JP3297720B2 - Absorption refrigerator - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

[0001] The present invention relates to an absorption refrigerator. More specifically, the present invention relates to an absorption refrigerator in which a so-called reverse cycle type steam-type double effect absorption refrigerator is combined with a solution concentration boiler. Here, the absorption refrigerator includes an absorption chiller / heater.

[0002]

2. Description of the Related Art Conventionally, a steam double-effect absorption refrigerator as exemplified in FIG. 7 has been known. This constitutes a reverse cycle in which the absorbent flows from the absorber a to the high-temperature regenerator e via the low-temperature regenerator c. The absorption cycle in this case will be described. First, an absorption liquid (dilute absorption liquid) whose concentration has been reduced by absorbing a large amount of refrigerant vapor in the absorber a is supplied from the absorber a to the low-temperature heat exchanger b.
After being heated by the low-temperature heat exchanger b, and then to the low-temperature regenerator c. The rare absorbing liquid is regenerated at a low temperature in the low-temperature regenerator c, releases a part of the absorbed refrigerant, and its concentration is increased by that amount to become an intermediate concentration absorbing liquid (intermediate absorbing liquid). Next, the intermediate absorbent is sent from the low-temperature regenerator c to the high-temperature heat exchanger d, and is heated by the high-temperature heat exchanger d and then sent to the high-temperature regenerator e.

[0003] The intermediate absorbent is regenerated at a high temperature in the high-temperature regenerator e and releases a part of the absorbed refrigerant to further increase its concentration to become a high-concentration absorbent (concentrated absorbent). Then, the concentrated absorbent is returned to the heating side of the high-temperature heat exchanger d as a heating source for heating the intermediate absorbent, and further heats the rare absorbent to the heating side of the low-temperature heat exchanger b. After being returned as a heating source, it is returned to the absorber a. The returned concentrated absorption liquid is sprayed in the absorber a, and is absorbed by the refrigerant vapor again while being cooled by the cooling water to become the rare absorption liquid.

In such a steam-type double-effect absorption refrigerator, high-temperature steam is supplied to the high-temperature regenerator e from a steam boiler f as a heating source. Is heated to release the absorbed refrigerant, and the released refrigerant vapor is used as a heating source in the low-temperature regenerator c for the low-temperature regenerator c, and then returned to the condenser g. Is condensed.

[0005] However, the steam-type absorption refrigerator combined with the steam boiler f has the following disadvantages.

[0006] The steam boiler f itself is large in size, which leads to an increase in the size of the entire absorption refrigerator. Moreover, in order to operate the steam boiler f, water supply of a system different from the absorption chiller system, recovery of the steam drain after heating, injection of chemicals, and the like are required.
Ancillary equipment for them is required, which promotes the above-mentioned enlargement. However, the contribution of the steam boiler f to the absorption refrigerator is merely to supply the heating source, and the effect corresponding to the fuel consumption for combustion in the steam boiler f is sufficiently obtained. It is hard to say that. In addition, legal regulations also involve the inconvenience of requiring a predetermined qualified person or an inspection as a handler.

[0007]

SUMMARY OF THE INVENTION The present invention has been made in view of the above-mentioned problems of the prior art, and aims to reduce the fuel consumption per cooling output and save energy by making full use of the function of a boiler. It is an object of the present invention to provide an absorption refrigerator capable of making the entire absorption refrigerator compact and easy to handle.

[0008]

The absorption refrigerator according to the present invention comprises:
Absorbent liquid, low-temperature heat exchanger, low-temperature regenerator,
A high-temperature heat exchanger, a steam-heated high-temperature regenerator, a steam-type absorption refrigerator that circulates back to the absorber via the high-temperature heat exchanger and the low-temperature heat exchanger, wherein the high-temperature regenerator and the high-temperature heat exchanger A solution concentration boiler that is interposed therebetween to heat and concentrate the absorbing solution, and a supply unit that extracts a part or all of the concentrated absorbing solution from the high-temperature regenerator and supplies the solution to the solution concentration boiler, The condensing boiler is connected to the high-temperature heat exchanger so as to return the heat-concentrated absorbent to the heating side of the high-temperature heat exchanger, while the refrigerant vapor evaporated from the absorbent in the solution condensing boiler is sent to the high-temperature regenerator. Connected to the high temperature regenerator to supply as a heating source ,
High-temperature heat exchange of part of the absorbing liquid from the near side of the intermediate liquid supply means
Orifice in the absorbent return line between the heat exchanger and the low-temperature heat exchanger.
Characterized Rukoto such by-pass through a pipe having an office.

