless of the demerits of the absorber A side. .

In the absorption refrigeration system according to the second aspect of the present invention, in the absorption refrigeration system according to the first aspect of the invention, the absorber A and the evaporator E are both low-pressure stages Aa having different refrigerant evaporation temperatures. , Ea and high pressure stages Ab and Eb, or the condenser C and the regenerator G ₁ having the lowest operating temperature are both high pressure stages Ca and G ₁ having different refrigerant condensation temperatures.
a and the low-pressure stage Cb, divided constructed G ₁ b, or the absorber A and the evaporator E and the both refrigerant evaporation temperature is different pressure stage Aa, the Ea of the high pressure stage Ab, with split configuration Eb, Both the condenser C and the regenerator G ₁ having the lowest operating temperature are divided into high pressure Ca and G ₁ a having different refrigerant condensation temperatures and low pressure stages Cb and G ₁ b, while the absorber A and the condensation are used. In the vessel C, the cooling water Wa is supplied to the high pressure stage Ab,
From the low pressure stage Cb side to the low pressure stage Aa, the high pressure stage Ca
It is configured to flow to the side.

Therefore, in the absorption refrigeration system of the present invention, the high and low two-stage divided structure of each of the above-mentioned devices does not affect the supply system of the cooling water Wa to the absorber A and the condenser C at all. Therefore, the same effects as those described above can be reliably obtained even though each of the above devices has a structure in which the device is divided into high and low stages.

Further, in the absorption refrigerating apparatus of the present invention, in the absorber A and the condenser C having the structure of being divided into high and low stages, the high pressure stage Ab and the low pressure stage Cb thereof are respectively.
By flowing the cooling water Wa from the low pressure stage Aa to the high pressure stage Ca, the absorption capacity or the condensation capacity on the high pressure stage Ab side and the low pressure stage Cb side is higher than those on the low pressure stage Aa side and the high pressure stage Ca side. Get higher Therefore, in the absorber A, the temperature gradient between the low-pressure stage Ea and the high-pressure stage Eb of the vaporized refrigerant produced in the low-pressure stage Ea and the high-pressure stage Eb of the evaporator E arranged in parallel with the absorber A, respectively, This corresponds to the heat dissipation capacity gradient of the absorption heat accompanying the absorption action of the vaporized refrigerant on the absorption liquid in the absorber A, and a higher absorption efficiency can be obtained for the absorber A as a whole. Further, the condenser also in C, which in juxtaposed the regenerator the high-pressure stage G ₁ a and the low-pressure stage of the refrigerant vapor produced respectively in the high-pressure stage G ₁ a in G ₁ and the low-pressure stage G ₁ b The temperature gradient between G ₁ b and the temperature gradient of the heat of condensation of the refrigerant vapor in the condenser C correspond to each other, and higher condensation efficiency can be obtained for the entire condenser C. As a synergistic effect of these, in this absorption refrigeration system, both the absorption capacity of the absorber A and the condensation capacity of the condenser C can be maintained at a high level, and as a result, high performance as a whole is secured. It is what is done.

According to the third invention of the present application, the following unique effect is obtained in addition to the effect described above or. That is, in the present invention, in the absorption refrigerating apparatus according to the first or second invention, the cooling water Wa that is divided and supplied to the absorber A and the condenser C is supplied to the absorber A side. Is set to a value greater than 50% and less than 100%.

Since the cooling water supply system between the absorber A and the condenser C is configured so that the entire amount of the cooling water Wa is always supplied to the condenser C, the present invention is used. As described above, even if the diversion rate to the absorber A side is set to a value greater than 50% and less than 100% (in other words,
Even when the cooling water Wa flows in parallel to the absorber A and the condenser C in excess of the diversion rate of 50% that is usually set), the flow rate of the cooling water Wa to the absorber A side may be larger or smaller. Regardless, the supply amount of the cooling water on the condenser C side is secured.

Therefore, according to the absorption refrigeration system of the present invention, the absorption capacity of the absorber A and the condenser C are
It is possible to obtain a high performance as the entire device by making both the condensing capacity and the condensing capacity compatible with each other. The absorption refrigerating device can be selected according to need, and the versatility of the absorption refrigerating device is promoted accordingly.

According to the absorption type refrigeration system of the fourth aspect of the present application, the cooling water Wa supplied from the same cooling water supply system is caused to flow in parallel to the absorber A and the condenser C, and the condensation is performed. Since the cooling water after cooling the vessel C is combined with the cooling water supplied to the absorber A, the cooling water Wa is directly supplied to the absorber A and the condenser C, respectively. In addition to being supplied in approximately half amounts, the absorber A is also supplied with cooling water after cooling the condenser C.

Therefore, looking at the condenser C side,
Although only approximately half of the cooling water Wa supplied from the cooling water supply system is supplied, since it is directly supplied without passing through the absorber A as in the conventional case, the water temperature is kept low. As a result, in the condenser C, even if the supply amount of the cooling water is small, the temperature of the cooling water is low, so that the cooling water has a large amount of cold heat, and therefore the condensation efficiency in the condenser C is improved. Correspondingly, the operating pressure of the regenerator having the lowest operating temperature, which communicates with the condenser C, decreases, and the internal pressure of the absorption refrigeration system as a whole decreases, which improves the operational reliability. To do.

On the other hand, when viewed from the side of the absorber A, approximately half of the cooling water Wa is directly supplied to the absorber A while maintaining a low water temperature, and the cooling water after passing through the condenser C is also supplied. Therefore, for example, the cooling water Wa as in the related art is used.
Although the cooling efficiency will be somewhat lower and the absorption capacity will be lower than in the case where the entire amount is directly supplied, the high absorption capacity will still be maintained. From this, it can be said that the absorption refrigerating apparatus of the present invention makes it possible to improve the operational reliability due to the decrease in the internal pressure and to maintain the absorption performance of the absorber A at the same time.

In the absorption refrigeration system according to the fifth aspect of the present application, in the absorption refrigeration system according to the fourth aspect of the invention, the absorber A and the evaporator E are both low-pressure stages Aa having different refrigerant evaporation temperatures. , Ea and high pressure stages Ab and Eb, or the condenser C and the regenerator G ₁ having the lowest operating temperature are both high pressure stages Ca and G ₁ having different refrigerant condensation temperatures.
a and the low-pressure stage Cb, divided constructed G ₁ b, or the absorber A and the evaporator E and the both refrigerant evaporation temperature is different pressure stage Aa, the Ea of the high pressure stage Ab, with split configuration Eb, Both the condenser C and the regenerator G ₁ having the lowest operating temperature are divided into high pressure stages Ca and G ₁ a and low pressure stages Cb and G ₁ b having different refrigerant condensation temperatures, while the absorber A and the above are used. In the condenser C, the cooling water Wa is supplied to the high pressure stage A.
b, from the low pressure stage Cb side toward the low pressure stage Aa and the high pressure stage Ca side.

