JP2001133067A - Absorption refrigerating machine - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide an absorption refrigerating machine in which fuel consumption per cooling output is reduced while saving energy by utilizing the function of a boiler sufficiently and which can be handled easily by making compact the entirety of the absorption refrigerating machine. SOLUTION: An evaporative absorption refrigerating machine circulating absorption liquid from an absorber 1 through a low temperature heat exchanger 3, a low temperature regenerator 4, a high temperature heat exchanger 6, a vapor heating high temperature regenerator 7, the high temperature heat exchanger 6 and the low temperature heat exchanger 3 to the absorber 1 comprises a boiler 10 for thermally condensing the absorption liquid interposed between the high temperature regenerator 7 and the high temperature heat exchanger 6, and a pump 13 for extracting concentrated absorption liquid from the high temperature regenerator 7 partially or entirely and supplying it to the solution condensing boiler. The solution condensing boiler 10 is coupled with the high temperature heat exchanger 6 to return the thermally condensed absorption liquid to the heating side thereof and coupled with the high temperature regenerator 7 to supply refrigerant vapor evaporated from the absorption liquid in the solution condensing boiler 10, as a heat source, to the high temperature regenerator 7.

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. 9 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]

According to a first embodiment of the absorption refrigerator of the present invention, a low-temperature heat exchanger, a low-temperature regenerator, a high-temperature heat exchanger, a steam-heated high-temperature regenerator, In a steam absorption refrigerator that circulates back to the absorber through the high-temperature heat exchanger and the low-temperature heat exchanger, a first bypass for returning a part of the absorbent from the low-temperature regenerator to a concentrated absorbent line A second bypass line for returning a part of the absorbent from the high-temperature regenerator to the concentrated absorbent line, and heating the absorbent by being interposed between the high-temperature regenerator and the high-temperature heat exchanger. A solution concentration boiler to be concentrated, and an additional heat exchanger interposed between the high temperature regenerator and the solution concentration boiler and heating the absorbing solution from the high temperature regenerator with the absorbing solution concentrated by the solution concentration boiler And the high temperature regeneration And an exhaust gas heat recovery unit that is interposed between the solution concentrating boiler and heats the absorbing solution with the exhaust gas from the solution condensing boiler, and extracts the concentrated absorbing solution from the high temperature regenerator to the solution condensing boiler. Supply means for supplying, the refrigerant vapor generated from the solution concentration boiler,
The high temperature regenerator is supplied as a heating source.

In a second embodiment of the absorption refrigerator of the present invention, a low-temperature heat exchanger, a low-temperature regenerator, a high-temperature heat exchanger, a steam-heated high-temperature regenerator, the high-temperature heat exchanger, and a low-temperature A steam-type absorption refrigerator that circulates back to the absorber through a heat exchanger, wherein a first bypass line for returning a part of the absorption liquid from the low-temperature regenerator to a concentrated absorption liquid line; A second bypass line for returning a part of the absorbent from the bypass to a concentrated absorbent line, a solution concentration boiler interposed between the high-temperature regenerator and the high-temperature heat exchanger to heat and concentrate the absorbent, An additional heat exchanger interposed between the high-temperature regenerator and the solution-concentrating boiler to heat the absorbing solution from the high-temperature regenerator with the absorbing solution concentrated by the solution-concentrating boiler; and the high-temperature heat exchanger. And distributed in parallel An exhaust gas heat recovery unit that heats an absorbing solution with exhaust gas from the solution concentration boiler, and a supply unit that extracts a concentrated absorption solution from the high temperature regenerator and supplies the concentrated absorption solution to the solution concentration boiler. The refrigerant vapor generated from the condensing boiler is supplied to the high-temperature regenerator as a heating source.