[0009] The absorption refrigerator of the present invention includes a first heat exchanger using a return absorption liquid as a heating source, which is returned to the high-temperature heat exchanger from the outlet side of the solution concentrating boiler, and supplied from the high-temperature regenerator. The absorption liquid may be configured to exchange heat with the return absorption liquid in the first heat exchanger before being introduced into the solution concentration boiler.

Further, the absorption refrigerator of the present invention is provided with a second heat exchanger using the combustion exhaust gas of the solution concentration boiler as a heating source, and the supply absorption liquid supplied from the high temperature regenerator is supplied to the solution concentration boiler. Before the introduction, the second heat exchanger may be configured to exchange heat with the combustion exhaust gas.

Further, in the absorption refrigerator of the present invention,
The second heat exchanger may be an economizer attached to the solution concentrating boiler, and the supply absorption liquid may be configured to flow through the economizer.

Further, in the absorption refrigerator of the present invention, between the low-temperature heat exchanger and the low-temperature regenerator, the inlet side of the absorbent to the low-temperature regenerator and / or the high-temperature regeneration from the high-temperature heat exchanger. An auxiliary regenerator using the combustion exhaust gas of the solution-concentrating boiler as a heating source may be provided between the reactor and the inlet side of the absorbent to the high-temperature regenerator.

Further, in the absorption refrigerator of the present invention, the third heat exchanger for heating the rare absorbing liquid, which uses the refrigerant drain of the low-temperature regenerator as a heating source, is provided in parallel with the low-temperature heat exchanger or in the low-temperature heat exchanger. It may be arranged in series on the outlet side of the absorbent in the exchanger.

Further, in the absorption refrigerator of the present invention, the fourth heat exchanger for heating the intermediate absorption liquid, which uses the refrigerant drain of the high-temperature regenerator as a heating source, is provided in parallel with the high-temperature heat exchanger or in the high-temperature heat exchanger. It may be arranged in series on the outlet side of the absorbent in the exchanger.

[0015]

Further, in the absorption refrigerator of the present invention, a plurality of combinations of the absorber and the evaporator may be provided, and the cold water, the cooling water and the absorbing liquid may be supplied in series to the plurality of combinations. Alternatively, a plurality of combinations of the absorber and the evaporator may be provided, and the cooling water and the absorbing liquid may be supplied in series to the plurality of combinations, and the cooling water may be supplied to the plurality of combinations in parallel.

Further, in the absorption refrigerator of the present invention, the cooling water may flow from the condenser to the absorber.

In the absorption refrigerator of the present invention, it is preferable that the solution concentration boiler is a once-through boiler.

[0019]

Since the absorption refrigerator of the present invention is configured as described above, it is not necessary to provide a special water supply facility in the boiler, and it is not necessary to collect the steam drain. In addition, since a chemical injection facility is not required, the size of the boiler is reduced. As a result, the boiler can be integrated with the absorption refrigerator.

[0020]

DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, the present invention will be described based on embodiments, but the present invention is not limited to only such embodiments.

According to the present invention, instead of supplying water to the boiler, the absorbing liquid is supplied, and the boiler is directly used for the concentration of the absorbing liquid to reduce the fuel consumption per cooling output.
The principle is to use the refrigerant vapor released as a result as a heating source for a high-temperature regenerator or the like.

More specifically, the present invention relates to a method for producing a low-temperature heat exchanger, a low-temperature regenerator, a high-temperature heat exchanger, a steam-heated high-temperature regenerator, a high-temperature heat exchanger, and a low-temperature heat exchanger. A solution-concentration boiler interposed between the high-temperature regenerator and the high-temperature heat exchanger for heating and concentrating the absorption liquid; and A supply means for extracting a part or all of the concentrated absorbent from the regenerator and supplying the concentrated absorbent to the solution-concentrating boiler, for example, a pump. It is connected to the high-temperature heat exchanger so as to return to the heating side of the heat exchanger, and is connected to the high-temperature regenerator to supply the refrigerant vapor evaporated from the absorption liquid in the solution-concentrating boiler as a heating source to the high-temperature regenerator. Also It is.