Therefore, in the absorption refrigerating apparatus of the present invention, the high-low two-stage divided structure of each of the above-mentioned devices does not affect the supply system of the cooling water Wa to the absorber A and the condenser C at all. Therefore, the same effects as those described above can be reliably obtained even though each of the above devices has a structure in which the device is divided into high and low stages.

Further, in the absorption refrigerating apparatus of the present invention, in the absorber A and the condenser C having the structure of being divided into high and low stages, the high pressure stage Ab and the low pressure stage Cb thereof, respectively.
By flowing the cooling water Wa from the low pressure stage Aa to the high pressure stage Ca, the absorption capacity or the condensation capacity on the high pressure stage Ab side and the low pressure stage Cb side is higher than those on the low pressure stage Aa side and the high pressure stage Ca side. Get higher Therefore, in the absorber A, the temperature gradient between the low-pressure stage Ea and the high-pressure stage Eb of the vaporized refrigerant produced in the low-pressure stage Ea and the high-pressure stage Eb of the evaporator E arranged in parallel with the absorber A, respectively, This corresponds to the heat dissipation capacity gradient of the absorption heat accompanying the absorption action of the vaporized refrigerant on the absorption liquid in the absorber A, and a higher absorption efficiency can be obtained for the absorber A as a whole. Further, the condenser also in C, which in juxtaposed the regenerator the high-pressure stage G ₁ a and the low-pressure stage of the refrigerant vapor produced respectively in the high-pressure stage G ₁ a in G ₁ and the low-pressure stage G ₁ b The temperature gradient between G ₁ b and the temperature gradient of the heat of condensation of the refrigerant vapor in the condenser C correspond to each other, and higher condensation efficiency can be obtained for the entire condenser C. As a synergistic effect of these, in this absorption refrigeration system, both the absorption capacity of the absorber A and the condensation capacity of the condenser C can be maintained at a high level, and as a result, high performance as a whole is secured. It is what is done.

According to the absorption type refrigeration system of the sixth aspect of the present application, the following peculiar effect can be obtained in addition to the effects described above or. That is, in the present invention, the diversion rate to the condenser C side of the cooling water Wa which is divided and supplied to the absorber A and the condenser C is set to a value greater than 50% and less than 100%. ing.

Here, because of the structure of the cooling water supply system between the absorber A and the condenser C, the absorber A is always supplied with the entire amount of the cooling water Wa. As described above, even if the diversion rate to the condenser C side is set to a value greater than 50% and less than 100% (in other words,
When the cooling water Wa flows in parallel to the absorber A and the condenser C in excess of the diversion rate of 50% that is usually set), how much the diversion rate to the condenser C is large or small. Regardless, the supply amount of the cooling water on the absorber A side is secured.

Therefore, according to the absorption refrigeration system of the present invention, the absorption capacity of the absorber A and the condenser C are
It is possible to obtain a high performance as the entire device by making both the condensing capacity and the condensing capacity compatible with each other. The absorption refrigerating device can be selected according to need, and the versatility of the absorption refrigerating device is promoted accordingly.

According to a seventh invention of the present application, in the absorption refrigerating apparatus according to the first, second, third, fourth, fifth or sixth invention, the number n of the regenerators is 2 or 3. There is.

Here, the number of regenerators installed, that is, the merit of improving the performance of the absorption refrigerating apparatus by increasing the number of concentration stages of the absorbing solution and increasing the thermal efficiency, and the number of regenerators installed increases. Considering the disadvantages such as the increase of the internal pressure and the increase of the manufacturing cost, the optimum number of the regenerators installed is two or three.

From this point of view, when the number n of the regenerators is set to 2 or 3 as in the present invention, the absorption type refrigerating apparatus which is practically very useful and has both performance and cost. Will be provided.

[0041]

BEST MODE FOR CARRYING OUT THE INVENTION A preferred embodiment of the present invention will be specifically described below by taking a so-called "serial flow" as an example.

I: First Embodiment FIG. 1 shows the system configuration of an absorption refrigerating apparatus Z ₁ according to a _first embodiment of the present invention. The absorption refrigerating apparatus Z ₁ is an absorption refrigerating apparatus that 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 Regenerators G ₃ , G ₂ , G ₁
The solution piping system and the refrigerant piping system are operatively connected to form a circulation cycle of the refrigerant R and the absorbing solution L.

First, the basic function of each of the above-mentioned devices constituting the absorption refrigerating apparatus Z ₁ will be described.

Evaporator E The evaporator E has a heat exchange section Ec for passing the liquid We to be cooled and a refrigerant spreader Es for distributing the refrigerant Re on the heat exchange section Ec in a container Et, The liquid to be cooled (water) We flowing from the liquid to be cooled Ue flowing through the heat exchange section Ec in the evaporator E is cooled. In addition, the refrigerant Re in the evaporator E is
Is pumped up to the refrigerant distributor Es side by the refrigerant pump RP.

Absorber A The absorber A communicates with the evaporator E and serves to absorb low-temperature vaporized refrigerant (water vapor) Ra flowing from the evaporator E into the absorbing liquid. The container At is provided with a solution sprayer As for spraying the concentrated solution Lg and a heat exchange unit Ac for removing the absorption heat generated in the absorber A. And the said heat exchange part Ac is the cooling water piping Ua.
By supplying the cooling water Wa from the absorption water, the absorption heat generated in the absorber A is removed.

The cooling water Wa is further fed to a condenser C which will be described later and is also used as cooling water for the condenser. The supply system of the cooling water Wa is the gist of the present invention. The details will be described later.

Regenerators G ₃ , G ₂ , G ₁ Each of the above-mentioned regenerators G ₃ , G ₂ , G ₁ is for heating and concentrating an absorption solution containing a refrigerant to obtain a concentrated solution of high concentration in sequence. However, their operating temperatures are different from each other, and the high temperature regenerator G ₃ that operates at the highest temperature, the middle temperature regenerator G ₂ that operates at the middle temperature, and the low temperature regenerator G ₁ that operates at the lowest temperature. It is said that. The dilute solution La from the absorber A is first introduced into the high temperature regenerator G ₃ side through the dilute solution pipe 11 by the solution pump LP.