In a third embodiment of the absorption refrigerator of the present invention, a low-temperature heat exchanger, a low-temperature regenerator, a high-temperature heat exchanger, a steam-heated high-temperature regenerator, the high-temperature heat exchanger, In a steam absorption refrigerator circulating back to the absorber through a low-temperature heat exchanger, a first bypass line for returning a part of the absorption liquid from the low-temperature regenerator to a concentrated absorption liquid line; A second bypass line for returning a part of the absorbent from the vessel to a concentrated absorbent line, and a solution concentration boiler interposed between the high-temperature regenerator and the high-temperature heat exchanger for heating and concentrating the absorbent. An additional heat exchanger interposed between the high-temperature regenerator and the solution-concentrating boiler to heat the absorbing solution from the high-temperature regenerator with the absorbing solution concentrated by the solution-concentrating boiler; Branch on the entrance side of And an exhaust gas heat recovery unit that regenerates a part of the absorbing solution with the exhaust gas from the solution-concentrating boiler, and a supply that extracts the concentrated absorbing solution from the high-temperature regenerator and supplies it to the solution-concentrating boiler. Means, wherein the refrigerant vapor generated from the solution-concentrating boiler is supplied as a heating source to the high-temperature regenerator, and the refrigerant vapor generated from the exhaust gas heat recovery unit supplies a heating source to the low-temperature regenerator. It is characterized by being supplied as.

In a fourth embodiment of the absorption refrigerator of the present invention, a low-temperature heat exchanger, a low-temperature regenerator, a high-temperature heat exchanger, a steam-heated high-temperature regenerator, the high-temperature heat exchanger, In a steam absorption refrigerator circulating back to the absorber through a low-temperature heat exchanger, a first bypass line for returning a part of the absorption liquid from the low-temperature regenerator to a concentrated absorption liquid line; A second bypass line for returning a part of the absorbent from the vessel to a concentrated absorbent line, and a solution concentration boiler interposed between the high-temperature regenerator and the high-temperature heat exchanger for heating and concentrating the absorbent. An additional heat exchanger interposed between the high-temperature regenerator and the solution-concentrating boiler to heat the absorbing solution from the high-temperature regenerator with the absorbing solution concentrated by the solution-concentrating boiler; And solution concentrating boil And a first exhaust gas heat recovery unit that heats the absorption liquid with the exhaust gas from the solution-concentrating boiler, and heats the refrigerant drain from the high-temperature regenerator with the exhaust gas from the solution-concentrating boiler. A fourth exhaust gas heat recovery unit, and a supply unit for extracting the concentrated absorption liquid from the high-temperature regenerator and supplying the concentrated absorption liquid to the solution-concentrating boiler; On the other hand, the refrigerant drain is supplied as a heating source, and the refrigerant drain heated by the fourth exhaust gas heat recovery unit is supplied to the low temperature regenerator as a heating source.

In the absorption refrigerator of the present invention, a second low-temperature heat exchanger is provided in parallel with the low-temperature heat exchanger, and the refrigerant drain from the low-temperature regenerator is supplied to the second low-temperature heat exchanger. It may be configured to be supplied as a heating source.

In the absorption refrigerator of the present invention, a second low-temperature heat exchanger is provided in parallel with the low-temperature heat exchanger, and the second low-temperature heat exchanger is provided with a refrigerant from the high-temperature regenerator. Drain may be supplied as a heating source. In this case, a third low-temperature heat exchanger is provided in parallel with the low-temperature heat exchanger, and the refrigerant drain from the low-temperature regenerator is supplied to the third low-temperature heat exchanger as a heating source. May be.

Further, in the absorption refrigerator of the present invention,
A second high-temperature heat exchanger disposed in parallel with the high-temperature heat exchanger, and a refrigerant drain from the high-temperature regenerator is supplied to the second high-temperature heat exchanger as a heating source. Good. In this case, a second low-temperature heat exchanger is provided in parallel with the low-temperature heat exchanger, and the refrigerant drain from the high-temperature regenerator is supplied to the second high-temperature heat exchanger as a heating source. The second low-temperature heat exchanger may be supplied with the refrigerant drain after the heat exchange in the second high-temperature heat exchanger, or the low-temperature regeneration may be performed as a heating source of the second low-temperature heat exchanger. The refrigerant drain from the vessel may be supplied.

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.

Furthermore, 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.

[0018]

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.

[0019]

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.