Here, the "solution enrichment boiler" has a function of heating the concentrated absorbing liquid by burning fuel, a function of discharging the refrigerant absorbed by the heating as refrigerant vapor, and a function of heating the concentrated absorbing liquid. What is necessary is just to have the function which can withstand the internal pressure of this.

In the case of the present invention, the concentrated absorbent which has been regenerated at a high temperature by the high-temperature regenerator and further concentrated from the intermediate absorbent is fed to the solution concentrating boiler by the pump, and further concentrated by the solution condensing boiler. You. Then, the highly concentrated absorbent, that is, the highly heated absorbent, is returned as a heating source for the high-temperature heat exchanger and then as a heating source for the low-temperature heat exchanger. On the other hand, in the solution concentration boiler, the refrigerant is released as refrigerant vapor when the absorption liquid is concentrated, and the refrigerant vapor is supplied as a heating source of the high-temperature regenerator. As a result, the high-temperature regeneration in the high-temperature regenerator is also performed more efficiently.

As described above, by combining the absorption chiller with the solution concentration boiler, the fuel consumption per cooling output as a whole can be reduced as much as possible.
Energy and resource savings can also be achieved. Such an effect can be qualitatively obtained irrespective of the magnitude of the amount of the concentrated absorbent from the high-temperature regenerator supplied to the solution-concentrating boiler.

In addition, the present invention eliminates the need for water supply, chemical injection, steam drain recovery, and the like as in the conventional steam boiler, so that the corresponding facilities are not required, and the overall absorption refrigerator can be made compact. In addition, the energy required for them is not required, and greater energy and resource savings can be achieved.

In the present invention, the following configuration may be added from the viewpoint of improving the thermal efficiency, mainly from the viewpoint of improving the boiler efficiency of the solution concentration boiler.

That is, the first heat exchanger for exchanging heat between the supply absorption liquid supplied from the high-temperature regenerator to the solution concentration boiler and the return absorption liquid returned from the solution concentration boiler to the high-temperature heat exchanger. May be provided. In this case, the supply absorption liquid is heated by receiving heat from the return absorption liquid that has been highly heated in the first heat exchanger, and the heated supply absorption liquid is introduced into the solution concentration boiler. Therefore, the boiler efficiency is increased as compared with the case without the heat exchanger. Further, a supply absorption liquid supplied from the high-temperature regenerator to the solution concentration boiler,
A second heat exchanger for exchanging heat with the combustion exhaust gas discharged from the solution concentration boiler may be provided.

The second heat exchanger may be constituted by, for example, an economizer attached to a solution concentrating boiler, and the supply and absorption liquid may flow through the economizer. Even when such a second heat exchanger is provided,
Since the supply absorption liquid heated in the second heat exchanger is introduced into the solution concentration boiler, the boiler efficiency is increased as compared with the case without the second heat exchanger. . In addition, in this case, since the temperature of the supply and absorption liquid is raised using the combustion exhaust gas of the solution-concentrating boiler itself as a heat source, it is possible to save energy and resources.

Further, the following configuration may be added mainly from the viewpoint of energy saving.

First, between the low-temperature heat exchanger and the low-temperature regenerator and at the position of the inlet side of the absorbent to the low-temperature regenerator and / or between the high-temperature heat exchanger and the high-temperature regenerator. At the position on the inlet side of the absorbent to the high-temperature regenerator,
An auxiliary regenerator (heat exchanger) using the combustion exhaust gas of the solution concentration boiler as a heating source may be provided. In this case, since a portion of the heating heat per cooling output that needs to be heated from the outside can be covered by the combustion exhaust gas, the heating heat can be reduced as compared with the case without the auxiliary regenerator, Energy saving is achieved.

Second, a third heat exchanger for heating the rare absorbing liquid using the refrigerant drain of the low-temperature regenerator as a heating source,
The series may be attached in parallel to the low-temperature heat exchanger or on the outlet side of the diluted absorption liquid of the low-temperature heat exchanger. In this case, since a part of the heating heat per cooling output which needs to be heated from the outside can be covered by the refrigerant drain, the heating heat can be reduced as compared with the case where the third heat exchanger is not provided. Energy saving.