High Temperature Regenerator G ₃ The high temperature regenerator G ₃ is provided with an external heat source J (for example, a gas combustor) in a container G ₃ t, and the diluted solution La produced in the absorber A is stored in the container G 3. _It is introduced into ₃ t and is heated and concentrated to generate a high temperature concentrated solution (high temperature solution L ₃ ) and a refrigerant vapor R ₃ . Then, of the high temperature solution L ₃ and the refrigerant vapor R ₃ generated in the high temperature regenerator G ₃ , the high temperature solution L ₃ is introduced into the intermediate temperature regenerator G _{2 of the} next stage through the high temperature solution pipe 23, Further, the refrigerant vapor R ₃ is introduced into the solution heating section K ₂ (described below) in the medium temperature regenerator G ₂ through the high temperature vapor pipe 33.

The medium temperature regenerator G ₂ the intermediate temperature regenerator G ₂ is provided with a solution heating unit K ₂ into the container G ₂ t, the high temperature through the hot solution pipe 23 into the container G ₂ t High-temperature concentrated solution L ₃ from the vessel G ₃ side
Will be introduced. Further, in the solution heating section K ₂ , the refrigerant vapor R ₃ generated in the high temperature regenerator G ₃ is fed into the high temperature steam pipe 33.
And is used as a heating source for the concentrated solution L ₃ .

[0050] In the intermediate temperature regenerator G _2, the by solution heating unit K _2, hot solution L ₃ to be introduced from the high temperature generator G ₃ is heated and concentrated, further high concentration and medium temperature solution L mesophilic ₂ is generated, and the refrigerant vapor R ₂ is also generated. Then, of the medium temperature solution L ₂ and the refrigerant vapor R ₂ produced in the medium temperature regenerator G ₂ , the medium temperature solution L ₂ is introduced into the low temperature regenerator G ₁ of the next stage through the medium temperature solution pipe 22. The refrigerant vapor R ₂ is introduced into the solution heating unit K ₁ provided in the low temperature regenerator G ₁ through the medium temperature vapor pipe 32. Further, the refrigerant vapor R ₃ introduced from the high temperature regenerator G ₃ into the solution heating section K ₂ of the medium temperature regenerator G _2.
Undergoes a phase change due to a heating action due to a latent heat change in the solution heating section K ₂ to become a refrigerant drain Rd ₂ , and the refrigerant drain pipe 41
Through the low temperature regenerator G ₁ and a condenser C described later, and is returned to the drain pipe 40.
It is returned to the condenser C via 0.

Low Temperature Regenerator G ₁ The low temperature regenerator G ₁ includes a solution heating section K ₁ in a container G ₁ t. In the solution heating section K ₁ , the refrigerant vapor R ₂ generated in the medium temperature regenerator G ₂ is fed with the medium temperature steam pipe 3
Is introduced through 2, the refrigerant vapor R ₂ is utilized as a heat source for medium temperature solution L ₂ which is introduced from the intermediate temperature regenerator G ₂ through the medium-temperature solution pipe 22, heating concentrated middle warm solution L ₂ As a result, a low-temperature solution L ₁ having a higher concentration is generated and a refrigerant vapor R ₁ is generated.

The low temperature solution L ₁ is introduced into the absorber A through the low temperature solution pipe 21 and is sprayed as a concentrated solution Lg from the solution sprayer As. Further, in the absorber A, the low-temperature refrigerant vapor Ra introduced from the evaporator E is absorbed in the concentrated solution Lg sprayed from the solution sprayer As, and the absorbing solution becomes a dilute solution La. The container At
Stored at the bottom of the. Further, in the absorber A, absorption heat is generated when the concentrated solution Lg absorbs the refrigerant vapor Ra, but this absorption heat is generated by heat exchange with the cooling water Wa supplied to the heat exchange section Ac. To be removed. After passing through the absorber A, the cooling water Wa is further fed to the condenser C described below.

Condenser C The condenser C cools and condenses the refrigerant vapor R ₁ introduced from the low temperature regenerator G ₁ through the refrigerant pipe 31 into the container Ct to generate the liquid refrigerant Rc. A heat exchange section Cc for cooling and condensing the refrigerant vapor R ₁ is provided in the container Ct. The cooling water Wa introduced into the cooling water pipe Ua is supplied to the heat exchange section Cc, and the supply system of the cooling water Wa will be described in detail later.

[0054] are introduced into the solution heating unit K ₁ of the low temperature regenerator G _1, and the refrigerant drain Rd ₁ produced condensed by heat exchange in this case, the solution heated portion K of the medium-temperature regenerator G ₂
The refrigerant drain pipe 4 generated by the heating action in ₂
Along with the refrigerant drain Rd ₂ joined to the drain pipe 40 side through 1 is introduced into the condenser C through the drain pipe 40 and joined to the liquid refrigerant Rc. The liquid refrigerant Rc is supplied to the evaporator E via the liquid refrigerant pipe 43.

On the other hand the heat exchanger _{H 1, H 2, H 3} , the absorber in the middle of the dilute solution pipe 11 leading to the high-temperature regenerator G ₃ are the A, 3 pieces of the heat exchangers H _1, H _2, H ₃
Is provided. Each of these heat exchangers H ₁ , H ₂ , H
₃ is for recovering the heat of each of the low temperature solution L ₁ , the intermediate temperature solution L ₂ and the high temperature solution L ₃ generated in each of the regenerators G ₁ , G ₂ and G ₃ to the absorption solution La side. The thing
The low temperature solution heat exchanger H ₁ on the lowest temperature side has a low temperature solution pipe 2
The low temperature solution L ₁ is introduced from the low temperature regenerator G ₁ via 1 and the medium temperature solution pipe 22 is connected to the medium temperature medium temperature solution heat exchanger H _2.
Through the introduction of medium temperature solution L ₂ from the intermediate temperature regenerator G _2, most hot high temperature solution heat exchanger H ₃ hot solution L ₃ through the hot solution pipe 23 is introduced, whereby a dilute The solution La is heated from the temperature in the absorber A,
The heating concentration effect on the low temperature regenerator G ₁ side is promoted.