Basically, according to the present invention, the absorption liquid is supplied in the order from the absorber to a low-temperature heat exchanger, a low-temperature regenerator, a high-temperature heat exchanger, a steam-heated high-temperature regenerator, the high-temperature heat exchanger and the low-temperature heat exchange. 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 example, a pump, for extracting a part or all of the concentrated absorption liquid from the regenerator and supplying the concentrated absorption liquid to the solution concentration boiler, the absorption solution having been heated and concentrated by the solution concentration boiler ( High-concentration absorption liquid) is connected to the high-temperature heat exchanger so as to return to the heating side of the high-temperature heat exchanger, and refrigerant vapor evaporated from the absorption liquid in the solution-concentrating boiler is supplied to the high-temperature regenerator as a heating source. So that the high temperature Those formed by connecting the raw device.

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,
What is necessary is just to have the function which can withstand the internal pressure at the time of heating of a thick absorption liquid.

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-concentrating boiler. You. Then, the highly concentrated absorbent, that is, the highly concentrated 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 also unnecessary, and the entire 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 in order to improve the thermal efficiency, mainly in order to improve the boiler efficiency of the solution concentration boiler.

That is, a first heat exchange in which heat is exchanged between a supply absorption liquid supplied from the high-temperature regenerator to the solution-concentrating boiler and a high-concentration absorption liquid returned from the solution-concentration boiler to the high-temperature heat exchanger. A container may be provided. In this case, the supply absorption liquid is heated by receiving heat from the highly concentrated absorption liquid in the first heat exchanger, and the heated supply absorption liquid is introduced into the solution concentration boiler. Thus, the boiler efficiency can be increased as compared with the case without the heat exchanger. Further, a second heat exchanger may be provided for exchanging heat between the supply-absorbing liquid supplied from the high-temperature regenerator to the solution-concentrating boiler and the combustion exhaust gas discharged from the solution-concentrating boiler. .

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, an exhaust gas heat recovery device for heating the intermediate absorption liquid by using the combustion exhaust gas of the solution-concentrating boiler as a heating source, that is, a second high-temperature heat exchanger may be provided in parallel with the high-temperature heat exchanger. Further, an exhaust gas heat recovery unit that heats and regenerates the intermediate absorption liquid by using the combustion exhaust gas of the solution-enriched boiler as a heating source downstream of the high-temperature heat exchanger, that is, an auxiliary regenerator may be provided. An exhaust gas heat recovery unit that heats the refrigerant drain from the high-temperature regenerator using the heat source as a heat source, that is, a refrigerant drain heater may be additionally provided. In this case, since a part of the heating heat per cooling output that needs to be supplied from the outside can be covered by the combustion exhaust gas, the heating heat is reduced as compared with the case where the auxiliary regenerator and the refrigerant drain heater are not provided. And energy saving is achieved.

Second, a first refrigerant heat recovery unit for heating the rare absorbing liquid using the refrigerant drain of the low-temperature regenerator as a heating source,
That is, the second low-temperature heat exchanger may be provided in series with the low-temperature heat exchanger or at 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 that needs to be supplied from the outside can be covered by the refrigerant drain, the heating heat can be reduced as compared with the case where the refrigerant heat recovery unit is not provided. Energy saving is achieved.

Third, a second refrigerant heat recovery unit for heating the rare absorbing liquid using the refrigerant drain of the high temperature regenerator as a heating source,
That is, the third low-temperature heat exchanger may be provided in series with the low-temperature heat exchanger or at 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 that needs to be supplied from the outside can be covered by the refrigerant drain, the heating heat can be reduced as compared with the case where the refrigerant heat recovery unit is not provided. Energy saving is achieved.

Fourth, a third refrigerant heat recovery unit for heating the intermediate absorption liquid using the refrigerant drain of the high temperature regenerator as a heating source, that is, a third high temperature heat exchanger is provided in parallel with the high temperature heat exchanger or in the high temperature heat exchanger. A fourth refrigerant heat recovery unit that is attached to the series on the outlet side of the intermediate absorption liquid of the exchanger and that uses the refrigerant drain after heating the third refrigerant heat recovery unit as a heat source and heats the rare absorption liquid, that is, A fourth low-temperature heat exchanger may be attached in series with the low-temperature heat exchanger or on the outlet side of the diluted absorbent of the low-temperature heat exchanger. In this case, since a part of the heating heat per cooling output that needs to be supplied from the outside can be covered by the refrigerant drain, the heating heat can be reduced when the third refrigerant heat recovery unit and the fourth refrigerant heat recovery unit are not provided. As a result, it is possible to reduce the energy consumption, thereby saving energy.