Third, a fourth heat exchanger for heating the intermediate absorbing liquid, which uses the refrigerant drain of the high temperature regenerator as a heating source, is provided in parallel with the high temperature heat exchanger or for the intermediate absorbing liquid of the high temperature heat exchanger. An outlet may be attached to the series. In this case, since a part of the heating heat per cooling output that needs to be heated from the outside can be covered by the refrigerant drain, the heating heat can be reduced as compared with the case without the fourth heat exchanger. Energy saving.

Fourth, a part of the intermediate absorbing liquid may be bypassed from the near side of the intermediate liquid pump (intermediate liquid supply means) to the absorbing liquid return line between the high-temperature heat exchanger and the low-temperature heat exchanger. Good. In this case, since the amount of lithium bromide supplied to the higher temperature side can be reduced, the amount of heat loss generated on the higher temperature side is reduced, improving the thermal efficiency and preventing cavitation of the rare liquid pump. And noise reduction is also achieved.

Fifth, a plurality of combinations of the absorber and the evaporator may be provided, and the cold water, the cooling water and the absorbing liquid may be supplied in series to the plurality of combinations, or the absorber and the evaporator may be provided in series. May be provided, and the cooling water and the absorbing liquid may be supplied in series to the plurality of combinations, and the cooling water may be supplied to the plurality of combinations in parallel. In this case, the inside pressure of the absorber and the inside pressure of the evaporator can be changed step by step for each group, thereby making it possible to use the absorber in a region of the concentration of the absorbing solution which is thinner than before, thereby improving the efficiency. In addition, the size of the high-temperature regenerator and the heat exchanger can be significantly reduced. As a result, downsizing of the absorption refrigerator is achieved.

Sixth, cooling water may flow from the condenser to the absorber. In this case, a rise in temperature and a rise in pressure in the high-temperature regeneration system or the boiler system, which is a drawback of the absorption refrigerator having a plurality of regenerators, can be relatively suppressed. That is, the temperature and pressure of the condenser are reduced, thereby lowering the temperature of the cold regenerator, thereby lowering the temperature of the hot regenerator, thereby lowering the temperature and pressure of the boiler system.

In the present invention, from the viewpoint of simplification of handling, a once-through boiler may be used as the solution concentration boiler. In this case, since the amount of the absorbing liquid held in the boiler is reduced, the total amount of the absorbing liquid is reduced, and the lithium in the absorbing liquid is expensive, thereby reducing the cost. It becomes possible to plan. Furthermore, when the heat transfer area is 10 m ² or less, a small boiler, 5
because it is a simple boiler in the case of m ² or less, qualified and establishment permit upon handling over it becomes unnecessary, respectively, so that the regulation of the inspection is alleviated.

[0038]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, the present invention will be described based on embodiments with reference to the attached drawings, but the present invention is not limited to only such embodiments.

Embodiment 1 FIG. 1 shows an absorption refrigerator according to Embodiment 1 of the present invention. In the first embodiment, an absorber 1, a pump (dilute liquid pump) 2, a low-temperature heat exchanger 3, a low-temperature regenerator 4, and a pump (intermediate liquid pump)
5. A once-through boiler 10 as a solution concentration boiler is combined with a reverse cycle type double effect absorption refrigerator comprising a high temperature heat exchanger 6, a high temperature regenerator 7, a condenser 8 and an evaporator 9. That is, in the first embodiment, the double effect absorption refrigerator and the solution concentration boiler 10 are integrated in a state where they are incorporated in a refrigeration cycle using an absorbent. In the first embodiment, in addition to the solution concentrating boiler 10, auxiliary regenerators 11, 12, a pump (concentrated liquid pump) 13, an additional heat exchanger 14 as a first heat exchanger, and a second heat exchanger Economizer 1 as a vessel
5 and so on are added. In FIG. 1, the arrow attached to the solid line indicates the flow direction of the absorbing liquid or the refrigerant, and the arrow attached to the broken line indicates the flow direction of the refrigerant vapor.