Cooling Water Supply System Now, the structure of the cooling water supply system for supplying cooling water to the absorber A and the condenser C will be described. The cooling water pipe Ua for introducing the cooling water Wa is first connected to the pipe Ua ₁ connected to the cooling water inlet side of the heat exchange section Ac of the absorber A and the heat exchange section Cc of the condenser C. It is branched to the pipe Ua ₂ . The pipe Ua ₃ branched from the intermediate position of the pipe Ua ₂ is connected to the cooling water outlet side of the heat exchange section Ac of the absorber A. A pipe Ua ₅ for discharging the cooling water to the outside is connected to the cooling water outlet side of the heat exchange section Cc of the condenser C.

Therefore, according to this cooling water supply system, the absorber A and the condenser C are connected in parallel to the cooling water pipe Ua, and the cooling water introduced into the cooling water pipe Ua is connected. Wa after the introduction, is diverted to the pipe Ua ₁ and the pipe Ua _2, through the respective pipe Ua _1, Ua ₂ respectively is supplied separately to the condenser C and the absorber a, the absorber a The cooling water after passing through is also supplied to the condenser C side through the pipe Ua ₂ .

[0058]Operation explanation of absorption refrigeration system Z ₁ Absorption refrigeration system Z configured as described above₁At
Is the three regenerators G having different operating temperatures as described above.₃，
G₂, G₁And each of these regenerators G₃, G₂, G₁smell
The absorption solution is concentrated in multiple stages, and
Organ G₂And low temperature regenerator G₁In each of the above
The regenerator located, that is, the above-mentioned medium temperature regenerator G₂In that case
High temperature regenerator G above₃, The low temperature regenerator G₁In that case
Medium temperature regenerator G ₂And the generated refrigerant vapor R₃, R
₂As a heating source for concentrating the dilute solution La.
By doing so, high thermal efficiency is secured for the entire system,
Higher performance can be obtained.

By the way, the absorption refrigerating apparatus Z ₁ is required to lower the internal pressure as much as possible to ensure its operational reliability and to reduce its cost. An effective means for realizing this is required. As the above-mentioned regenerators G ₃ , G ₂ ,
Of G ₁ , the low temperature regenerator G ₁ having the lowest operating temperature (that is, operating pressure) is attached, and the refrigerant vapor R ₁ introduced from the low temperature regenerator G ₁ side is condensed to generate the liquid refrigerant Rc. As described above, it is effective to lower the refrigerant condensing temperature in the condenser C, in other words, to increase the cooling capacity of the condenser C with the cooling water. However, even in this case, needless to say, it is necessary to sufficiently consider the cooling capacity on the absorber A side.

In the absorption type refrigerating apparatus Z ₁ of this embodiment, such a demand is dealt with by configuring the cooling water supply system as described above.

That is, the absorption refrigerating apparatus Z _{1 of} this embodiment
The cooling water W supplied to the cooling water pipe Ua
a is split into two pipes Ua ₁ and Ua ₂ which are connected in parallel to the absorber A and the condenser C, and the heat exchange section Ac of the absorber A and the heat exchange section Cc of the condenser C are divided. While performing the cooling action on the heat exchange section Ac side of the absorber A, the cooling water discharged from the heat exchange section Ac is introduced to the pipe Ua ₂ side, and the cooling water is introduced to the condenser C. I am trying to supply it to. In the following, the ratio of the amount of cooling water supplied to the absorber A side with respect to the total amount of introduced cooling water, that is,
A case where the flow dividing ratio is set to 50% will be described as an example.

According to this cooling water supply mode, first, the cooling water Wa having a low temperature introduced from the cooling water pipe Ua is passed through the pipe Ua _{1 to} the heat exchange section Ac side of the absorber A. And the heat exchange section Cc side of the condenser C through the pipe Ua ₂ in a substantially equal amount. Therefore, on the absorber A side, the cooling action in the heat exchange section Ac is executed by approximately half the total amount of the low temperature cooling water, and the absorption heat accompanying the absorption of the vaporized refrigerant into the absorption liquid in the absorber A is executed. The heat is dissipated. Therefore, on the absorber A side, for example, as in the conventional case,
Compared to the case where the entire amount of the introduced cooling water is directly supplied to the absorber A, the cooling capacity is reduced by the amount that the supply amount is halved, but the cooling heat amount is sufficient because the supplied cooling water is at a low temperature. However, despite the fact that the amount of cooling water supplied is halved, it still exhibits relatively high absorption performance.

On the other hand, on the side of the condenser C, about half the low-temperature cooling water of the total supply amount and the cooling water of about half the amount and after the cooling operation on the side of the absorber A are joined together. Is supplied as a cooling medium, and the cooling water condenses the refrigerant vapor R ₁ in the heat exchange section Cc. Therefore, on the side of the condenser C, the entire amount of the introduced cooling water is supplied, and about half of the supplied amount is the cooling water that maintains the low water temperature at the time of introduction. However, compared with the case where all of the supplied cooling water is cooling water having a relatively high water temperature that has already been cooled by the absorber A in the preceding stage, the condensed water is The amount of cold heat held by the cooling water supplied to the condenser C is large because the uncooled approximately half amount of the cooling water is present, and the condensing temperature (that is, the condensing pressure) of the refrigerant vapor R _{1 in} the condenser C is correspondingly large. descend. Corresponding to the decrease in the condensation pressure of the condenser C, the operating pressure on the side of the low temperature regenerator G ₁ also decreases, and as a result, the internal pressure of the entire system of the absorption refrigeration apparatus Z ₁ is surely decreased. You will be able to The reduction in the internal pressure improves the operational reliability of the absorption refrigeration system Z ₁ and promotes cost reduction.

In the absorption refrigeration system Z ₁ of this embodiment, as described above, the merit that the internal pressure of the condenser C decreases due to the decrease of the condensation pressure on the side of the condenser C and the absorption capacity of the absorber A. Although having both a disadvantage of decreased, the influence of the disadvantage factors gives in terms of performance of the absorption refrigerating apparatus Z _1, from where the influence of the benefit component gives greater in each stage, a whole the absorption refrigerating apparatus Z ₁ In that case, the existence of the above disadvantages does not cause a problem.