Fifth, a third refrigerant heat recovery device that heats the intermediate absorbent using 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. A fifth refrigerant heat recovery unit, which is attached to the series at the outlet side and heats the rare absorbing liquid by using the refrigerant drain after heating the third refrigerant heat recovery unit and the refrigerant drain of the low-temperature regenerator as heating sources, that is, the fifth refrigerant heat recovery unit A low-temperature heat exchanger may be provided in series with the low-temperature heat exchanger or at the outlet side of the diluted absorbent of the low-temperature heat exchanger. In this case, since a part of the heating heat per cooling output that needs to be supplied from the outside can be covered by the refrigerant drain, the heating heat can be supplied without the third refrigerant heat recovery unit and the fifth refrigerant heat recovery unit. As a result, it is possible to reduce the energy consumption, thereby saving energy.

Sixth, a part of the intermediate absorption liquid is bypassed from the front side of the intermediate liquid pump (intermediate liquid supply means) to the absorption liquid return line between the high-temperature heat exchanger and the low-temperature heat exchanger. Is also 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.

Seventh, 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. 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.

Eighth, 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 simplicity 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.

[0039]

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 concentration boiler 10, the first additional heat exchanger 14, the first exhaust gas heat recovery unit 21, the second exhaust gas heat recovery unit 22, the third exhaust gas heat recovery unit 23, the fourth Exhaust gas heat recovery unit 24, pump (concentrated liquid pump) 13, first bypass line 41 branched from before intermediate liquid pump 5 and connected to concentrated absorbent line 43, branched from before concentrated liquid pump 13. A second bypass line 42 and the like connected to the return concentrated absorbent line 43 are added. The flow control and the like in the first bypass line 41 and the second bypass line 42 are achieved by well-known means such as a flow control valve.

In the first embodiment, the first exhaust gas heat recovery unit 21 is specifically an economizer 21 for heating the concentrated absorbent from the high temperature regenerator 7, and the second exhaust gas heat recovery unit 22 is Specifically, it is a second high-temperature heat exchanger 6A for heating the intermediate absorbent, and the third exhaust gas heat recovery unit 23 is specifically an auxiliary regenerator 23 for auxiliary regeneration of the intermediate absorbent. 4 The exhaust gas heat recovery unit 24 is a refrigerant drain heater 24 for heating the refrigerant drain from the high temperature regenerator 7. 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.

Next, the circulation cycle of the absorbent will be described in order.

First, a diluted absorption liquid whose concentration has been reduced by absorbing a large amount of refrigerant vapor in the absorber 1 is sent from the absorber 1 to the low-temperature heat exchanger 3 by the diluted liquid pump 2, and the low-temperature heat exchange is performed. After being heated by the unit 3, it is sent to the low-temperature regenerator 4. 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-concentration intermediate absorbing liquid.

Then, a part of the intermediate absorbent is sent from the low-temperature regenerator 4 to the high-temperature heat exchanger 6 and the second high-temperature heat exchanger 6A in parallel by the intermediate absorbent pump 5, and the high-temperature heat exchanger 6 And after being heated by the second high-temperature heat exchanger 6A, they are merged and sent to the high-temperature regenerator 7,
A part of the combined intermediate absorbent is branched before being introduced into the high-temperature regenerator 7, sent to the auxiliary regenerator 20, and subjected to auxiliary regeneration by the auxiliary regenerator 20. At the same time, the refrigerant vapor generated by the regeneration is merged by the pipe 18 into the pipe 17 that supplies the refrigerant vapor line of the high-temperature regenerator 7 to the low-temperature regenerator 4.
On the other hand, the remainder of the intermediate absorbent is returned to the concentrated absorbent line 43 by the first bypass line 41.