The circulation cycle of the absorbing solution will be described in order. First, the rare absorbing solution whose concentration has been reduced by absorbing a large amount of refrigerant vapor in the absorbing device 1 is separated from the absorbing device 1 by the dilute solution pump 2 into the low-temperature heat exchanger. 3, the low-temperature heat exchanger 3
After being heated by, it is sent to the low-temperature regenerator 4. Before being introduced into the low-temperature regenerator 4, the diluted absorbing liquid is further heated by an auxiliary regenerator 11 described later, and is introduced into the low-temperature regenerator 4 in the heated state. Then, the rare absorbing liquid is regenerated at a low temperature in the low-temperature regenerator 4, and a part of the absorbed refrigerant is released and the concentration is increased by that amount to become an intermediate absorbing liquid having an intermediate concentration.

Next, the intermediate absorbent is sent from the low-temperature regenerator 4 to the high-temperature heat exchanger 6 by the intermediate-absorbent pump 5, and after being heated by the high-temperature heat exchanger 6, is sent to the high-temperature regenerator 7. Be paid. Before being introduced into the high-temperature regenerator 7, the intermediate absorbent is further heated by the auxiliary regenerator 12 in the same manner as before the introduction into the low-temperature regenerator 4. It is adapted to be introduced into the vessel 7. The intermediate absorbing liquid is regenerated at a high temperature in the high-temperature regenerator 7 and releases a part of the absorbed refrigerant to further increase the concentration to become a high-concentration concentrated absorbing liquid.

Further, the concentrated absorption liquid is fed from the high-temperature regenerator 7 to the once-through boiler 10 by the concentrated liquid pump 13.
The refrigerant that has been further heated and absorbed by the once-through boiler 10 is discharged as refrigerant vapor, and becomes a more concentrated highly concentrated absorbent.

Here, before being introduced into the once-through boiler 10, the concentrated absorbent is first heated by the additional heat exchanger 14, and then heated by the economizer 15. That is, in the additional heat exchanger 14, the concentrated absorbent fed by the concentrated absorbent pump 13 is concentrated by the once-through boiler 10 and then returned to the high-temperature heat exchanger 6 with heat. It will be replaced and heated. In the economizer 15, the concentrated absorbent heated by the additional heat exchanger 14 exchanges heat with the combustion exhaust gas discharged from the once-through boiler 10 and is further heated.

The highly concentrated absorbent concentrated by the once-through boiler 10 passes through the heating side of the additional heat exchanger 14 and then passes through the heating side of the high-temperature heat exchanger 6 to remove the intermediate absorbent. The diluted absorbent is heated and then passed through the heating side of the low-temperature heat exchanger 3 to heat the diluted absorption liquid, and then returned to the absorber 1. In the absorber 1, the returned high-concentration absorbing liquid is sprayed and cooled by the cooling water, thereby absorbing a large amount of the refrigerant vapor supplied from the evaporator 9 and becoming a rare absorbing liquid again.

On the other hand, the refrigerant vapor evaporated in the once-through boiler 10 is sent as a steam heating source to the high-temperature regenerator 7 through the pipe 16 and used for high-temperature regeneration of the intermediate absorbent in the high-temperature regenerator 7. Then, the refrigerant vapor used in the high-temperature regenerator 7 is joined to the pipe 17. Also,
The refrigerant vapor discharged from the high-temperature regenerator 7 is sent to the low-temperature regenerator 4 as a heating source. Thus, the refrigerant vapor used for the heating joins the pipe 19 and is sent to the condenser 8, where it is condensed by the cooling water to become a refrigerant.

The combustion exhaust gas discharged from the once-through boiler 10 passes through the economizer 15 and is sent to two auxiliary regenerators 11 and 12 as a heating source. For the two auxiliary regenerators 11, 12, the combustion exhaust gas may be supplied to the auxiliary regenerator 12 first and then to the auxiliary regenerator 11 in a series, or the combustion exhaust gas may be supplied to the series. The two auxiliary regenerators 1
You may make it supply to 1 and 12 in parallel.

Example 2 Example 2 of the present invention is a modification of Example 1,
As shown by a dashed line in FIG. 1, a part of the concentrated absorption liquid is supplied to the once-through boiler 10 and the remaining part is branched by a pipe 18 so as to be supplied to the high-temperature heat exchanger 6 on the heating side. is there. That is, the pipe 18 connects the outlet side of the high-temperature regenerator 7 and the inlet side of the high-temperature heat exchanger 6 on the heating side. It should be noted that a known means such as a flow control valve may be employed for the flow control or the like of the branch portion.