On the other hand, in the above-described embodiment, the case where the flow division ratio of the cooling water Wa to the absorber A side is set to 50% has been described as an example, but in the absorption refrigerating apparatus Z _{1 of} this embodiment, It is possible to easily change the diversion rate by providing a diversion rate changing means such as a variable diversion valve at the branch portion of the pipe Ua ₁ and the pipe Ua ₂ , and particularly, in claim 3 of the present application, The diversion rate is set to "a value greater than 50% and less than 100%".

Here, the case where the diversion rate is set to 50% is the case of the above-mentioned embodiment, and the diversion rate is set to 5 in this way.
Even if it is set to 0%, as described above, since the entire amount of the cooling water Wa to be introduced is supplied to the condenser C side, the condensing pressure of the condenser C is lowered and the in-machine pressure is lowered. That is, the effect peculiar to the present invention can be obtained. In other words, since the entire amount of the introduced cooling water is always supplied to the condenser C, it is assumed that the absorption capacity of the absorber A is appropriately maintained by supplying 50% of the cooling water to the absorber A side. Also, at the same time, the condensing capacity of the condenser C can be increased to obtain the effect of lowering the internal pressure of the machine.

On the other hand, the case where the diversion rate is set to 100% and the entire amount of the cooling water Wa is supplied only to the absorber A side, also in this case, the total cooling is performed after passing through the absorber A. Since water is supplied to the condenser C, the effect of lowering the in-machine pressure by improving the condensing capacity of the condenser C is reduced, but the absorption refrigeration apparatus Z _{1 as a} whole can have high performance. is there.

Therefore, as in the above embodiment, the absorption type refrigerating apparatus Z ₁ in which the cooling water diversion rate to the absorber A side is set to 50% maintains the absorption capacity of the absorber A appropriately. On the other hand, it is possible to effectively reduce the in-machine pressure of the system, in other words, an absorption refrigeration system that places importance on operational reliability and the like.

II: Second Embodiment FIG. 2 shows the system configuration of an absorption refrigeration system Z ₂ according to a _second embodiment of the present invention. Absorption refrigerating apparatus Z ₂ in this embodiment is a one having the same system configuration as the absorption refrigerating apparatus Z ₁ of the first embodiment, the absorption type refrigerating apparatus according to an embodiment of said 1 Z ₁ 2 is the configuration of the cooling water supply system for the absorber A and the condenser C.

That is, in the absorption type refrigerating apparatus Z ₁ of the _first embodiment, the cooling water Wa introduced from the cooling water pipe Ua is split into the absorber A and the condenser C and flows in parallel. The cooling water that has passed through the absorber A is further supplied to the condenser C.

On the other hand, in the absorption refrigerating apparatus Z ₂ of this embodiment, the cooling water Wa introduced from the cooling water pipe Ua is split into the absorber A and the condenser C and flows in parallel. The cooling water after passing through the condenser C is further supplied to the absorber A.

That is, the absorption refrigerating apparatus Z _{2 of} this embodiment
The cooling water W supplied to the cooling water pipe Ua
a is split into two pipes Ua ₁ and Ua ₂ which are connected in parallel to the absorber A and the condenser C, and the heat exchange section Ac of the absorber A and the heat exchange section Cc of the condenser C are divided. And the cooling water after performing the cooling action on the heat exchange section Cc side of the condenser C through the pipe Ua _{3 and the} pipe Ua ₂
Is combined with the cooling water flowing therethrough, and the combined cooling water is supplied to the heat exchange section Ac of the absorber A.
In the following, the ratio of the amount of cooling water supplied to the condenser C side with respect to the total amount of introduced cooling water, that is, the diversion rate is 50.
The case where it is set to% will be described as an example.

According to such a cooling water supply mode, first, the cooling water Wa having a low temperature introduced from the cooling water pipe Ua is passed through the pipe Ua _{1 to} the heat exchange section Ac side of the absorber A. And the heat exchange section Cc side of the condenser C through the pipe Ua ₂ in a substantially equal amount. Therefore, on the side of the condenser C, the cooling action in the heat exchange section Cc is executed by approximately half the total amount of the low-temperature cooling water, and the refrigerant vapor R in the condenser C is executed.
A condensation action of ₁ is performed. Therefore, on the side of the condenser C, as compared with the case where the entire amount of the introduced cooling water is supplied to the side of the condenser C as in the conventional case, for example, the cooling capacity is reduced by half the supply amount. Since the supplied cooling water is at a low temperature as it is introduced from the cooling water pipe Ua side, the amount of cooling heat is sufficiently large. Therefore, even though the amount of cooling water supplied is halved, its condensing capacity is Drop,
Along with this, it is possible to reduce the internal pressure of the system premise, which in turn makes it possible to ensure the operational reliability of the absorption refrigeration system Z ₂ or to promote cost reduction.

On the other hand, on the absorber A side, about half the low-temperature cooling water of the total supply amount and the cooling water of about half the amount and after the cooling action on the condenser C side are joined together. Is supplied as a cooling water, and the cooling water serves to cool the heat exchange section Ac. Therefore, on the side of the absorber A, the entire amount of the introduced cooling water is supplied, and about half of the supplied amount is the cooling water that maintains the low water temperature at the time of introduction. Although the absorption capacity is somewhat lower than that in the case where all the water is directly supplied at a low water temperature, it still retains a high absorption capacity.

In the absorption refrigeration system Z ₂ of this embodiment, as described above, the merit that the internal pressure decreases due to the decrease in the condensation pressure on the condenser C side and the absorption capacity of the absorber A. However, this demerit is smaller than the merit of improving the operational reliability by lowering the condensing pressure of the condenser C to lower the internal pressure. The absorption refrigeration system Z _{2 as a} whole causes almost no problem.

On the other hand, in the above-described embodiment, the case where the splitting ratio of the cooling water Wa to the condenser C side is set to 50% has been described as an example, but in the absorption refrigerating apparatus Z _{2 of} this embodiment. Similarly to the case of the absorption refrigeration system Z ₁ of the _first embodiment, by providing a flow dividing ratio changing means such as a variable flow dividing valve at the branch portion of the pipe Ua ₁ and the pipe Ua ₂ , It is possible to change the rate easily,
In particular, in claim 3 of the present application, the diversion rate is set to "a value greater than 50% and less than 100%".