The intermediate absorbent introduced into the high-temperature regenerator 7 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, thereby increasing the concentration of the concentrated absorbent. Becomes

Further, a part of the concentrated absorbing liquid is fed from the high-temperature regenerator 7 to the once-through boiler 10 by the concentrated liquid pump 13, and the refrigerant further heated and absorbed by the once-through boiler 10 as refrigerant vapor. It is released and becomes a more concentrated highly concentrated liquid. On the other hand, the remaining part of the concentrated absorbent is returned to the concentrated absorbent line by the second bypass line 42.

Here, a part of the concentrated absorbing liquid is supplied to the additional heat exchanger 14 and the economizer 21 in parallel before being introduced into the once-through boiler 10, and is supplied by the additional heat exchanger 14 and the economizer 21. Heated. After being heated, they are combined and supplied to the once-through boiler 10. 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. It will be replaced and heated.
Further, in the economizer 21, the concentrated absorbent supplied by the concentrated absorbent pump 13 is heated by exchanging heat with the combustion exhaust gas discharged from the once-through boiler 10.

The highly concentrated absorbent concentrated by the once-through boiler 10 is returned to the heating side of the additional heat exchanger 14 via the concentrated absorbent line 43 as described above, and then the high-temperature heat exchange is performed. The intermediate absorbent is passed through the heating side of the vessel 6 to heat the intermediate absorbent, and then passed through the heating side of the low-temperature heat exchanger 3 to heat the diluted absorbent, 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. The refrigerant vapor that has been used in the high-temperature regenerator 7 is sent to the refrigerant drain heater 24 and is heated by the combustion exhaust gas before being joined to the pipe 17. The refrigerant vapor discharged from the high-temperature regenerator 7 is sent to the low-temperature regenerator 4 through a pipe 17 as a heating source. Thus, the refrigerant vapor used for the heating is joined to the pipe 19 and sent to the condenser 8 together with the refrigerant vapor from the low-temperature regenerator 4, and 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 21 and then flows through the refrigerant drain heater 24, the second high-temperature heat exchanger 6A, the auxiliary regenerator 2
3 is sent as a heating source. In this case, the combustion exhaust gas may be supplied in the order of the auxiliary regenerator 23, the second high-temperature heat exchanger 6A, and the refrigerant drain heater 24, or the auxiliary regenerator 23, the second high-temperature heat exchanger 6
A, It may be supplied to the refrigerant drain heater 24 in parallel.

As described above, according to the first embodiment, since the retained calorie of the combustion exhaust gas discharged from the once-through boiler 10 is effectively recovered, energy can be saved by reducing the amount of heating supplied from the outside. Is obtained. Further, since a part of the intermediate absorption liquid and the concentrated absorption liquid is returned to the concentrated absorption liquid line 43, the amount of lithium bromide supplied to the once-through boiler 10 can be reduced.
Therefore, in addition to the effect of reducing the amount of heat loss generated on the boiler side, the effect of preventing cavitation of the intermediate absorption liquid pump 5 and the concentrated liquid pump 13 is obtained.

Example 2 Example 2 of the present invention is a modification of Example 1,
As shown in FIG. 2, a first refrigerant heat recovery unit 31 for heating the rare absorbing liquid in parallel to the low temperature heat exchanger 3, that is, a second low temperature heat exchanger 3A is added. As a heating source of the second low-temperature heat exchanger 3A, the refrigerant drain from the low-temperature regenerator 4 is used. Then, the refrigerant drain used for this heating is joined to the pipe 19.

The remaining structure of the second embodiment is the same as that of the first embodiment.
Is the same as

In the second embodiment, however, by adopting such a configuration, the heat retained in the refrigerant drain is recovered, so that an effect of saving energy by reducing the amount of heating supplied from the outside can be obtained.