According to the second embodiment, by adopting such a configuration, the amount of lithium bromide supplied to the once-through boiler can be reduced, so that the amount of heat loss generated on the boiler side and, consequently, the amount of heating can be reduced. The effect of saving energy by reduction is obtained.

Example 3 Example 3 of the present invention is a modification of Example 1,
As shown in FIG. 2, in parallel with the low-temperature heat exchanger 3, a second refrigerant in which the rare absorbing liquid is heated by the refrigerant drain from the low-temperature regenerator 4 is heated.
A low-temperature heat exchanger 21 is provided, and a second high-temperature heat exchanger 31 is provided in parallel with the high-temperature heat exchanger 6 to heat the intermediate absorbent by the refrigerant drain from the high-temperature regenerator 7.

Thus, in the third embodiment, by adopting such a configuration, the heat of the refrigerant drain cooled and radiated by the cooling water is effectively recovered for the heating of the absorbing liquid, and the amount of heating in the once-through boiler is reduced. Therefore, the effect that energy saving is achieved can be obtained.

In the illustrated example, the second low-temperature heat exchanger 21 and the second high-temperature heat exchanger 31 are arranged in parallel with the low-temperature heat exchanger 3 and the high-temperature heat exchanger 6, respectively. (2) The low-temperature heat exchanger 21 may be arranged in series with the low-temperature heat exchanger 3 on the diluted absorption liquid outlet side of the low-temperature heat exchanger 3. It may be arranged in series with the high-temperature heat exchanger 6 on the liquid outlet side.

Embodiment 4 In Embodiment 4 of the present invention, as shown in FIG. 3, a part of the intermediate absorbing liquid is fed to the high-temperature regenerator 7 by the intermediate liquid pump 5, and the remaining part is sucked by the intermediate liquid pump 5. It is branched from the near side by a pipe 41 and is directly fed to the heating side of the low-temperature heat exchanger 3. That is, the inlet side of the intermediate liquid pump 5 communicates with the inlet side of the low-temperature heat exchanger 3 on the heating side by the pipe 41. Note that the flow rate control of the branch portion may be performed by the orifice 42, for example.

Thus, in the fourth embodiment, by adopting such a configuration, the amount of the absorbing liquid supplied to the high temperature side is reduced, the amount of heat loss generated on the high temperature side is reduced, and the thermal efficiency is improved. The effect of preventing cavitation of the pump can be obtained.

Example 5 Example 5 of the present invention is a modification of Example 1, and
As shown in FIG. 4, the combination of the absorber 1 and the evaporator 9 is made into two sets, that is, the absorber 1 and the evaporator 9 are composed of a first absorption 1A unit and a first evaporator 9A in a first block. A, and a second block B composed of a set of a second absorber 1B and a second evaporator 9B.
While the block B is supplied in series to the first block A, the highly concentrated absorbing liquid is supplied in series from the first block A to the second block B.

According to the fifth embodiment, the pressure in the absorbing solution 1 and the pressure in the evaporator 9 can be changed step by step for each block by adopting such a configuration, and the absorbing solution can be formed in a wide concentration range. As a result, the range of use can be extended to a lean concentration region, and the effect of reducing the circulation amount of the absorbing solution and effectively utilizing the low-temperature heat source can be obtained.

Example 6 Example 6 of the present invention is a modification of Example 5,
As shown in FIG. 5, the combination of the absorber 1 and the evaporator 9 is made into two sets, that is, the absorber 1 and the evaporator 9 are connected to the first absorber 1A.
And a first block A composed of a set of a first evaporator 9A and a second block B composed of a set of a second absorber 1B and a second evaporator 9B. The first block A is supplied to the series, and the highly concentrated absorbing solution is supplied from the first block A to the second block B in the series.
The cooling water is supplied to the first block A and the second block B in parallel.

According to the sixth embodiment, the pressure in the absorbing solution 1 and the pressure in the evaporator 9 can be changed step by step for each block by adopting such a configuration. As a result, the usable range can be expanded to a lean concentration region, and the effect of reducing the circulation amount of the absorbing solution and effectively utilizing the low-temperature heat source can be obtained.