Here, the case of setting the flow dividing ratio to 50% is the case of the above-mentioned embodiment, but the flow dividing ratio is set to 5 in this way.
Even if it is set to 0%, as described above, since the low-temperature cooling water that maintains the water temperature at the time of introduction is supplied to the condenser C side, the condensation pressure of the condenser C is lowered to reduce the internal pressure of the machine. It is possible to obtain the effect peculiar to the invention of the present application in that

On the other hand, when the diversion rate is set to 100%, that is, the cooling water W introduced from the cooling water pipe Ua.
This is a case where the entire amount of a is directly supplied to the condenser C side. In this case, the cooling water W is provided on the condenser C side.
Since the total amount of a is all low and the water temperature is low,
The cooling capacity by the cooling water is further improved, and correspondingly, the internal pressure of the entire system can be further reduced, and the operational reliability of the absorption refrigeration system Z ₂ is further enhanced. It will be.

In this case, on the side of the absorber A,
The entire amount of cooling water after passing through the condenser C side is supplied as is.
Is supplied, the total cooling water of low water temperature as in the conventional
As compared with the case where the amount is directly supplied to the absorber A, the cooling water is
Although the absorption capacity is reduced due to the higher temperature,
Absorption-type refrigeration system Z that does not cause any problems ₂
There is no problem in terms of performance.

Therefore, the absorption refrigerating apparatus Z of this embodiment is
₂ can be said to be an absorption type refrigeration system that places more importance on operational reliability and the like than the absorption type refrigeration system Z ₁ of the first embodiment.

The constituent elements other than the above and the effects thereof are the same as those of the absorption refrigerating apparatus Z _{1 of the first} embodiment.
2 is the same as that of the first embodiment, the same reference numerals are given to the respective constituent members of FIG. 2 corresponding to the respective constituent members of FIG.
The description here is omitted by applying the corresponding description in the embodiment.

III: Third Embodiment FIG. 3 shows the system configuration of an absorption refrigerating apparatus Z ₃ according to a _third embodiment of the present invention. Absorption refrigerating apparatus Z ₃ of this embodiment, the first be those having the same system configuration as the absorption refrigerating apparatus Z ₁ embodiment, this absorption refrigerating apparatus Z of the first embodiment _The difference from ₁ is that the absorber A and the evaporator E, and the condenser C and the low temperature regenerator G ₁ have a high-low two-stage split structure, respectively.

That is, as shown in FIG. 3, in the absorber A, the absorber A is divided into a low pressure stage Aa and a high pressure stage Ab, and the absorber A is arranged so as to straddle the low pressure stage Aa and the high pressure stage Ab. The cooling water is configured to flow from the high pressure stage Ab side to the low pressure stage Aa side with respect to the heat exchange section Ac. Further, in the evaporator E, it is connected to the low pressure stage Ea and the high pressure stage Eb.
And is configured to allow the liquid We to be cooled to flow from the high pressure stage Eb side to the low pressure stage Ea side with respect to the heat exchange section Ec which is disposed over the low pressure stage Ea and the high pressure stage Eb. ing. Then, from the low pressure stage Ea side of the evaporator E to the low pressure stage Aa of the absorber A, and the high pressure stage E of the evaporator E.
The vaporized refrigerant Ra is moved from the b side to the high pressure stage Ab side of the absorber A, respectively.

On the other hand, in the condenser C, it is divided into a high pressure stage Ca and a low pressure stage Cb, and these high pressure stages Ca are
The cooling water is made to flow from the low pressure stage Cb side to the high pressure stage Ca side with respect to the heat exchange part Cc arranged across the low pressure stage Cb. In the low temperature regenerator G _1, it is divided into a high pressure stage G ₁ a and a low pressure stage G ₁ b,
The refrigerant vapor R ₂ from the medium temperature regenerator G ₂ is supplied to the solution heating unit K ₁ arranged across the high pressure stage G ₁ a and the low pressure stage G ₁ b from the above and low pressure stage G ₁ b side. It is configured to flow to the high pressure stage G ₁ a side. Then, from the high pressure stage G ₁ a side of the low temperature regenerator G _{1 to} the high pressure stage Ca of the condenser C,
From the low pressure stage G ₁ b side of the low temperature regenerator G ₁ to the lower pressure stage G ₁ b side of the condenser C, and configured to move the refrigerant vapor R _1, respectively.

As described above, in the absorption refrigeration system Z ₃ of this embodiment, the absorber A, the evaporator E and the condenser C are used.
And the configuration of the cooling water supply system for the absorber A and the condenser C is different from that of the absorption refrigerating device Z ₁ of the first embodiment only in the configuration of the low temperature regenerator G _1. This is the same as the absorption refrigerating apparatus Z ₁ of the embodiment. Therefore, it goes without saying that the absorption refrigerating apparatus Z ₃ of this embodiment can also obtain the same effects as the absorption refrigerating apparatus Z ₁ of the first embodiment.

By the way, in the absorption refrigerating apparatus Z _{3 of} this embodiment, the cooling water is supplied to the high pressure stage Ab and the low pressure stage C in the absorber A and the condenser C having the high and low two-stage split structure.
Since the flow is made to flow from the b side toward the low pressure stage Aa and the high pressure stage Ca side, the following unique operational effects can be obtained.

That is, in the absorber A and the condenser C having the structure of being divided into high and low stages, the high pressure stage A is respectively formed.
b, by flowing the cooling water Wa from the side of the low pressure stage Cb toward the side of the low pressure stage Aa and the high pressure stage Ca, the high pressure stage Ab and the low pressure stage C
The absorption capacity or the condensation capacity on the b side is higher than those on the low pressure stage Aa side and the high pressure stage Ca side.

Therefore, in the absorber A, between the low pressure stage Ea and the high pressure stage Eb of the vaporized refrigerant produced in the low pressure stage Ea and the high pressure stage Eb of the evaporator E arranged in parallel with each other, respectively. The temperature gradient and the heat dissipation capacity gradient of the absorption heat accompanying the absorption action of the vaporized refrigerant in the absorber A in the absorber A correspond to each other, and the absorber A as a whole can obtain higher absorption efficiency.

[0089] Further, the condenser also in C, which in juxtaposed the regenerator G ₁ of the high-pressure stage G ₁ a and the low-pressure stage G ₁ b the high pressure stage of the refrigerant vapor R ₁ respectively generated in the G ₁
a temperature gradient between the a and the low pressure stage G ₁ b, and the temperature gradient of the heat of condensation of the refrigerant vapor in the condenser C correspond, higher condensation efficiency than the whole the condenser C is obtained.