Example 3 Example 3 of the present invention is a modification of Example 2;
As shown in FIG. 3, the refrigerant drain heater 24 is eliminated, and the second refrigerant heat recovery unit 32 that heats the rare absorbing liquid in parallel to the low-temperature heat exchanger 3 and the second low-temperature heat exchanger 3A,
That is, the third low-temperature heat exchanger 3B is added. As a heating source of the third low-temperature heat exchanger 3B, a refrigerant drain from the high-temperature regenerator 7 is used. Then, the refrigerant drain used for this heating is joined to the pipe 19.

The remaining structure of the third embodiment is the same as that of the second embodiment.
Is the same as

In the third embodiment, however, by adopting such a configuration, the heat retained in the refrigerant drain is recovered, so that the effect of reducing the amount of heating supplied from the outside to save energy can be obtained.

Example 4 Example 4 of the present invention is a modification of Example 2;
As shown in FIG. 4, the first refrigerant drain heater 24 is eliminated, and the first refrigerant heat recovery unit 31, which heats the rare absorbing liquid in parallel with the low temperature heat exchanger 3, that is, the second low temperature heat exchanger 3A is used. In addition, the heat source of the second high-temperature heat exchanger 6A is a refrigerant drain. That is, the second high-temperature heat exchanger 6A serves as the second refrigerant heat recovery unit 32. Here, the heating sources of the first refrigerant heat recovery unit 31 and the second refrigerant heat recovery unit 32 are both the refrigerant drain from the high-temperature regenerator 7 and the heating by the heat is performed by the second high-temperature heat exchanger 6A and the second high-temperature heat exchanger 6A. The order is 2 low-temperature heat exchangers 3A. The refrigerant drain used for this heating is connected to the pipe 1
9

The remaining structure of the fourth embodiment is the same as that of the second embodiment.
Is the same as

However, in the fourth embodiment, by adopting such a configuration, the heat retained in the refrigerant drain is recovered, so that the effect of reducing the amount of heat supplied from the outside to save energy can be obtained.

Example 5 Example 5 of the present invention is a modification of Example 4,
As shown in FIG. 5, the heating source of the first refrigerant heat recovery unit 31 is changed. That is, the first refrigerant heat recovery unit 3
As the first heating source, a mixed drain of the refrigerant drain after heating the second refrigerant heat recovery unit 32 and the refrigerant drain from the low-temperature regenerator 4 is used.

The remaining structure of the fifth embodiment is the same as that of the second embodiment.
Is the same as

However, in the fifth embodiment, by adopting such a configuration, the heat retained in the refrigerant drain is recovered, so that the effect of reducing the amount of heating supplied from the outside to save energy can be obtained.

Example 6 Example 6 of the present invention is a modification of Example 1,
As shown in FIG. 6, 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 evaporator 9A, and a second block B composed 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 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 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 7 Example 7 of the present invention is a modification of Example 6,
As shown in FIG. 7, 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 seventh 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 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 8 Example 8 of the present invention is a modification of Example 1, and
As shown in FIG. 8, 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.

According to the eighth embodiment, the temperature and pressure of the condenser 8 are reduced by first passing the low-temperature cooling water to the condenser 8 by adopting such a configuration. 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 embodiments and the examples, the present invention is not limited to the embodiments and the examples, and various modifications are possible. For example, in the sixth and seventh embodiments, the combination of the absorber 1 and the evaporator 9 is two, but may be three or more.

[0071]

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 and absorption liquid into the solution concentration boiler, the supply and 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, by providing an auxiliary regenerator using the above-mentioned effluent from the solution condensing boiler as a heating source at a position on the absorption liquid inlet side to the high-temperature regenerator, a cooling output required for external heating is required. An excellent effect that the amount of heat of heating can be reduced and further energy saving can be achieved is also obtained.

In addition, by using a once-through boiler as the solution-concentrating boiler, it is possible to obtain 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 2 of the present invention.

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

FIG. 4 is a schematic diagram of Embodiment 4 of the present invention.

FIG. 5 is a schematic view of Embodiment 5 of the present invention.

FIG. 6 is a schematic diagram of a main part of a sixth embodiment of the present invention.

FIG. 7 is a schematic diagram of a main part of a seventh embodiment of the present invention.

FIG. 8 is a schematic diagram of Embodiment 8 of the present invention.

FIG. 9 is a schematic view of a conventional absorption refrigerator.