Example 7 Example 7 of the present invention is a modification of Example 1, and
As shown in FIG. 6, the cooling water is made to flow in series from the condenser 8 to the absorber 1 in a manner opposite to the usual case.

Thus, in the seventh embodiment, by adopting such a structure, the temperature and pressure of the condenser 8 are reduced by first passing the low-temperature cooling water through the condenser 8, thereby reducing the temperature of the low-temperature regenerator 4. The temperature and pressure drop, and the temperature of the high-temperature regenerator 7
As the pressure drops and the temperature and pressure of the boiler system decrease,
The temperature and concentration of the absorbing solution can be reduced, and an effect of effectively utilizing a low-temperature heat source can be obtained.

Although the present invention has been described based on the embodiment and the examples, the present invention is not limited to the embodiment and the examples, and various modifications are possible. For example, in the fifth embodiment and the sixth embodiment, the combination of the absorber 1 and the evaporator 9 is two, but may be three or more.

[0061]

As described above in detail, according to the absorption refrigerator of the present invention, by integrating the absorption refrigerator with the solution concentration boiler, the overall fuel consumption per cooling output can be reduced. As well as energy and resource savings,
In addition, an excellent effect that the entire absorption refrigerator can be downsized can be obtained.

When introducing the supply absorption liquid into the solution concentration boiler, the supply absorption liquid is supplied to the first heat exchanger using the product (highly concentrated absorption liquid) in the solution concentration boiler as a heat source, or to the solution concentration boiler. By providing one or both of the second heat exchangers that use the exhaust gas (combustion exhaust gas) from the boiler as a heat source, it is possible to increase the boiler efficiency and also achieve greater energy and resource savings. That is an excellent effect.

Further, an auxiliary regenerator using the above-mentioned effluent from the solution condensing boiler as a heat source is provided at a position on the inlet side of the absorbent to the low temperature regenerator and / or at a position on the side of the absorbent inlet to the high temperature regenerator. Thereby, an excellent effect that the amount of heating heat per cooling output, which needs to be heated from the outside, can be reduced, and further energy saving can be achieved.

In addition, the use of a once-through boiler as the solution concentrating boiler has the effect of reducing the cost of the absorbing solution in addition to making the entire absorption refrigerator compact and easy to handle.

[Brief description of the drawings]

FIG. 1 is a schematic diagram of Embodiment 1 of the present invention.

FIG. 2 is a schematic diagram of Embodiment 3 of the present invention.

FIG. 3 is a schematic view of Embodiment 4 of the present invention.

FIG. 4 is a schematic diagram of a main part of a fifth embodiment of the present invention.

FIG. 5 is a schematic diagram of a main part of a sixth embodiment of the present invention.

FIG. 6 is a schematic diagram of Embodiment 7 of the present invention.

FIG. 7 is a schematic view of a conventional absorption refrigerator.

[Explanation of symbols]

 Reference Signs List 1 absorber 3 low-temperature heat exchanger 4 low-temperature regenerator 6 high-temperature heat exchanger 7 high-temperature regenerator 10 once-through boiler (solution concentration boiler) 11, 12 auxiliary regenerator 13 concentrated liquid pump (pump) 14 additional heat exchanger (first Heat exchanger) 15 Economizer (second heat exchanger)

──────────────────────────────────────────────────の Continuing on the front page (72) Inventor Kenichi Saito 1000 Aomachi-cho, Kusatsu-shi, Shiga Prefecture Inside Kawashii Refrigerating Industry Co., Ltd. (56) References JP-A-1-98865 (JP, A) JP-A-10-205908 (JP, A) JP-A-63-290363 (JP, A) JP-A-3-152362 (JP, A) JP-A-60-178265 (JP, A) JP-A-7-218015 (JP, A) JP-A-3-152357 (JP, A) JP-A-62-272068 (JP, A) JP-A-59-225266 (JP, A) JP-A-2-290474 (JP, A) JP-A-9-250837 (JP, A) JP-A-58-219371 (JP, A) JP-A-60-134172 (JP, A) JP 60-21727 (JP, Y1) Table 9-512332 (JP, A) (58) Survey The field (Int.Cl. ^7, DB name) F25B 15/00 102 F25B 15/00 303