As a synergistic effect of these, in the absorption type refrigerating apparatus Z ₃ , both the absorption capacity of the absorber A and the condensation capacity of the condenser C can be maintained at a high level,
As a result, it becomes possible to secure high performance as the entire device.

IV: Fourth Embodiment FIG. 4 shows the system configuration of an absorption refrigeration system Z ₄ according to a _fourth embodiment of the present invention. Absorption refrigerating apparatus Z ₄ in this embodiment, the second embodiment absorption refrigerating apparatus comprising a Z ₂ which have the same system configuration and, this absorption refrigerating apparatus Z embodiment the second _The difference from ₂ is that the absorber A and the evaporator E, and the condenser C and the low temperature regenerator G ₁ have a high-low two-stage split structure, respectively.

That is, as shown in FIG. 4, in the absorber A, the absorber A is divided into a low pressure stage Aa and a high pressure stage Ab, and the absorber A is arranged so as to straddle the low pressure stage Aa and the high pressure stage Ab. The cooling water is configured to flow from the high pressure stage Ab side to the low pressure stage Aa side with respect to the heat exchange section Ac. Further, in the evaporator E, it is connected to the low pressure stage Ea and the high pressure stage Eb.
And is configured to allow the liquid We to be cooled to flow from the high pressure stage Eb side to the low pressure stage Ea side with respect to the heat exchange section Ec which is disposed over the low pressure stage Ea and the high pressure stage Eb. ing. Then, from the low pressure stage Ea side of the evaporator E to the low pressure stage Aa of the absorber A, and the high pressure stage E of the evaporator E.
The vaporized refrigerant Ra is moved from the b side to the high pressure stage Ab side of the absorber A, respectively.

On the other hand, in the condenser C, it is divided into a high pressure stage Ca and a low pressure stage Cb, and these high pressure stages Ca are
The cooling water is made to flow from the low pressure stage Cb side to the high pressure stage Ca side with respect to the heat exchange part Cc arranged across the low pressure stage Cb. In the low temperature regenerator G _1, it is divided into a high pressure stage G ₁ a and a low pressure stage G ₁ b,
The refrigerant vapor R ₂ from the medium temperature regenerator G ₂ is supplied to the solution heating unit K ₁ arranged across the high pressure stage G ₁ a and the low pressure stage G ₁ b from the above and low pressure stage G ₁ b side. It is configured to flow to the high pressure stage G ₁ a side. Then, from the high pressure stage G ₁ a side of the low temperature regenerator G _{1 to} the high pressure stage Ca of the condenser C,
From the low pressure stage G ₁ b side of the low temperature regenerator G ₁ to the lower pressure stage G ₁ b side of the condenser C, and configured to move the refrigerant vapor R _1, respectively.

As described above, in the absorption type refrigeration system Z ₄ of this embodiment, the absorber A, the evaporator E and the condenser C are used.
And the configuration of the cooling water supply system for the absorber A and the condenser C is different from that of the absorption refrigerating apparatus Z ₂ of the second embodiment only in the configuration of the low temperature regenerator G _1. This is the same as the case of the absorption refrigeration system Z ₂ of the embodiment. Therefore, it goes without saying that the absorption refrigerating apparatus Z ₄ of this embodiment can also obtain the same operational effects as the absorption refrigerating apparatus Z ₂ of the second embodiment.

By the way, in the absorption refrigerating apparatus Z _{4 of} this embodiment, in the absorber A and the condenser C having the high and low two-stage divided structure, the cooling water is supplied to the high pressure stage Ab and the low pressure stage C.
Since the flow is made to flow from the b side toward the low pressure stage Aa and the high pressure stage Ca side, the following unique operational effects can be obtained.

That is, in the absorber A and the condenser C having the structure of being divided into high and low stages, the high pressure stage A
b, by flowing the cooling water Wa from the side of the low pressure stage Cb toward the side of the low pressure stage Aa and the high pressure stage Ca, the high pressure stage Ab and the low pressure stage C
The absorption capacity or the condensation capacity on the b side is higher than those on the low pressure stage Aa side and the high pressure stage Ca side.

Therefore, in the absorber A, between the low pressure stage Ea and the high pressure stage Eb of the vaporized refrigerant produced in the low pressure stage Ea and the high pressure stage Eb of the evaporator E arranged in parallel, respectively, between the low pressure stage Ea and the high pressure stage Eb. The temperature gradient and the heat dissipation capacity gradient of the absorption heat accompanying the absorption action of the vaporized refrigerant in the absorber A in the absorber A correspond to each other, and the absorber A as a whole can obtain higher absorption efficiency.

[0098] Further, the condenser also in C, which in juxtaposed the regenerator G ₁ of the high-pressure stage G ₁ a and the low-pressure stage G ₁ b the high pressure stage of the refrigerant vapor R ₁ respectively generated in the G ₁
a temperature gradient between the a and the low pressure stage G ₁ b, and the temperature gradient of the heat of condensation of the refrigerant vapor in the condenser C correspond, higher condensation efficiency than the whole the condenser C is obtained.

As a synergistic effect of these, in this absorption refrigerating apparatus Z ₄ , both the absorption capacity of the absorber A and the condensation capacity of the condenser C can be maintained at a high level,
As a result, it becomes possible to secure high performance as the entire device.

Others In each of the above-mentioned embodiments, the description has been made based on the so-called "serial flow". However, the present invention is not limited to this. For example, "parallel flow", "reverse flow", or The same applies to any cycle such as a combination of these two.

[Brief description of drawings]

FIG. 1 is an explanatory diagram of a system configuration and an operation cycle in an absorption type refrigeration system according to a first embodiment of the present invention.

FIG. 2 is an explanatory diagram of a system configuration and an operation cycle in an absorption refrigerating device according to a second embodiment of the present invention.

FIG. 3 is an explanatory diagram of a system configuration and an operation cycle in an absorption refrigerating apparatus according to a third embodiment of the present invention.

FIG. 4 is an explanatory diagram of a system configuration and an operation cycle in an absorption refrigeration system according to a fourth embodiment of the present invention.