[Explanation of symbols]

 DESCRIPTION OF SYMBOLS 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) 13 Concentrated liquid pump (pump) 14 Additional heat exchanger (first heat exchanger) 21 Economizer (Second heat exchanger)

 ──────────────────────────────────────────────────の Continued on the front page (72) Inventor Eiji Arai 1000 Aochi-cho, Kusatsu-shi, Shiga Prefecture Kawagei-Hiroshi Kogyo Co., Ltd. Co., Ltd. F term (reference) 3L093 BB16 BB22 BB29 BB37

Claims (14)

[Claims] 1. An absorbent is supplied to the absorber through a low-temperature heat exchanger, a low-temperature regenerator, a high-temperature heat exchanger, a steam-heated high-temperature regenerator, the high-temperature heat exchanger, and a low-temperature heat exchanger in this order from the absorber. In a steam absorption refrigerator circulating back, a first bypass line for returning a part of the absorption liquid from the low-temperature regenerator and bypassing the concentrated absorption liquid line, and returning a part of the absorption liquid from the high-temperature regenerator. A second bypass line for bypassing the concentrated absorbent line, a solution concentrating boiler interposed between the high temperature regenerator and the high temperature heat exchanger for heating and condensing the absorbent, the high temperature regenerator and the solution condensing boiler, Interposed between
An additional heat exchanger that heats the absorbing solution from the high-temperature regenerator with the absorbing solution concentrated by the solution-concentrating boiler, and is interposed between the high-temperature regenerator and the solution-concentrating boiler;
An exhaust gas heat recovery unit that heats an absorbing solution with exhaust gas from the solution concentration boiler, and a supply unit that extracts a concentrated absorption solution from the high temperature regenerator and supplies the solution to the solution concentration boiler. An absorption refrigerator wherein the generated refrigerant vapor is supplied to the high-temperature regenerator as a heating source. 2. The absorbent is passed through the low-temperature heat exchanger, the low-temperature regenerator, the high-temperature heat exchanger, the steam-heated high-temperature regenerator, the high-temperature heat exchanger and the low-temperature heat exchanger in order from the absorber to the absorber. In a steam absorption refrigerator circulating back, a first bypass line for returning a part of the absorption liquid from the low-temperature regenerator and bypassing the concentrated absorption liquid line, and returning a part of the absorption liquid from the high-temperature regenerator. A second bypass line for bypassing the concentrated absorbent line, a solution concentrating boiler interposed between the high temperature regenerator and the high temperature heat exchanger for heating and condensing the absorbent, the high temperature regenerator and the solution condensing boiler, Interposed between
An additional heat exchanger for heating the absorbing solution from the high-temperature regenerator with the absorbing solution concentrated by the solution-concentrating boiler; and an additional heat exchanger disposed in parallel with the high-temperature heat exchanger to absorb the exhaust gas from the solution-concentrating boiler. An exhaust gas heat recovery unit that heats the liquid; and a supply unit that extracts the concentrated absorption liquid from the high temperature regenerator and supplies the concentrated absorption liquid to the solution concentration boiler. An absorption refrigerating machine characterized by being supplied as a heating source to a vessel. 3. The absorbent is passed through the low-temperature heat exchanger, the low-temperature regenerator, the high-temperature heat exchanger, the steam-heated high-temperature regenerator, the high-temperature heat exchanger, and the low-temperature heat exchanger in order from the absorber to the absorber. In a steam absorption refrigerator circulating back, a first bypass line for returning a part of the absorption liquid from the low-temperature regenerator and bypassing the concentrated absorption liquid line, and returning a part of the absorption liquid from the high-temperature regenerator. A second bypass line for bypassing the concentrated absorbent line, a solution concentrating boiler interposed between the high temperature regenerator and the high temperature heat exchanger for heating and condensing the absorbent, the high temperature regenerator and the solution condensing boiler, Interposed between