Claims (11)

(57) [Claims] 1. A low-temperature heat exchange of an absorbing liquid in order from an absorber.
, Low-temperature regenerator, high-temperature heat exchanger, steam-heated high-temperature regeneration
Through the heat exchanger, the high-temperature heat exchanger and the low-temperature heat exchanger.
In a steam absorption refrigerator that circulates back to the collector, it is interposed between the high-temperature regenerator and the high-temperature heat exchanger and absorbed.
A solution condensing boiler for heating and concentrating the liquid;
Extract a part or all of the concentrated absorption solution and concentrate the solution.
Supply means for supplying to the boiler, wherein the solution-concentrating boiler heats and concentrates the absorbent to the high temperature.
Connected to the high temperature heat exchanger to return to the heating side of the heat exchanger
While evaporating from the absorbent in the solution concentration boiler
Supply the cooled refrigerant vapor to the high-temperature regenerator as a heating source
To be connected with the high temperature regenerator, High-temperature heat exchange of part of the absorbing liquid from the near side of the intermediate liquid supply means
Orifice in the absorbent return line between the heat exchanger and the low-temperature heat exchanger.
Do not bypass by piping with Features
And absorption refrigerator. 2. A method according to claim 1, further comprising a first heat exchanger that uses a return absorbing liquid returned from an outlet side of the solution concentrating boiler to the high temperature heat exchanger as a heating source, wherein the supply absorbing liquid supplied from the high temperature regenerator is the solution condensing liquid. 2. The absorption refrigerator according to claim 1, wherein heat is exchanged between the first heat exchanger and the return absorption liquid before introduction into the boiler. 3. 3. A second heat exchanger using a combustion exhaust gas of a solution condensing boiler as a heating source, wherein a supply absorption liquid supplied from a high-temperature regenerator is subjected to the second heat exchange before being introduced into the solution condensing boiler. 3. The absorption chiller according to claim 1, wherein the chiller is configured to exchange heat with the combustion exhaust gas. 4. The absorption refrigeration according to claim 3, wherein the second heat exchanger is an economizer attached to the solution concentrating boiler, and the supply and absorption liquid is heated by the economizer. Machine. 5. The absorption liquid from the low-temperature heat exchanger to the low-temperature regenerator and the inlet side of the absorbent to the low-temperature regenerator, and / or the high-temperature heat exchanger to the high-temperature regenerator and 5. The absorption refrigerator according to claim 1, further comprising an auxiliary regenerator provided on the inlet side to the high-temperature regenerator, the auxiliary regenerator using a combustion exhaust gas of the solution-concentrating boiler as a heating source. 6. A third heat exchanger for heating the rare absorbing liquid, which uses a refrigerant drain of the low-temperature regenerator as a heating source, is connected in series with the low-temperature heat exchanger or at the outlet side of the absorbing liquid of the low-temperature heat exchanger. The absorption refrigerator according to any one of claims 1, 2, 3, 4 and 5, wherein the absorption refrigerator is provided. 7. A fourth heat exchanger for heating the intermediate absorption liquid, which uses the refrigerant drain of the high temperature regenerator as a heating source, is connected in series with the high temperature heat exchanger or at the outlet side of the absorption liquid of the high temperature heat exchanger. The absorption refrigerator according to any one of claims 1, 2, 3, 4, 5, and 6, wherein the absorption refrigerator is provided. 8. The method according to claim 1, wherein a plurality of combinations of the absorber and the evaporator are provided, and the cold water, the cooling water and the absorbing liquid are supplied in series to the plurality of combinations.
8. The absorption refrigerator according to 2, 3, 4, 5, 6, or 7 . 9. A plurality of combinations of an absorber and an evaporator are provided, chilled water and an absorbing liquid are supplied in series to the plurality of combinations, and cooling water is supplied to the plurality of combinations in parallel. Claims 1, 2, 3, 4,
8. The absorption refrigerator according to 5, 6 or 7 . 10. The method according to claim 1, wherein cooling water is supplied from the condenser to the absorber.
6. The absorption refrigerator according to 6, 7, 8 or 9 . 11. The method according to claim 1, wherein the solution-concentrating boiler is a once-through boiler.
11. The absorption refrigerator according to 8, 9 or 10 .