[Explanation of symbols]

11 is a dilute solution pipe, 21 is a low temperature solution pipe, 22 is a medium temperature solution pipe, 23 is a high temperature solution pipe, 31 is a refrigerant pipe, 32 is a medium temperature steam pipe, 33 is a high temperature steam pipe, 40 to 42 are refrigerant drain pipes, 43 liquid refrigerant pipe, A is the absorber, C is the condenser, E is the evaporator, G ₁ ~G ₃ is regenerator, H ₁ to H ₃ is solution heat exchanger, J is the heater, K ₁ ~K ₃ Is a solution heating part, La is a dilute solution, Lg is a concentrated solution, LP is a solution pump, L ₁ is a low temperature solution, L ₂ is a medium temperature solution, L ₃ is a high temperature solution, Ra is a vaporized refrigerant,
Rc is a liquid refrigerant, Re is a refrigerant, Rd is a refrigerant drain, RP is a refrigerant pump, R _{1 to} R ₃ are refrigerant vapors, Ua is a cooling water pipe,
Ua _{1 to} Ua ₄ are piping, Wa is cooling water, We is a liquid to be cooled,
Z _{1 to} Z ₄ are absorption type refrigerating apparatuses.

   ─────────────────────────────────────────────────── ─── Continued front page    (72) Inventor Tatsumi Takase             1304 Kanaoka-cho, Sakai City, Osaka Prefecture Daikin Industries             Sakai Plant Kanaoka Factory (72) Inventor Kenji Yasuda             1304 Kanaoka-cho, Sakai City, Osaka Prefecture Daikin Industries             Sakai Plant Kanaoka Factory F term (reference) 3L093 BB11 BB16 BB29 BB37 BB49                       MM07

Claims (7)

[Claims] 1. At least one condenser (C), evaporator (E), absorber (A), and n (n ≧ 2) different operating temperatures to which an absorption solution containing a refrigerant is supplied. Regenerator (G
n to G ₁ ) are operatively connected to the solution piping system and the refrigerant piping system to form a circulation cycle, and the refrigerant vapor generated in the high temperature side regenerator (Gn) is transferred to the low temperature side regenerator (Gn _−1). ) which are sequentially introduced into the low temperature side of the regenerator (Gn _-1 of the low temperature side by using as a heating source) regenerator (Gn _-1) absorbent solution of most operating temperatures the heating concentrated in An absorption type refrigerating apparatus configured to repeat until a low regenerator (G ₁ ), wherein cooling water (Wa) supplied from the same cooling water supply system is
Flowing in parallel to the absorber (A) and the condenser (C), the cooling water after cooling the absorber (A) is merged with the cooling water supplied to the condenser (C). An absorption type refrigerating apparatus having the above-mentioned constitution. 2. The low pressure stage (Aa) according to claim 1, wherein the absorber (A) and the evaporator (E) have different refrigerant evaporation temperatures, and the high pressure stage (Aa) and the evaporator (Ea) have different refrigerant evaporation temperatures.
b), (Eb), or a condenser (C) and a regenerator (G) having the lowest operating temperature.
₁ ) is divided into a high pressure stage (Ca), a high pressure stage (G ₁ a) and a low pressure stage (Cb), (G ₁ b), both of which have different refrigerant condensation temperatures, or the absorber (A) and the evaporator. (E) is divided into a low pressure stage (Aa), a high pressure stage (Aa), and a high pressure stage (Ab) (Eb), both of which have different refrigerant evaporation temperatures, and the operating temperature is the lowest with that of the condenser (C). High-pressure stage (Ca) and refrigerant (G _{1 a} ) with different refrigerant condensing temperatures with the regenerator (G ₁ )
And the low pressure stages (Cb) and (G ₁ b) are divided, while the cooling water (Wa) in the absorber (A) and the condenser (C) is in the high pressure stage (Ab) and the low pressure stage. Step (C
An absorption type refrigerating apparatus, which is configured to flow from the b) side toward the low pressure stage (Aa) and the high pressure stage (Ca) side. 3. The split flow of the cooling water (Wa), which is split and supplied to the absorber (A) and the condenser (C), to the absorber (A) side according to claim 1 or 2. An absorption type refrigerating apparatus, wherein the rate is set to a value greater than 50% and less than 100%. 4. At least one condenser (C), evaporator (E), absorber (A) and n (n ≧ 2) n (n ≧ 2) different operating temperatures to which an absorption solution containing a refrigerant is supplied. Regenerator (G
n to G ₁ ) are operatively connected to the solution piping system and the refrigerant piping system to form a circulation cycle, and the refrigerant vapor generated in the high temperature side regenerator (Gn) is transferred to the low temperature side regenerator (Gn _−1). ) which are sequentially introduced into the low temperature side of the regenerator (Gn _-1 of the low temperature side by using as a heating source) regenerator (Gn _-1) absorbent solution of most operating temperatures the heating concentrated in An absorption type refrigerating apparatus which is repeated up to a low regenerator (G ₁ ), wherein cooling water (Wa) supplied from the same cooling water supply system is supplied to the absorber (A) and the condenser (C). And the cooling water after cooling the condenser (C) together with the cooling water supplied to the absorber (A). 5. The low pressure stage (Aa) according to claim 4, wherein the absorber (A) and the evaporator (E) have different refrigerant vaporization temperatures, and the high pressure stage (Aa) and the vaporizer (Ea) have different refrigerant vaporization temperatures.
b), (Eb), or a condenser (C) and a regenerator (G) having the lowest operating temperature.
₁ ) is divided into a high pressure stage (Ca), a high pressure stage (G ₁ a) and a low pressure stage (Cb), (G ₁ b), both of which have different refrigerant condensation temperatures, or the absorber (A) and the evaporator. (E) is divided into a low pressure stage (Aa), a high pressure stage (Aa), and a high pressure stage (Ab) (Eb), both of which have different refrigerant evaporation temperatures, and the operating temperature is the lowest with that of the condenser (C). High-pressure stage (Ca) and refrigerant (G _{1 a} ) with different refrigerant condensing temperatures with the regenerator (G ₁ )
And the low pressure stages (Cb) and (G ₁ b) are divided, while the cooling water (Wa) in the absorber (A) and the condenser (C) is in the high pressure stage (Ab) and the low pressure stage. Step (C
An absorption type refrigerating apparatus, which is configured to flow from the b) side toward the low pressure stage (Aa) and the high pressure stage (Ca) side. 6. The split flow of the cooling water (Wa), which is split and supplied to the absorber (A) and the condenser (C), to the condenser (C) side according to claim 4 or 5. An absorption type refrigerating apparatus, wherein the rate is set to a value greater than 50% and less than 100%. 7. The absorption refrigerating device according to claim 1, 2, 3, 4, 5 or 6, wherein the number n of the regenerators is 2 or 3.