An additional heat exchanger that heats the absorbing solution from the high-temperature regenerator with the absorbing solution concentrated by the solution-concentrating boiler; An exhaust gas heat recovery unit that regenerates a part of the absorption liquid with the exhaust gas; and a supply unit that extracts the concentrated absorption liquid from the high-temperature regenerator and supplies the concentrated absorption liquid to the solution concentration boiler. Steam is supplied to the high-temperature regenerator as a heating source, and refrigerant vapor generated from the exhaust gas heat recovery unit is supplied to the low-temperature regenerator as a heating source. Absorption refrigerator. 4. The absorbent is passed through the low-temperature heat exchanger, the low-temperature regenerator, the high-temperature heat exchanger, the steam-heated high-temperature regenerator, the high-temperature heat exchanger, and the low-temperature heat exchanger in order from the absorber to the absorber. In a steam absorption refrigerator circulating back, a first bypass line for returning a part of the absorption liquid from the low-temperature regenerator and bypassing the concentrated absorption liquid line, and returning a part of the absorption liquid from the high-temperature regenerator. A second bypass line for bypassing the concentrated absorbent line, a solution concentrating boiler interposed between the high temperature regenerator and the high temperature heat exchanger for heating and condensing the absorbent, the high temperature regenerator and the solution condensing boiler, Interposed between
An additional heat exchanger for heating the absorbing solution from the high-temperature regenerator with the absorbing solution concentrated by the solution-concentrating boiler; and an exhaust gas heat for heating the refrigerant drain from the high-temperature regenerator by the exhaust gas from the solution-concentrating boiler. A recovery unit, comprising: a supply unit that extracts the concentrated absorption liquid from the high-temperature regenerator and supplies the concentrated absorption liquid to the solution-concentrating boiler; refrigerant vapor generated from the solution-concentrating boiler serves as a heating source for the high-temperature regenerator. An absorption refrigerator, wherein the refrigerant drain is supplied, and the refrigerant drain heated by the exhaust gas heat recovery device is supplied to the low temperature regenerator as a heating source. 5. A low-temperature heat exchanger, wherein a second low-temperature heat exchanger is provided in parallel with the low-temperature heat exchanger, and a refrigerant drain from the low-temperature regenerator is supplied to the second low-temperature heat exchanger as a heating source. 4. The method according to claim 1, wherein
Or the absorption refrigerator according to 4. 6. A second low-temperature heat exchanger disposed in parallel with the low-temperature heat exchanger, wherein refrigerant drain from the high-temperature regenerator is supplied to the second low-temperature heat exchanger as a heating source. The absorption refrigerator according to claim 1, 2 or 3, wherein 7. A low-temperature heat exchanger provided in parallel with the low-temperature heat exchanger, wherein refrigerant drain from the low-temperature regenerator is supplied to the third low-temperature heat exchanger as a heating source. 7. The absorption refrigerator according to claim 6, wherein: 8. A high-temperature heat exchanger, wherein a second high-temperature heat exchanger is provided in parallel with the high-temperature heat exchanger, and refrigerant drain from the high-temperature regenerator is supplied to the second high-temperature heat exchanger as a heating source. 4. The method as claimed in claim 1, wherein:
The absorption refrigerator described. 9. A second low-temperature heat exchanger disposed in parallel with the low-temperature heat exchanger, wherein refrigerant drain from the high-temperature regenerator is supplied to the second high-temperature heat exchanger as a heating source. 9. The absorption refrigerator according to claim 8, wherein the refrigerant drain after the heat exchange in the second high-temperature heat exchanger is supplied to the second low-temperature heat exchanger. 10. The absorption refrigerator according to claim 9, wherein a refrigerant drain from a low-temperature regenerator is supplied as a heating source of the second low-temperature heat exchanger. 11. 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.
The absorption refrigerator according to 2, 3, 4, 5, 6, 7, 8, 9 or 10. 12. 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,
The absorption refrigerator according to 5, 6, 7, 8, 9 or 10. 13. The method according to claim 1, wherein cooling water is supplied from the condenser to the absorber.
The absorption refrigerator according to 6, 7, 8, 9, 10, 11 or 12. 14. The method of claim 1, wherein the solution concentration boiler is a once-through boiler.
An absorption refrigerator according to 8, 9, 10, 11, 12 or 13.